CN1688720B - Sugar juice purification system - Google Patents

Abstract

The present invention relates to a method of purifying the syrup obtained from plants, which includes the following step: The syrup (1) is exposed in gas (3) with a characteristic which can transfer at least one substance from the syrup into the gas, so that the quantity of the substance in the syrup is reduced. The present invention also relates to a syrup-purifying system used to realize the method, and a product produced by the method.

Description

Juice Purification System

This International Patent Cooperation Treaty (PCT) patent application claims the benefit of US Provisional Patent Application No. 60/403,594, which is hereby incorporated by reference.

technical field

The present invention relates to processing systems for the manufacture of sugar and other products from a sucrose-containing juice obtained from plant matter such as sugar cane, sugar beet or sweet sorghum. The invention also relates to an apparatus and a method for producing sucrose-containing juice with reduced dissolved matter content. The present invention also relates to the modification of conventional sugar production systems to produce or use such reduced sucrose-containing juices.

technical background

Sucrose, C ₁₂ H ₂₂ O ₁₁ , a disaccharide, is a condensed molecule linking a glucose monosaccharide and a fructose monosaccharide. Sucrose occurs naturally in many fruits and vegetables in the plant kingdom, such as sugar cane, sugar beet, sweet sorghum, sugar palm or sugar maple. The amount of sucrose a plant receives depends on the genetic strain, soil or fertilizer factors, weather conditions during growth, plant disease incidence, maturity, or handling between harvest and processing, among many factors.

Sucrose concentrates in certain parts of the plant, such as the stems of sugar cane plants or the roots of sugar beets. The whole plant or a part of the plant in which sucrose is concentrated can be harvested and the plant juice removed or extracted to obtain a juice containing a certain concentration of sucrose. Typically, methods of removing or extracting sugar juice from plant matter include milling, diffusion, pressing, or combinations thereof. Milling is a method traditionally used to extract sugar juice from sugar cane. Sugar cane can be cut into pieces of desired size and then passed through rollers to squeeze out the sugar juice. This process can be repeated several times along the series of mills to ensure that substantially all of the cane juice is removed.

Extraction is considered the traditional method of extracting the juice from sugar beets. Sugar beets are cut into small strips called "cossettes" which are then fed to one end of the extractor while an extracting solution, such as warm water, enters the other end. When using this convective process approximately 98% of the sucrose in cossette or sugar beet material can be extracted. The resulting sucrose-containing liquid is commonly referred to as "leaching juice". Beet couscous or beet flakes coming out of the extractor are still very wet, while their juice (88-92% water) still contains some sucrose. Therefore, these beet shreds or beet slices can be pressed in a screw press or other type of press in order to extract as much sugar juice as possible from them. This juice, commonly called "beet waste press water", has a pH of about 5 and is returned to the extractor in some cases. The resulting beet pulp (pulp) contains approximately 75% moisture. The addition of cationic charged press aids to the press feed can reduce the moisture content of beet waste by approximately 1.5 to 2%. Sucrose can also be extracted from sugarcane stalks by leaching. One method of extraction for sugarcane involves passing a moving bed of finely prepared sugarcane pieces through an extractor to enable leaching of sucrose from the sugarcane.

Extraction, milling, or other methods of extracting juice from plant matter or bringing plant juice into an aqueous solution to produce a juice containing sucrose, non-sucrose substances, and water. The nature and amount of non-sucrose matter in the juices obtained by these methods can vary and can include a variety of plant and non-plant derivatives, including but not limited to: insoluble matter such as plant fibers or soil particles; and soluble matter , such as fertilizers, sucrose, sugars other than sucrose, organic and inorganic non-sugar substances, organic acids, dissolved gases, proteins, inorganic acids, organic acids, phosphates, metal ions (such as iron, aluminum or magnesium ions), pectin , colored substances, saponins, waxes, fats or gums, their associated or linking parts, or their derivatives.

These non-sucrose species are often highly coloured, heat labile, or otherwise interfere with certain processing steps or negatively affect the quality or quantity of the sugar product resulting from the purification process. It has been estimated that, on average, one pound of non-sucrose material reduces the weight of the sugar product resulting from the purification process by 1 to 1.5 pounds. It is desirable to be able to separate or remove all or some of these non-sucrose materials from juice obtained by leaching, milling or other methods used to extract juice from plant matter. A good leaching operation can remove 25-30% of adulterated impurities. Recycled beet waste or carbonated press water can reduce this level to 17-20%, but it is still economical due to: heat recovery, saved make-up water, reduced wastewater pollution, recovered sugar .

Traditional processing systems utilize leaching, milling, or other methods for extracting sugar juice from plant matter (such as those described in U.S. Patent Nos. 6,051,075, 5,928,42, 5,480,490, each of which is incorporated herein by reference; Or "SugarTechnology, Beet and Cane Sugar Manufacture (Sugar Technology, Beet Sugar and Cane Sugar Production)" (1998) such as PW van der Poel et al; "Beet-Sugar Technology (Beet Sugar Technology)" edited by RAMcGinnis, third edition (1982 ); or the method described in James CPChen, CaneSugar Handbook of Chung Chi Chou: A Manual for Cane Sugar Manufacturers and TheirChemists (Sucrose Handbook: Manual for Cane Sugar Producers and Their Chemists), 12th Edition (1993), each literature all are hereby incorporated by reference) for the manufacture of the following: process juice (process juice); obtained from residual plant matter or from such process juice during its clarification, purification or refining Solids separated from sugar juice; sugar juice containing sugar or sucrose; sugar or sucrose crystallized from such sugar or sucrose juice; mother liquors of such sugar or sucrose crystallization, and products or derivatives thereof Combinations, permutations, each of which contains impurities in amounts compatible with the processing steps described herein, or any part thereof, or with the processing steps actually employed in its production, or with one or more of the following products Traditional Criteria Compliant Impurities: One of a class or a product including, but not limited to, animal feed containing plant matter from which sugar juice has been removed, such as leached beet chips, beet waste, bagasse, or Using other solids separated from sugar juice or sugar juice; using vegetable matter from which juice has been removed as fuel to generate energy to boil water to generate high-pressure steam to drive turbines to generate electricity, or to generate low-pressure steam for the processing system, or to generate Low-calorie; from pure sucrose solution syrups such as those sold to industrial users to syrups treated with added flavoring and coloring, or with invert sugar added to prevent crystallization of sucrose, such as brown molasses; by removing all or any molasses, or products derived from molasses, obtained from quantities of crystallizable sucrose or sugar, such as molasses (treacle); alcohols obtained by distillation from molasses; straight white sugars produced by sulfitation using sulfur dioxide (SO ₂ ) as a bleaching agent ( blanco directo) or plantation sugar; juggeri or jaggery produced by boiling juice containing sucrose or sugar until substantially dry; sugar juice obtained by melting refined white sugar or from syrup which may be further decoloured; in England or The rest of Europe is often referred to as the "unrefined sugar" or, in the North American natural food industry, "evaporated canejuice" (to describe the free-flowing single-crystal sucrose obtained with minimal processing); ground sucrose (milled cane); brown sugar (demerara); mixed sugar; rapedura; red granulated sugar; turbina; rough sugar containing 94 to 98% sucrose, the remainder being molasses, ash or other trace elements; refined sugar, such as water-white and containing at least 99.9% sucrose, extra fine grained and of a quality based on "bottled" designation by the National Soft Drink Association; specialty white sugar, such as caster sugar, rock sugar, cube sugar, or preserving sugar ; brown sugar obtained by spraying and blending white refined sugar with molasses, which may be light or dark brown sugar according to the characteristics of molasses; or various fine brown sugar obtained by grinding granulated sugar into powder in a mill 100% powdered sugar, which may further contain cornstarch or other chemicals to prevent clumping. This list does not represent a limitation on products produced by traditional sugar systems, but is meant to provide some examples of the variety of products produced by sugar systems.

It will be appreciated that part of the conventional processing system includes steps of progressive clarification, purification or refining of juice obtained by leaching, milling or other methods used to extract juice from plant matter. Typically, one or more mechanical methods, such as sieving, can be used to remove some of the insoluble or suspended matter from plant matter-derived sucrose-containing juices. The resulting sieved juice, when derived from sugar beets, may contain about 82% to 85% by weight water, about 13 to 15% by weight sucrose, about 2.0 to 3.0% by weight dissolved non-sucrose matter or impurities, and a certain amount of residual insoluble matter.

Typically, the resulting sucrose-containing juice at a volume of 1000 to 2500 gallons per minute can be treated by gradually adding alkali to raise the pH of the juice. In some conventional processing systems, the pH of the juices can be raised from between about 5.5 pH to about 6.5 pH to between about 11.5 pH to about 11.8 pH so that some of the non- Sucrose species can reach their respective isoelectric points. This step is commonly referred to as "preliming". However, the latter use of this term is not intended to limit the step of adding alkali to sucrose-containing juices to only those processing systems in which such alkali addition is referred to as "preliming". It should be understood that in various conventional juice processing systems it is desirable to first raise the pH of the juice with an alkali, followed by a processing step such as the filtration step described in US Patent Nos. 4,432,806, 5,759,283, etc.; Ion exchange steps as described in Patent No. 1,043,102 or U.S. Patent Nos. 3,618,589, 3,785,863, 4,140,541 or 4,331,483, 5,466,294, etc.; as described in U.S. Patent Nos. 4,432,806 et al.; phase separation as described in U.S. Pat. No. 6,051,075; process system for adding active material to the final carbonator as described in U.S. Pat. An alternative to the traditional juice processing step of carbonation, the above references are hereby incorporated by reference.

Use of the term "alkali" includes the use of substances capable of raising the pH of the juice, including, but not limited to, the use of lime or the underflow of a process employing lime. Use of the term "lime" generally includes the specific use of quicklime or calcium oxide produced by heating calcium (usually in the form of limestone) in oxygen. Milk of lime is preferred in many juice processing systems, consisting of a calcium hydroxide (Ca(OH) ₂ ) suspension according to the following reaction:

The term "isoelectric point" includes the pH value at which dissolved or colloidal substances (eg proteins) in juice have a zero potential. When these dissolved or colloidal substances reach their assigned isoelectric point, they can form many solid particles, flocs or cotton wool.

Calcium carbonate substances may be added to the juice to further enhance flocculation, which functionally forms a core or substrate to which solid particles or flocs can bind. The process increases the size, weight or density of the particles, thereby facilitating the filtration or settling of these solid particles or materials and their removal from the juice.

The resulting mixture of juice, residual lime, excess calcium carbonate, solids, flocculant or cotton wool can then be fed to subsequent processing steps as described above. In particular, with respect to processing systems for clarification, purification or refining of juice from previous sugar beet processing, the mixture may first be subjected to a cold main liming step so that the preliming The solid formed in this step was stable. This cold main liming step may include the addition of about 0.3-0.7 wt% of additional lime (or more depending on the mass of the prelimed juice) at a temperature of about 30°C to about 40°C. ).

The cold main liming juice is then subjected to hot main liming to further degrade the invert sugar and other components unstable to this step. Hot main liming may include further addition of lime to raise the pH of the limed juice to a level between about 12 pH and about 12.5 pH. This results in a partial breakdown of soluble non-sucrose species unaffected by previously added alkali or lime. Specifically, hot primary liming of limed juices can be thermally stabilized by partial decomposition of invert sugars, amino acids, amides, and other dissolved non-sucrose species.

After cold or hot main liming, the main liming juice may be subjected to a first carbonation step in which carbon dioxide gas is mixed with the main liming juice. The carbon dioxide gas reacts with the residual lime in the main limed juice to form calcium carbonate in precipitated form. Not only is residual lime removed by this procedure (typically about 95% by weight of residual lime is removed), the surface active calcium carbonate precipitate also captures a considerable amount of remaining dissolved non-sucrose. In addition, calcium carbonate precipitates can also act as filter aids in the physical removal of solid matter from primary liming and carbonated juices.

The clarified juice resulting from the first carbonation step may then be fed to an additional liming step, heating step, carbonation step, filtration step, membrane ultrafiltration step, chromatographic separation step or ion exchange step, or a combination thereof, as described above, A displacement or derivatization step to further clarify or purify the juice obtained in the first carbonation step to produce a processing juice commonly referred to as "thin juice".

This further clarified juice or "thin juice" may be thickened by evaporating some of the water to obtain a product traditionally known as "molasses". Evaporation of part of the water can take place in multi-stage evaporators. This technology is used because it is an efficient way of using steam and if required, it also produces another low-grade steam that can be used to drive the subsequent crystallization process.

Thickened clarified sugar juice or "syrup" can be placed in a container that can usually hold 60 tons or more. In this vessel, boil to evaporate more water until conditions are suitable for sucrose or sugar crystal growth. Because it may be difficult to get crystals of sucrose or sugar to grow well, some sucrose or sugar seeds are added to initiate crystal formation. Once the crystals have grown, the resulting mixture of crystals and remaining juice can be separated. Traditionally, the two substances are separated using a centrifuge. The separated sucrose or sugar crystals are then dried to the desired humidity prior to packaging, storage, transport or further refining or the like. For example, raw sugar can be refined after it is shipped to the country of use.

A competitive global commercial market exists for products derived from plant matter and juices containing sucrose. The market for products derived from sucrose-containing plant matter is large enough that even a slight reduction in the cost of a single processing system step would save considerable and desirable levels of money. Therefore, there is a huge incentive for independent researchers and distributors who can benefit from new processing system chemicals and equipment to conduct research on the sugar industry's sugar processing or juice system to obtain processing system savings, and in some In some cases, additional compensation based on the percentage of savings in the process when improvements are made is another motivation.

However, even after processing systems for the purification of sucrose-containing juices obtained from certain plant matter have been established and improved for at least 1000 years, especially for sugar beets, industrial processing systems have existed for more than 100 years, and Even though there is a huge incentive to promote improvements in sugar or juice processing systems, significant problems remain with regard to the processing of juice obtained from plant matter.

A significant problem with conventional sugar production systems is the cost of obtaining and using a base such as calcium oxide to raise the pH of the sucrose-containing liquid or juice obtained from the plant matter. As mentioned above, calcium oxide or calcium hydroxide can be added to the juice to raise the pH so that some dissolved matter can come out of solution as solids, flocs or lint. Calcium oxide is usually obtained by calcining limestone, in which the limestone is heated in the presence of oxygen in a kiln to liberate carbon dioxide, forming calcium oxide.

As shown in Figure 5, calcination is expensive because it requires the purchase of a kiln (40), limestone (41) and fuels (42) such as gas, oil, coal, coke, etc., which can be burned to increase the temperature in the kiln to Sufficient to release carbon dioxide (43) from limestone (41). Auxiliary equipment for the delivery of limestone and fuel to the kiln and for removal of the resulting calcium oxide from the kiln must be accompanied by equipment for scrubbing certain kiln gases and particles from the kiln exhaust gases emitted during the limestone calcination process. Naturally manpower must be available to operate and maintain the equipment, as well as to monitor the quality of the calcined limestone produced and also to monitor the removal of gases and particles released during kiln operation.

In addition, the calcium oxide produced by calcination must be converted to calcium hydroxide for use in typical juice processing systems. This in turn involves purchasing equipment to reduce the calcium oxide into particles of the appropriate size and mixing these particles with water to produce calcium hydroxide. Likewise, manpower must be available to operate and maintain the equipment.

Finally, the investment in equipment and manpower associated with the use of calcium oxide increases with the amount used. This includes the added expense of additional manpower for mixing the extra calcium hydroxide with the juice, or it may include the added expense of using higher load capacity or more powerful equipment.

Another significant problem associated with the manufacture and use of base in conventional processing systems is the disposal of excess base or the products formed when base reacts with dissolved organic or inorganic acids in sugar juice. For example, when a processing system uses one or more carbonation steps in the clarification or purification of juice, the amount of calcium carbonate or other salts produced, commonly referred to as "waste lime," is proportional to the amount of lime added to the juice. proportional. Simply put, the greater the amount of lime added to the juice, the greater the amount of precipitate that will typically be formed during the carbonation step. "Carbonated lime" can be allowed to settle to the bottom of the carbonation vessel, forming what is sometimes called "caustic sludge". The sludge can be separated by rotary vacuum filters or plate and frame presses. The product that is then formed is called "lime cake". Thin filter sludge or caustic sludge can be mostly calcium carbonate precipitates, but can also contain sugars, other organic or inorganic matter, or water. These separated sediments are almost always treated separately from other process system wastes and can, for example, be slurried with water and pumped into clarifiers or areas bounded by dikes or sent to land fills.

Alternatively, carbonated lime, caustic sludge or thin filter sludge can be recalcined. However, the cost of recalcination kilns and peripheral equipment for waste lime is much more expensive than kilns for calcining limestone. Furthermore, the quality of recalcined "carbonated lime" is not the same as that of calcined limestone. The purity of calcined limestone compared to re-calcined carbonated lime may be, to name just one example, 92% versus 77%. Accordingly, the amount of recalcined lime required to neutralize the same amount of hydronium ions in the juice is correspondingly higher. Likewise, waste lime has a much higher carbon dioxide content than limestone. Therefore, not only is the production of recalcined limestone expensive, but it also requires the use of much larger gas conduits and equipment to transfer the _CO2 generated when recalcined spent lime, larger conveying carbonation tank, or similar equipment.

In addition, the greater the amount of lime used in a particular processing system, the more expensive it is generally to dispose of the spent lime, whether it is disposed of in a pond, landfilled in a pond, or through recycling.

Another significant problem with traditional sugar systems is that the throughput of the processing system decreases with the amount of lime used in the processed sugar juice. One aspect of this problem is the limited amount or rate of lime being produced or supplied to the juice processing step. As mentioned above, limestone must be calcined to make calcium oxide before it can be used as a base in juice processing systems. The amount of lime obtained is limited by limestone utilization, kiln capacity, fuel utilization or similar factors. The rate at which lime is produced to feed the juice processing system may vary depending on the size, type and amount of lime generating equipment, available manpower or the like. Another aspect of the problem is that the amount of lime used in the processing system proportionally reduces the volume of the processing system used to hold the juice. An increase in the amount of alkali such as lime also requires the use of larger volume zones, conduits or similar equipment to maintain the same volume of juice processed.

Another significant problem with traditional sugar systems is the excess acid produced in the plant matter prior to extraction of the plant's sugar juice. Organic acids act as a buffer system in the acid-base balance of plant cells, thereby maintaining the desired pH in plant tissues. The sources of these acids can be divided into two groups, the first being acids absorbed by plants from the soil during the growth cycle and the second being acids formed by biochemical or microbial action. When acid uptake from the soil is insufficient, plants synthesize organic acids, mainly oxalic, citric, and malic acids, to maintain a healthy pH in plant cell fluids. Therefore, the sugar juice extracted from plant tissue contains a certain amount of various organic acids.

In addition to this organic acid, which occurs naturally in plant tissues, acids can also be formed during storage, mainly by the action of microorganisms. Severely deteriorated plant matter may produce large amounts of organic acids, mainly lactic, acetic, and citric acids. The total acid content in plant tissues can triple or more in some cases.

In addition, carbon dioxide (CO2) is produced in plant tissues due to disruption of the natural alkalinity in the sugar juice. During this process, bicarbonate and carbonate ions are converted into carbon dioxide. The resulting carbon dioxide, which remains in solution, produces carbonic acid, which is a source of hydronium ions. All or part of the organic acids contained in the plant cell fluid are retained in the sugar juice obtained from the plant. Therefore, in order to raise the pH of the juice, it is necessary to neutralize these organic and inorganic acids with alkali. The higher the concentration of organic or inorganic acids in the juice, the greater the amount of alkali required to raise the pH of the juice to the desired value.

Another significant problem with conventional sugar systems is that plant matter or juice treated with antimicrobial chemicals has a higher acid content than untreated plant matter or juice. For example, sulfur dioxide (SO ₂ ) or ammonium bisulfite (NH ₄ HSO ₃ ) can be added continuously or intermittently to help control microbial growth or infection. The amount of SO _added depends on the severity of microbial growth or infection. The amount of lactic acid and nitrite can be monitored or tracked to determine the severity of microbial growth or infection. Up to approximately 1000ppm _SO2 can be used to shock or treat infected systems. Up to 400-500ppm can be added continuously to control infection. The addition of SO ₂ or NH ₄ HSO ₃ for antimicrobial protection lowers the pH and alkalinity of the juice. Alkalinity decreases due to the conversion of naturally occurring bicarbonate ions to _CO2 , or carbonic acid.

Another significant problem with conventional sugar production systems is the formation of scale in vessels such as evaporators or sugar crystallization equipment. The calcium salt of oxalic acid usually constitutes the main constituent of scale. Oxalate has low solubility in solution which decreases with increasing calcium levels in solution. Even after the juice has been purified to become "thin" or "thick" juice, there is enough calcium in solution to cause the oxalate to come out of solution. Methods of removing scale from equipment surfaces are expensive, including but not limited to costs associated with slowed production and loss of efficiency, or reduced useful life of the equipment.

Another significant problem with conventional sugar production systems is the failure to recognize that the juice extraction equipment or methods used to obtain juice from plant matter can alter or lower the pH of the extracted juice. With regard to extractors for extracting juice from sugar beet material, it is not recognized that the pH of sugar beet juice can be altered or lowered during the extraction process. Another aspect of the problem is the failure to recognize that different equipment or different methods used to extract juice from sugar beet material alter or lower the pH of the resulting juice to different degrees. Improvements in extraction techniques have generally produced juices with increasingly lower pH values, and as such, these devices and methods have come a long way from the solutions provided by the present invention.

Another problem with traditional sugar systems is that organic matter, dissolved gases or other substances that are soluble in, or added to, the juice extracted, removed or leached from sugar beets, The preliming step of traditional sugar purification cannot be brought to equilibrium or reached equilibrium with atmospheric partial pressure or selected partial pressure gas mixture before. Thus, the transfer of dissolved substances from the extracted, removed or leached juice to the atmosphere or other selected gas mixture, thereby reducing the partial pressure or concentration of those dissolved substances in the leached juice, is still being carried out Preliming, initial liming, lime addition steps before or at the same time directly contribute to or in combination with other pH adjustment methods in the juice to indirectly contribute to the reduction of the pH value of the leach juice. As mentioned above, a lower pH can result in the use of more lime to achieve the desired pH of the juice.

Concerning the traditional extraction of sugar beet silk (or other traditional methods of removing or extracting sugar juice or substances from the plant matter), one aspect of which is traditional extraction equipment or used to remove or extract sugar from the plant matter Other conventional equipment for extracting juice or other substances cannot or is insufficient to provide a surface interface between the extracted juice or the liquid containing the extracted or removed plant matter and the atmosphere or other selected or desired gas mixture (the interface is used In order to bring the substances dissolved in the leach juice or other liquid containing extracted or removed vegetable matter to an equilibrium, so as to reduce the concentration of these substances in the sugar juice or other liquid containing extracted or removed vegetable matter. concentration.

Another aspect of the problem is that traditional sugar beet-extraction methods or equipment (or other traditional equipment used to remove or extract juice or other substances from plant matter) cannot provide atmospheric partial pressure or other selected conditions within the equipment. Sufficient recirculation of partial pressure gases to maintain a partial pressure difference between the concentration of solutes in juice or other liquids containing plant matter that has been extracted or removed The pressure gas is potentially equilibrated to effectively achieve a desired, potential or possible reduction in pH lowering species in leach juice or other liquids containing plant matter that has been extracted or removed. Thus, partial or complete equilibrium between the partial pressure of gas present at the liquid interface and the partial pressure of gas in solution prevents or slows down further reductions in the concentration of pH-lowering substances, compounds or gases in the leach juice.

The third aspect of the problem is that traditional sugar beet-extraction methods or equipment (or other traditional equipment or methods for removing or extracting juice or other substances from plant matter) do not mix the extracted juice sufficiently well to The entire volume or a sufficient volume of leach juice (or other liquid containing plant matter that has been extracted or removed) to cause the pH to drop tends toward equilibrium with the atmosphere or other gaseous mixture at the liquid-air interface.

A fourth aspect of the problem is that traditional sugar beet-extraction methods or equipment (or other traditional equipment or methods for removing or extracting juice or other matter from plant matter) do not leach juice or other The liquid of the extracted or removed plant matter is heated to a temperature sufficient to reduce the solubility of the leach juice or other liquid containing the extracted or removed plant matter to a point where the concentration of the pH-lowering substance tends towards the liquid- The concentration in or in equilibrium with a partial pressure of a gas present at a gas interface, or to move the point of equilibrium so as to reduce the concentration of a pH-lowering substance to a desired, potential, or possible concentration; potential or possible at a desired rate or desired or achievable The equilibrium rate of the gas tends to or reaches equilibrium with the partial pressure gas at the gas-liquid interface.

Another significant problem with conventional sugar systems is that the extracted or leached juice can tend to equilibrate or reach equilibrium with atmospheric partial pressure or other gas mixtures containing higher concentrations of pH-lowering species present on the surface of the juice as it cools. As the leach juice or other liquid containing plant matter that has been extracted or removed cools, the solubility of the atmosphere or other gas mixture increases. Thus, as the leach juice cools, the concentration of gases or other substances soluble in the juice, including but not limited to pH lowering substances, increases. As just one example, when the leach juice is cooled in the leaching step from between about 55°C to about 70°C to between about 20°C and about 30°C prior to the preliming or liming step, the atmospheric _CO2 Solubility increases. The amount leached from the juice when exposed to an atmospheric partial pressure of _CO2 or to any gas mixture with a partial pressure of _CO2 sufficient to transfer _CO2 into the juice as it cools, relative to when the temperature is higher The CO ₂ concentration is increased. The elevated _CO2 concentration in the leach juice will lower the pH of the juice. Therefore, increased concentrations of _CO2 or other gases in the leach juice require the addition of more lime in subsequent liming, preliming or other liming steps to achieve the desired or necessary pH.

Another problem with conventional sugar systems is that the partial pressure of gas at the gas-liquid interface of leach juice or other liquid containing plant matter that has been extracted or removed effectively builds up sufficient to Concentration gradient in which a necessary or desired portion of the liquid of extracted or removed plant matter is volatilized, mobilized, removed, or otherwise transferred to sufficiently raise the pH of the leach juice or to reduce the pH-lowering substance in the leach juice concentration.

The present invention provides a sugar juice processing system, which includes equipment and methods for solving the above-mentioned problems.

Contents of the invention

Therefore, the main object of the present invention is to provide a juice processing system for preparing products from sucrose-containing liquid or juice obtained from plant matter. One aspect of this main purpose is to provide an alternative to traditional juice or sugar processing systems. Thus, the present invention provides a complete processing system, including equipment and methods, for obtaining products from liquids or juices containing sucrose. A second aspect of this main objective is to provide a juice processing system method that is compatible with conventional juice or sugar processing system methods. With regard to this purpose, the present invention provides method steps and devices which can further add to, replace or modify conventional methods and devices for processing sucrose-containing liquids or juices.

A second main object of the present invention is to reduce the cost of preparing products from liquids or juices containing sucrose. One aspect of this object of the invention is to increase the throughput of juice processing which is wholly or partly limited by the availability of alkali, for example by reduced availability of limestone or insufficient ability to convert limestone to calcium oxide, or similar factors . Another aspect of this object is to provide cost savings by reducing the amount of alkali (eg lime) that must be used to process a sucrose-containing liquor or juice into a product. A third aspect of this object of the invention is the reduction of the amount of waste generated, for example reducing the amount of spent lime.

The third main object of the present invention is to provide a liquid product or juice product containing sucrose obtained by using the present invention. One aspect of this object is to provide a sucrose-containing liquid or juice product with reduced content or concentration of dissolved substances such as water soluble acids, volatile organic compounds, dissolved gases (eg _CO2 or _SOs ), ammonia, or the like. A second aspect of this object is to provide a sucrose-containing liquid or juice product having a higher pH after treatment according to the invention. A third aspect of this object is to provide a sucrose-containing liquid or juice product having a higher pH after treatment according to the invention without the use of any alkali. A fourth aspect of the present invention is to provide a sucrose containing liquor with a higher pH even when a certain amount of alkali such as lime or underflow from conventional juice processing or similar has been added prior to treatment according to the present invention or syrup products. A fifth aspect of this object is to provide a sucrose-containing liquid product or juice product having a reduced ability to generate hydronium ions. A sixth aspect of this object of the present invention is to provide a liquid or juice product containing sucrose that requires less alkali to raise the pH to the desired value, isoelectric focusing of the lysates, and pretreatment in conventional processing systems. The liming or main liming step, which degrades invert sugar or otherwise obtains a product from a sucrose-containing liquid or juice.

A fourth main object of the present invention is to provide methods and apparatus for reducing the content or concentration of dissolved substances in juice obtained by conventional juice extraction procedures such as pressing, milling or leaching. One aspect of this object is to provide a method for reducing the level or concentration of solutes without, without, requiring, or prior to the addition of base. A second aspect of the present invention is to provide a method of reducing the level or concentration of dissolved matter in a sucrose containing liquid or juice which can be used before, during or after adding alkali to the juice. A third aspect of this object is to provide a method which facilitates a reduction in the level or concentration of dissolved substances in a sucrose-containing liquid or juice. A fourth aspect of this object is to provide a method for rendering sucrose-containing liquid or juice in juice compatible with conventional juice clarification or purification methods including but not limited to preliming, main liming, ion exchange or filtration as described above. Methods of solute reduction.

A fifth main object of the present invention is to provide apparatus and methods for increasing the interfacial area between a sucrose-containing liquid or juice and a desired partial pressure of gas.

A sixth main object of the present invention is to provide various devices for infusing, adding or otherwise mixing gases at desired partial pressures in juice obtained from plant matter. One aspect of this object is to provide apparatus for injecting a gas mixture into juice to provide a mixed flow of juice comprising juice and gas at a desired partial pressure.

A seventh main object of the present invention is to provide apparatuses for separating or removing partial pressure gases contained or dissolved in a gas mixture which has been brought into partial or complete equilibrium with a dissolved substance, or in a sugar juice.

The eighth main object of the present invention is to evaluate, monitor, manufacture or preserve a liquid containing extracted or removed plant matter at a temperature (which may be adjusted manually or automatically) in response to or adjusted relative to: the time elapsed; the concentration of any particular substance or component contained therein; the specific process or steps by which the liquid is purified or otherwise processed; the method by which the substance is extracted, removed or leached from the plant; Or any manner of preparation or storage of such a liquid for setting the solubility of a substance that controls the concentration of a substance that lowers or potentially lowers the pH of such a liquid to a range or specific value.

A ninth main object of the present invention is to provide a solution for the treatment of leached sugar juices or liquids containing substances extracted or removed from plant matter prior to initial and subsequent lime additions in order to prevent separation at the liquid-air interface. pressure gas, minimize it, or control it. equipment and methods.

A tenth main object of the present invention is to provide a solution that allows the required or necessary volume of juice to interact with the liquid-air interface so that substances can be transferred from the extracted juice to atmospheric partial pressure or selected partial pressure as desired or necessary. Apparatus and methods in pressurized gas.

Naturally, other objects of the invention are disclosed in the rest of the description and drawings.

Description of drawings

Figure 1 shows an embodiment of the present invention for reducing the substance content of juice obtained from plant matter, comprising sugar with a gas mixture delivered into the juice to produce a mixed stream of juice and gas mixture A juice delivery device further comprising a gas distribution element, such as a pipe or groove in a juice delivery device, or an impeller of a pump.

Figure 2 shows a specific embodiment of the invention for producing juice with reduced substance content.

Figure 3 shows a second embodiment of the invention for producing juice with reduced substance content.

Figure 4 shows a third embodiment of the invention for the production of reduced substance juice.

Figure 5 shows an embodiment of the present invention for producing reduced substance juice which further comprises the use of liming and carbonation to further render this juice prior to reducing the water content to produce a syrup or prior to sugar crystallization Clarify or purify.

Figure 6 shows an embodiment of the present invention for producing reduced substance juice which further comprises the use of ion exchange to further clarify or purify such juice prior to water reduction to produce syrup or prior to sugar crystallization .

Figure 7 shows an embodiment of the invention for producing reduced substance juice which further comprises a filtration step such as ultrafiltration to further clarify such juice prior to reducing the water content to produce a syrup or prior to sugar crystallization or purification.

Figure 8 shows the solubility of certain substances, materials or components contained in juices, extract juices or other juice processing liquids as the temperature of these juices, extract juices or other juice processing liquids increases will decrease.

Figure 9 shows several embodiments of the present invention for processing sugar beet silk by reducing certain substances in the pulp juice or leach juice prior to the preliming step.

Figure 10 shows another embodiment of the invention for processing sugar beet silk by reducing certain substances in the pulp juice or leach juice prior to the preliming step.

Figure 11 shows a specific embodiment of the present invention.

Figure 12 shows a top view of an embodiment of the invention, showing section A-A.

FIG. 13 shows a side view section A-A of the embodiment shown in FIG. 12 .

Detailed ways

In general, the present invention includes juice processing systems that purify juice with no or less alkali addition prior to evaporation of excess water or fractional crystallization of sucrose. In particular, the present invention provides juice with reduced dissolved matter content, reduced dissolved gas, higher pH, or lower alkalinity for use in a juice purification system.

As mentioned above, sugar juice can be obtained from plant matter such as sugar beet, sugar cane, sweet sorghum. Naturally, there may be large commercial or niche markets for products for which the juice must be derived from other kinds of plant matter, and it should be understood that the present invention is not limited to harvesting from any particular kind of plant or Sugar juice removed, extracted or obtained from a plant or any part of a plant. Furthermore, the term juice may be broadly understood as any juice or liquid containing sucrose at any step of any processing system prior to sugar crystallization. Thus, sucrose-containing liquids obtained from plant matter by milling or pressing steps, or juices obtained from the step of leaching plant matter are two examples of sugar juices. As stated above, the term juice includes a liquid containing sucrose, non-sucrose matter and water in varying proportions, depending on the nature of the plant matter and the steps used to remove the juice from the plant matter. Removal or partial dissolution may be desirable because they are highly colored, thermally unstable, or otherwise interfere with certain processing steps or negatively affect the quality or quantity of the sugar product obtained from the purification process. The term juice also includes sucrose-containing liquids resulting from these various clarification or purification steps.

Embodiments of the invention include the removal of at least a portion of dissolved matter, volatiles, dissolved gases, water-soluble acids, or the like, such as carbon dioxide or sulfur dioxide capable of forming water-soluble acids, which produces hydronium ions in solution, altering the The concentration of hydronium ions or decrease the pH of the juice.

For example, when the juice contains enough cations, the hydroxide ion OH- can act as an anion, which can make carbon dioxide CO ₂ in the form of carbonate ion (CO ₃ ) ^-2 , or in the form of bicarbonate ion HCO ₃ ^- Dissolved in sugar juice. The dissociation of HCO ₃ ^-provides a very weak acid. However, an equilibrium occurs between carbon _dioxide and carbonated _H2CO3 when the juice contains insufficient cations for the dissolved _CO2 to form carbonate or bicarbonate ions. Carbonic acid can act as a strong acid in the pH range at which juice is prepared. The subsequent generation of hydronium ions increases the existing concentration in the juice, resulting in a decrease in pH.

Similarly, sulfur dioxide (SO ₂ ) or ammonium bisulfite (NH ₄ HSO ₃ ) can be added to juice to control, reduce, or eliminate microbial activity, sucrose hydrolysis, invert sugar formation, or loss of sucrose, or to lower the pH Turn down. Likewise, sulfites such as calcium sulfite are produced when the juice contains sufficient cations, such as calcium. However, when the number of cations contained in sugar juice is not enough to form sulfite from dissolved sulfur dioxide (SO ₂ ), between sulfur dioxide (SO ₂ ), sulfurous acid (H ₂ SO ₃ ) and sulfuric acid (H ₂ SO ₄ ) There will be a balance between. Sulfuric acid and sulfurous acid can act as strong acids. The subsequent production of hydronium ions increases the existing concentration in the juice, resulting in a lower pH.

In addition, other water-soluble acids are produced by plants during normal growth and by microbial action, including but not limited to phosphoric acid, hydrochloric acid, sulfuric acid, citric acid, oxalic acid, succinic acid, fumaric acid, lactic acid, glycolic acid, pyrrolidone -Carboxylic acid, formic acid, acetic acid, butyric acid, maleic acid, lactic acid, etc.

In addition, the breakdown of amino acids or the conversion of substances such as ammonium bisulfite added to the juice can produce other solutes.

Referring now primarily to FIG. 1 , an embodiment of the present invention may include increasing the interfacial surface area (4) between the juice (1) and the mixture (3) by allowing the Sugar juice (1) is exposed to gas mixture (3) total. By increasing the interfacial surface area (4) between the juice (1) and the gas mixture (3), when the concentration of each component of the solute (5) tends to reach the concentration of that component in the gas mixture (3) At equilibrium, the rate of transfer of the various dissolved substances (5) from the juice (1) to the gas mixture (3) can be increased. The gas mixture (or stripping gas) can be selected to provide the partial pressure required to transfer unwanted dissolved matter (5) from the juice (1) into the gas mixture (3). The gas mixture (3) can be regenerated, or the partial pressure gas can be adjusted continuously or intermittently over the increased interfacial surface area (4) with the juice (1) to prevent the gap between the gas mixture (3) and the dissolved matter (5). Equilibrium, whereby dissolved substances (5) are continuously transferred from the juice to the gaseous mixture (3).

When using the present invention, dissolved or volatile matter, such as volatile inorganic compounds, volatile organic compounds or dissolved gases such as carbon dioxide, sulfur dioxide or ammonia, can be removed from juice. Compared with the same sugar juice without using the present invention, the sugar juice product obtained by using the present invention has reduced dissolved matter content, reduced dissolved gas, reduced ability to generate hydronium ions or concentration of hydronium ions, lower alkalinity or lower pH value. high. As just one example, the concentration of carbon dioxide in the juice can be substantially reduced when the juice is stripped using atmospheric partial pressure. The pH value of the sugar juice product obtained by the method can be increased by 0.05pH, 0.1pH, 0.2pH, 0.3pH, 0.4pH, 0.5pH, 0.6pH, 0.7pH, 0.8pH, 0.9pH, 1.0pH, 1.1pH, 1.2pH , pH1.3, pH1.4, pH1.5, pH1.6, pH1.7, pH1.8, pH1.9, 2.0pH, however, any degree of pH Any upward adjustment of the value can save considerable money and is commercially important. The actual amount of upward adjustment from the initial pH value will generally depend on the type and quality of juice treated by the present invention, the degree of increase in interfacial surface area resulting from the volume of the juice, and the duration of time the gas mixture responds to the increased interfacial surface area , and the partial pressure provided in the gas mixture. Thus, depending on the particular embodiment of the invention used, the amount of upward adjustment in pH varies. For example, varying the volume or amount of juice processed per unit of time, while otherwise using the same embodiment of the invention, can produce different increments in pH change.

The present invention still further comprises the step of: making the pH value, hydronium ion concentration or alkalinity necessary or desired in comparison with untreated juice or juice treated by conventional methods, The amount of alkali added in the sugar juice treated by the present invention is reduced. After reducing the dissolved matter in the juice treated according to the present invention, much less alkali can be added to achieve the desired pH, for example between about 11.0 and about 12.0, or between about 11.5 and about 12.5, Either for "preliming", "main liming", "interliming" pH ranges, or to achieve a pH corresponding to the isoelectric point of any particular non-sucrose species in the juice, or to achieve the The acidity or alkalinity is adjusted to the desired pH of the specified concentration. With regard to lime usage, for example, using various embodiments of the present invention can reduce usage by up to about 30% compared to untreated juice or juice treated by conventional methods.

Referring now primarily to FIG. 2, an embodiment of the invention includes a gas mixture (3), which may contain atmospheric gas or air, passed through one or more filters to reduce or substantially eliminate non-biological or biological particles (e.g. bacteria, viruses , pollen, microscopic flora or fauna, or other pathogens), atmospheric gases or air that have been subjected to chemical scrubbers or otherwise treated to produce the desired partial pressure gas concentration or concentration range, purified gases , or a combination or replacement thereof.

Embodiments of the invention may further include a gas filter (6) responsive to the flow of the gas mixture (3). The gas filter (6) can be located before or after the flow generator (7) which is fluidly responsive to the gas mixture (3). The gas filter (6) responsive to the flow of the gas mixture (3) may comprise a Hepa filter or an Ulpa filter or other type of macro or micro particle filter. Other pre-filters may also be used to capture particles in the gas mixture before entering the flow generator (7), or may be used after the flow generator (7) but before the gas filter (6).

The unfiltered air mixture (3) can be drawn into the primary pre-filter (8), then through the secondary pre-filter (9), and then through the air flow generator (7). The pre-filtered gas mixture is then passed through a gas filter (6) (HEPA filter, or UHEPA filter or other type of filter). The resulting filtered air mixture (removes 99.99% of all particles down to about 0.3 microns from the gas mixture (3) when using a HEPA filter), from the gas mixture (3) when using an ultra-high efficiency air filter ) to remove up to 99.99% of particles as small as about 0.12 microns) can then create or respond to increased interfacial surface area (4) between juice (1) and gas mixture (3). As for other embodiments of the invention, the gas mixture (3) or the juice (1) can be exposed to a source of short wavelength ultraviolet radiation (10) to reduce the number of pathogenic or bacterial particles. The invention may further comprise a temperature control device (11) to bring the gas mixture (3) to a desired temperature prior to responding to the juice (1) or increased interface surface area (4). The temperature control device (11) can be made to respond to a temperature sensor (12) which detects the temperature of the gas mixture (3) or juice (1) and sends a signal or causes the temperature control device (11) to change the temperature of the gas mixture (3) ) and/or the temperature of the juice (1) is adjusted to the desired temperature.

For some embodiments of the invention, the gas mixture (3), whether filtered or not, can be used to form or assist in the formation of the increased interfacial surface area (4). For example, the juice (1) may be fed into the gas injector (13) by gravity feed or under pressure generated by a pump (14) or other liquid delivery element. The gas injector (13) may have an inlet (15) through which juice (1) enters the gas injector (13), an outlet (16) through which juice (1) exits the gas injector (13), at least one gas The mixture (13) is fed through the injection port into the injection port (17) in at least part of the sugar juice (1) contained in or passed through the gas injector (13).

When the gas injector (13) has a configuration for batch processing of sugar juice (the gas injector is periodically fed and emptied), for some embodiments of the invention, the inlet (15) and outlet (16) may be same mouth. When the gas injector (13) is equipped for pulse flow processing (the juice (1) flow can be periodically reduced or interrupted to increase the residence time of the juice (1) in the gas injector (13)) or continuous flow processing (the liquid flow of sugar juice (1) flows continuously through the gas injector (13), and the rate or volume of the sugar juice flowing through the gas injector (13) can be adjusted), the inlet (15) and outlet (16) can be separated .

For each specific embodiment of the present invention, the gas mixture (3) can be injected into the sugar juice (1) under sufficient pressure, or in a certain distribution mode (such as diffusion or in the form of small bubbles) to The desired increased interfacial surface area (4) is created between the juice (1) and the gas mixture (3). The increased interface surface area (4) may provide an interface through which at least part of the dissolved matter (5) in the juice may transfer from the juice (1) to the gas mixture (3).

Whether it is configured to operate in a batch, pulsed, batch or continuous embodiment of the invention, the gas injector (13) may further agitate, run, agitate or otherwise provide a mixing device (18) to allow the gas mixture (3) Further distribution into the juice (1) to further increase the interfacial surface area (4). When the gas injector (13) is configured to generate a flow of juice (1), whether produced continuously, pulsatingly or intermittently, injecting the gas mixture (3) into the juice (1) produces a mixed flow of juice ( 19). The gas mixture in the juice mixing stream (19) can be further distributed in the juice mixing stream (19) by means of extensions, channels or the like connected to the inner surface of the gas injector (13). These add-ons or pipes are oriented to create the desired disturbance to the juice flow in the gas injector (13). The invention may further provide an injection pressure regulating device (20) to which the gas flow generator (7) responds to increase or decrease the pressure or amount of the gas mixture injected, mixed or sprayed into the juice (1). In some embodiments of the present invention, the injection pressure adjusting device (20) may independently or in combination comprise a variable adjustable limiting device located between the gas flow generator (7) and the injection port (17).

With respect to certain embodiments, the present invention can produce more fully dissolved gases in the juice than the initial concentration of the juice. It can reach about 10 times the concentration obtained by saturating the juice at atmospheric pressure. The pressure of the gas mixture (3) injected into the juice (1) can be between the initial pressure exerted by the juice (1) and a pressure of about 20 bar.

Multiple gas injectors (13) in series or in parallel may be used, and each gas injector in parallel or in series may have multiple gas injection ports (17) at substantially the same location or at different locations. Each injection port (17) can independently or variably control the volume and pressure of the gas mixture (3) injected into the juice (1). The variable adjustable injection port (17) can adjust the volume of sugar juice (1), the residence time of sugar juice in the gas injector (13), the concentration or amount of dissolved substances in sugar juice (1), or the concentration or amount of sugar juice (1) ) in response to the concentration of dissolved substances.

For other embodiments of the present invention, the gas mixture (3) can be injected into the juice (1) before the pump (14), so that the pump (14) can play a role in distributing the gas mixture (3) to the juice ( 1) in the flow to create a mixed flow (19) and increase the interfacial surface area (4). Depending on the type of pump, the mixed stream (19) can contain at least 35% gas mixture, wherein the juice stream (1) is almost 100% filled with gas bubbles of the gas mixture (3). As just one example, a Shanley pump can be used to generate the mixed flow (19). The Shanley pump is incorporated herein by reference. Multiple pumps (14) can be operated in series or in parallel as required to process a volume of juice (1) for a predetermined duration.

For other embodiments of the invention, the juice (1) flow may be further configured to provide a Venturi effect, or otherwise create a reduced pressure in response to the juice flow (1), to draw the gaseous mixture (3) In juice flow (1), the suction mode can be pulsating, continuous or intermittent.

For certain embodiments of the invention, only a portion of the juice stream (1 ) is exposed to the gas mixture (3). For example, if the juice (1) contains small amounts of dissolved matter (5), then the juice (1) flow can be split, exposing only part of the juice (1) to the gaseous mixture (3). The juice (1) streams are then recombined in the desired ratio.

Referring now mainly to Figure 3, for further embodiments of the invention, the juice (1) may be sprayed through a juice distribution element (21) such as a nozzle. The juice distribution element (21) can produce a very fine spray of juice droplets (22) or particles. Thus, spraying increases the interfacial surface area (4). The juice can be sprayed in a vented container (23) and the gas mixture (3), whether filtered or washed as described above, can be exposed to the droplets of the sprayed juice. The sugar juice can be sprayed onto the top area of the aeration container (23) (eg via spray nozzles) and then exposed to the gas mixture (3) passing through the aeration container (23). The gas mixture can pass through the ventilation vessel (23) counter-currently to the direction of the juice drops (22) to increase the efficiency of the transfer of dissolved substances (5) in the juice (1) to the gas mixture (3). The aeration vessel (23) can be, for example, a 150 gallon tank, but it is conceivable that the size and shape of the tank will vary depending on the amount of juice being processed.

In some embodiments of the present invention, the ventilated container (23) may further comprise a juice distribution surface (24). Juice (1) can be distributed onto the juice distribution surface (24) to further increase the interfacial surface area (4). Additionally, the juice can be sprayed onto the top area of the aeration container (23), distributed over the juice distribution surface (24), and then exposed to the gas mixture (3) passing through the aeration container (23). Furthermore, the gas mixture (3) can flow through the ventilated container (23) counter to the general direction of flow of the juice (1) on the juice distribution surface (24), so that the dissolved substances (5) in the juice (1) ) into the gas mixture (3) with increased efficiency.

For these embodiments of the invention using the aeration vessel (23), the juice (1) can be collected and circulated through the aeration vessel (23) as many times as desired.

Referring now primarily to FIG. 4 , in other embodiments of the present invention, juice ( 1 ) may be delivered to a juice container ( 25 ) and sprayed into juice ( 1 ) by spraying juice ( 26 ). ) into the gas mixture (3). The pressure and volume of the gas mixture (3) can be adjusted relative to the volume of the juice (1) and the size of the juice container (25). The juice container can be further combined with the above-mentioned ventilation container (23).

The general discussion of gas absorption provided in Chemical Engineer's Handbook, Perry, ed., McGraw-Hill Book Company (1950) pp. 668 et seq. is incorporated herein as A reference to the extent necessary to understand the general principles of gas absorption.

It will be appreciated that various conventional conduits, valves or other devices (e.g. pressure gauges) may be provided to generate and deliver juice (1) to the gas injector (13), aeration vessel (23) or juice vessel (25). process, the quantity and pressure of the gas mixture (3) injected, sprayed or sprayed, the quantity of dissolved substances (5) in the juice (1), etc.

Referring again primarily to Figure 2, the present invention may further comprise a gas separator (27) to release a gas mixture (3) containing dissolved matter imported from the juice (1). In certain embodiments of the invention, when a vented container (23) is used as described above, the gas separator (27) may include openings in the vented container to allow the gas mixture to vent through the vented container to the atmosphere. In those embodiments of the invention in which the gas injector (13) includes a nebulizer, the gas separator (27) may be an orifice enabling the discharge of the gas mixture (3) containing dissolved substances to the atmosphere. In those embodiments of the invention where the gas mixture (3) is added to the stream of juice (1) by a gas injector (13) to produce a mixed stream of juice (19), whether the process is continuous, pulsed or intermittent Transmitted in a conduit sealed off from the atmosphere, the gas separator (27) may comprise a portion of the conduit further providing an internal volume fluidically connected to the atmosphere. In particular, the gas separator (27), which is fluidically connected to the atmosphere, may comprise a portion of a conduit configured or defined for regulating the response time of the mixed stream (19) to the atmosphere.

Specifically, one configuration of the gas separator (27) may be an increase in the volume inside the conduit to spread the mixed flow (19) over the inner surface of the conduit to prolong the retention time of the juice fluidically connected to the atmosphere , and/or increase the surface area of the juice when fluidically connected to the atmosphere. In some embodiments of the gas separator (27), the juice may be distributed over a surface area large enough to allow the gas mixture (3) in the juice (1) to pass through the gas separator (27) Just reach equilibrium with atmospheric partial pressure substantially before transfer, the inner surface of gas separator (27) can be further configured to be provided with add-on parts, corrugated groove (corrugates), groove or similar structure to further in gas separator (27) ) to mix or agitate the juice (1) to increase the rate at which the gaseous mixture (3) is transferred from the juice (1) to the atmosphere.

A flow of the gas mixture (28) transferred from the juice (1) to the atmosphere can be generated by connecting a reduced pressure source (29) to the gas separator (27). The depressurization involves the development of a partial pressure of gas on the increased surface area (4) of the juice (1) below the partial pressure of the dissolved matter transferred into the gas mixture (3). It will be appreciated that the source of reduced pressure (29) may be the atmosphere when the partial pressure of the gas mixture containing the dissolved matter (5) removed from the juice exceeds atmospheric pressure. For some embodiments of the invention, as described above, the source of reduced pressure (29) may be created by increasing the internal volume of the conduit in which the mixed stream (19) flows. The source of reduced pressure (29) may also be generated by a vacuum pump, venturi, or other device fluidically connected to the gas separator (27). The partial pressure of gas generated over the increased surface area of the juice (4) can then be adjusted as desired (e.g. subatmospheric pressure) to increase the flow of gas mixture (3) containing dissolved matter (5) from the mixed juice stream (19 ) transfer rate.

For some specific embodiments, the gas separator can further include a safety valve (30) or further include a signal generator (31), which is connected to a decompression source (29), and can be used to control the gas accumulation in the gas separator (27) or Response to partial pressure of gas, or to a decrease in dissolved matter (total dissolved matter, some dissolved matter, dissolved matter concentration, or some dissolved matter concentration) in the juice, decreased juice acidity, decreased juice alkalinity, sugar A rise in juice pH or other measure that indicates that sufficient lysate has been removed from the juice (1) responds.

The invention further comprises storage or transport of the gas mixture (32) containing dissolved substances removed from the juice, such storage or transportation avoiding the discharge of all or part of the gas mixture to the atmosphere. In certain embodiments of the invention, a gas mixture containing dissolved matter removed from the juice (for example containing carbon dioxide) may be used, for example, in the carbonation step described above.

The present invention may also include adding an antifoaming agent (33) to the juice (1). Sugar juice contains a lot of substances that are surface active or can change the surface tension of water. Thus, entrainment of air in the juice or dissolved gases transferred from the juice to the atmosphere creates foam. There are many antifoam agents that can be used to reduce the amount of foam. Including, but not limited to, fatty acids, oils or similar substances. In order to achieve the infusion of the gas mixture (3) in the juice (1) as described above or to transfer the gas mixture (3) containing at least some dissolved substances (5), it may further be necessary to expose the juice to the desired gas mixture ( 3) A step of adding an antifoam agent at or near the same time as injecting the gas mixture into the sugar juice.

Once a predetermined amount of dissolved matter, volatiles, dissolved gases, water-soluble acids or similar has been transferred from the juice (1), the resulting juice product can be sent to an existing sugar plant for further clarification or purification. Alternatively, various embodiments of the present invention may be incorporated into a sugar plant to produce reduced dissolved matter juice in situ.

Referring now to Figure 5, for a sugar system that uses a base such as calcium oxide or calcium hydroxide to raise the pH to initially reach the isoelectric point of the various substances dissolved in the juice (1), or as a prelimed sugar part of the traditional method of juice (33), which can be separated or combined with other steps such as cold liming (34), main liming (35) or intermediate liming (36), which in turn can Separate or combined with a first carbonation step (37) or a second carbonation step (38) that produces a calcium carbonate (39) precipitate to capture at least a portion of the non-sucrose material in the juice (1), so that The obtained clarified or purified juice is filtered (44) before the amount of water (45). The method and apparatus of the present invention can be used to manufacture sugar juice products with reduced dissolved matter content or reduced dissolved gas content. These methods and apparatus can Incorporated into one or more or all of these traditional steps, or modified to some extent to benefit from the characteristics of the juice treated in accordance with the present invention.

It will be appreciated that the present invention can be used to reduce dissolved matter prior to the addition of any base. Since the present invention can fully increase the pH value of the sugar juice or reduce the acidity of the sugar juice, the amount of alkali used in the traditional preliming or main ashing step can be reduced. Alternatively, in those processing systems where the underflow of the process system (eg spent lime) is greater than a portion of the acid in the juice for neutralization or to reduce foaming, the underflow may be added either before or after employing the present invention.

Specifically, the method for purifying sugar juice using the present invention may include obtaining sugar juice (1) from plant matter (2), wherein the sugar juice contains sucrose, non-sucrose substances and water as described above. The invention is applied in the various embodiments shown or described to increase the pH of the juice or to reduce the acidity of the juice prior to preliming (33). The process of cold main liming (34) and/or hot main liming (35) of juice (1) can be carried out in combination with carbonation (37) (38). When calcium oxide or calcium hydroxide is used as base (46) in the preliming (33) or main liming (34) (35) steps, the carbonation step (37) which precipitates calcium carbonate (39) can trap sugars At least a portion of non-sucrose matter in the juice (1). These precipitates ( 39 ) can be removed by separating the juice ( 1 ) from the precipitate ( 39 ) to remove captured non-sucrose matter. In some embodiments of the invention, an intermediate liming (36) step may be performed with additional carbonation (38). Reprecipitation of calcium carbonate (39) removes trapped non-sucrose species. Removal of the calcium carbonate precipitate (39) results in a juice (1) capable of producing the desired syrup (46) after removal of the water content (45) to the desired amount. Alternatively, crystallization (47) of the sucrose contained in the juice can produce a sugar product (48).

Referring now primarily to Figure 6, it is known from U.S. Pat. Nos. 3,785,863, 4,331,483 or 4,140,541 (hereby incorporated by reference) regarding a sugar system employing ion exchange (49) in place of the traditional calcium carbonate purification step in the sugar system described above, The juice can be pre-treated with a base such as lime to make it easier to filter before the ion exchange step (49), thereby regenerating the ion exchange material to produce the calcium form, which removes the polar load in the juice ( polar load) for calcium, or to reduce the acidity of the juice after the ion exchange process.

In these types of processes, the invention can be used to reduce the amount of dissolved matter or dissolved gases prior to or in conjunction with juice pretreatment, or to make the juice less acidic, or to make the juice less acidic prior to ion exchange. Decrease in the polar loading of the juice, or reduce the acidity of the juice after the ion exchange step. The above objects can be achieved by processing sugar juice according to the present invention.

Referring now primarily to Figure 7, it is known from U.S. Patent No. 4,432,806 (incorporated herein by reference) regarding a sugar system employing filtration or ultrafiltration instead of the traditional calcium carbonate purification step in the sugar system described above, using, for example, lime Alkalines such as Alkali pretreat the juice to make it easier to filter (50).

In these types of processes, the invention can be used to reduce the amount of dissolved matter or dissolved gases prior to or simultaneously with pretreatment of the juice with alkali to bring the non-sucrose species to their isoelectric point and aggregate, or to reduce the The acidity is reduced, or otherwise produces solid particles that can be filtered from the remaining liquid portion of the juice. The above objects can be achieved by processing sugar juice according to the present invention.

Referring now primarily to FIG. 8, the present invention may include apparatus or methods for processing sucrose-containing liquids or leach juices that take advantage of the lower solubility of pH-lowering substances in these liquids. When a sucrose-containing liquid is heated, the solubility of certain substances, including gases like _CO2 and _SO2 , decreases. Therefore, even when these species cannot be transferred at lower liquid temperatures or cannot be further transferred into this partial pressure gas, it is possible to initiate or promote these species at the interface between the mixture of these liquids and the partial pressure gas. discharge of these liquids.

Referring now primarily to Figure 9, which shows an embodiment of the invention in which sugar beet silk (51) is added to a mixer (52), usually with a conveyor belt or other conveying device, or may be directly fed using a pump (54). Add sugar beet silk (51) to beet silk extractor (53). In an embodiment of the invention where the sugar beet cossette (51) is added to the mixer (52), the sugar beet cossette (51) can be mixed before being pumped to the cossette extractor (53). The extractor (52) is in contact with some or all of the leach juice or effluent (55) from the cossette extractor (53).

In the extractor (53), the sugar beet silk is treated with hot water (59) (usually between 50°C and 80°C), sometimes in convection, so that the sugar beet juice (which may contain the above other soluble and insoluble substances and substances) are removed or transferred from the sugar beet shreds (51) to hot water (59). The hot water (59) containing the sugar beet juice (sometimes called "leach juice") leached from the sugar beet shreds (51) is now collected and passed through the pump (60) in a single or multiple effluent stream. Streams (55) (58) are sent to mixer (52).

Importantly, although extractor technology has been used for decades, it was not known prior to the present invention that the extractor (53) itself could prevent or reduce the The leaching of substances or materials in juice or extractor liquids to remove certain substances or to lower the pH of substances. Embodiments of the present invention take advantage of the elevated temperatures used in the sugar beet cosserge extraction process, which deactivates some of the Reduction of the solubility of substances to remove, reduce, or transfer certain substances or materials, such as alcohols, aldehydes, ketones, esters, nitriles, thioethers, pyrazines, carbon dioxide, carbonic acid, sulfur dioxide, phosphoric acid, hydrochloric acid, sulfuric acid, sulfurous acid, citric acid , oxalic acid, succinic acid, fumaric acid, lactic acid, glycolic acid, pyrrolidone-carboxylic acid, formic acid, acetic acid, butyric acid, maleic acid, propionic acid, 3-methylbutyric acid, butanoic acid ), valeric acid, 5-methylhexanoic acid, hexanoic acid, heptanoic acid or lactic acid.

The higher temperature of the leach liquor or leach juice (lower solubility of the pH lowering species) is utilized in configurations of the invention such as those illustrated in Figures 1 to 7 and 11, 12, 13 and herein , sugar beet waste silk liquor or other leaching liquid monitoring, evaluation and control, can be carried out in the extractor (53) itself or at various positions (200) (201) (202) shown in Fig. 9, so that in the leaching Between the extractor (53) and the preliming device (57), the squeeze liquid of beet waste shreds is processed or the leached sugar juice is processed. Heaters (T) (203) (204) may be added in series to bring the juice or leach juice to or maintain a juice temperature between about 60°C and about 80°C. Various embodiments of the present invention with a heater can cause the juice to reach or maintain a temperature of about 60°C, about 61°C, about 62°C, about 63°C, about 64°C, about 65°C, about 66°C, about 67°C, about 68°C, about 69°C, about 70°C, about 71°C, about 72°C, about 73°C, about 74°C, about 75°C, about 76°C, about 77°C, about 78°C, about 79°C , about 80°C, or other desired temperature.

Thus, there are many embodiments of the invention showing various configurations using extractors and sugar beet cossette extraction techniques, some of which are shown in Figure 9 (showing exemplary positions ( 200) (201) (202), on these positions, place the various configurations of the present invention shown in Figures 10 to 13 or hereinafter described), these configurations provide enough to carry out and use the various configurations of the present invention Figure example of an implementation. These illustrations are not considered to limit various other specific implementations that are not shown.

Certain embodiments of the present invention include controlled exchange rates of atmospheric partial pressure, or maintaining a partial pressure of gas in the extractor that allows the extraction of water from the heated leach juice (205) within the extractor (53). ) in additional shifted-out or pH-lowering substances. In some embodiments of the invention, the extractor (53) can be modified to additionally be fluidly connected to the atmosphere so that the exchange of atmospheric partial pressure on the heated leach juice surface can be enhanced. In some other embodiments of the present invention, when it is not possible to modify the configuration of the extractor to enhance the exchange of atmospheric pressure in the extractor (53), a gas flow generator (64) can be installed. The increased ventilation (63) can be balanced with the air flow created in the extractor (53). An evaluation element (65) monitoring the transfer of certain substances from the extractor liquid into the gas stream can provide information on the extractor liquid or atmospheric partial pressure (or other selected gas mixture or partial pressure) at the leach juice interface. information on the rate of material exchange between gases).

Referring now primarily to FIG. 10, other embodiments of the present invention include transferring the heated leach juice (66) to a container (67) using a pump (60) or other delivery means, thus increasing the heat leach juice (66) ) to reduce the concentration of pH lowering species to a greater extent (or to achieve a predetermined amount of pH lowering species such as _CO2 or _SO2 ) or to allow more rapid transfer of pH lowering species from heated leach juice. The increased surface area (or variably adjustable desired surface area) of heated leach juice (66) can be obtained in various ways as described above by injecting the desired partial pressure of gas (to strip the leach juice), Sprayed into containers or transported onto increased area substrates.

Certain embodiments of the invention include a container (67) with a substantially open top, and may further provide a substantially open bottom (which for convenience may reduce the size of the opening to deliver the treated leach juice to the mixing chamber). device, settling tank (68) or pump (56) (54) or other conveying equipment. The heated juice (66) from the extractor can be added near the top of the container (67) so that the heated juice (66) Relative to the atmospheric partial pressure in the container, there is a surface area that increases to a considerable extent.As shown in Figure 10, a specific embodiment of the present invention adds heating sugar juice near container (67), makes heating sugar juice distribute on the inner wall and have sufficient force to spiral down at least part of the height of the inner surface to increase residence time in the container (67).

For some embodiments of the present invention, when the container (67) is only used to hold and collect the treated leached juice, the way to add heated juice to the container (67) can be to increase the heated juice (66) surface area method. In these embodiments of the invention, the configuration of the liquid flow of the heated juice may be modified by agitation, pulsation, splitting into multiple streams, spraying, formation of droplets, or otherwise in order to generate additional flow through fluidics and the atmosphere or the resulting flow. The surface area required to connect the partial pressure gases.

Other embodiments of the present invention can utilize the structure of the container (67) to take full advantage of the increased surface area of the heated leached juice (66). For example, the container may have a circular or conical configuration or even a variable adjustment configuration that controllably increases or decreases the surface area of heated juice added to the surface of the container (67) and the residence time on the surface of the container. For some embodiments of the present invention, the vessel can be fluidically connected to atmospheric partial pressure or a desired partial pressure of gas (the partial pressure of gas can be injected into the conduit to neutralize the pH-lowering substances in the heated leach juice or not). The required strippable components are stripped) the diameter of the conduit (69) connected to the delivery of sugar juice is increased.

In certain embodiments of the invention, the partial pressure of gas in contact with the surface area of the heated juice can be controlled by evacuation or predetermined exchange of a selected gas mixture to maintain a continuously decreasing desired partial pressure of gas concentration to increase A specified gas or substance removed from heated leach juice, including stripping as described above.

Referring now primarily to FIG. 11 , another embodiment of the present invention may include a pump (70) and other liquid delivery elements to achieve sufficient process liquid pressure (at about 20 per square inch) at the injection port of the gas injector (71). pounds to about 25 pounds per square inch). As noted above, the process liquid may be heated to between about 50°C and about 80°C to volatilize gases such as CO ₂ , SO ₂ , volatile organic compounds in the process liquid, or Reduced solubility of inorganic compounds. After injecting air or other partial pressure gases into the process liquid at the injection port (71) as required, the process liquid can be transferred to the gas-liquid separator (72), which is used in some embodiments of the present invention. In the way is a centrifugal gas-liquid separator that can reach about 4 times the gravity. A gas-liquid separator (72) allows partial pressure gas injected into the process liquid to transfer dissolved gases, volatile organic compounds or volatile inorganic compounds to the atmosphere to reduce the concentration of these substances in the process liquid. In some embodiments of the invention, the gas-liquid separator may be a vessel that holds the process liquid in a manner that increases the atmosphere-process liquid interface, which allows material to be transferred from the process liquid in a shorter period of time to the atmosphere. When using a centrifugal gas-liquid separator, the centrifugal force applied to the process liquid can cause the process liquid to spread over the interior surface of the cylindrical vessel (although other configurations can also be used), and in some cylindrical embodiments of the invention The central centrifugal force is about 4 times the gravity. The process liquid is spread over the inner surface of the cylindrical container of the centrifugal gas-liquid separator, which can be achieved by maintaining a gas column in the center of the cylinder (the gas in the process liquid can be transferred to this gas column) ) mode increases the area of the atmosphere (or other partial pressure gas)-production liquid interface. A gas removal system (73) allows the transfer of partial pressure gas from the process liquid to the atmosphere. In some embodiments of the invention, the process liquid from the gas-process liquid separator (72) may enter the preliming step of a conventional sugar system or enter other processing steps as described above.

For other embodiments of the invention, a pump (74) or other process liquid delivery element delivers process liquid to a liquid dispersing element (76), such as a nozzle, so that the atmosphere (or other partial pressure gas ) - distributes the process liquid in such a way that the surface area of the process liquid increases. In some embodiments, the liquid dispersion element (76) can produce droplets or a spray. A gas distribution manifold (77) or other gas distribution element moves air or other partial pressure gas through the dispersion of the process liquid to further dissipate the gas from dissolved gases, volatile organic compounds or volatile acids or the like in the process liquid and partial pressure gas added through the gas distribution manifold. In some cases, this partial pressure gas flow added through the gas distribution manifold (77) can be countercurrent to the dispersed process liquid from the direction of the liquid dispersion element (76), thereby enabling gas partitioning or stripping. The process is more efficient. A foam dispersing element (78) may further be added to break up the foam generated by the liquid during gas distribution or stripping. A mesh or sieve with a suitable sized opening can be used. The liquid dispersing element (76), gas distribution manifold (77) and foam dispersing element (78) may be located within a container (79) or a gas distribution column. The gas delivery element (80) can be used to determine the gas flow into the gas distribution manifold (77). The gas flow can be adjusted based on a separate or combined analysis of the conditions in the vessel (79) or the chemical conditions in the process liquid. In some embodiments of the invention, process liquids may enter the preliming step of a conventional sugar system, or enter other processing steps as described above.

Certain embodiments of the invention may further include a vacuum chamber (84) into which process liquid may be introduced. The pressure in the vacuum chamber (84) can be adjusted or adjusted to remove a desired amount of volatile species (or to achieve a desired pH) from the volume of process liquid passing through the vacuum chamber (84). The vacuum in the vacuum chamber can be created by a vacuum pump or in some embodiments of the invention by the movement of liquid through the discharge tube system (88)(89)(90). The amount of process liquid entering the vacuum chamber (84) can also be adjusted by the liquid control valve (81) and can be dispersed through the second liquid dispersing element (82) to increase the process liquid-gas interface area. The process liquid is then transferred from the vacuum chamber (84) to the preliming step of a conventional sugar system, or to other processing steps as described above.

The invention further comprises an exhaust system (91) consisting of various components (72) (79) (84) (90) for transferring spilled process liquid or process liquid foam to an exhaust collection container (93 ), antifoam can be added to the vessel through the antifoam dispersing element (92). The process liquid collected in the vent collection vessel (93) is then transferred from the vacuum chamber (84) to the preliming step of a conventional sugar system, or to other processing steps as described above.

Referring now primarily to Figures 12 and 13, an embodiment of the present invention may include a juice treatment system provided with a juice distribution element (300), a non-limiting example of which may be a BEX PSQ full square spray nozzle or a BEX PSWSQ wide angle full square spray nozzle (300). See Example ___________. Juice (301), whether heated as described above or not, can be dispersed into a gas (302) or gas mixture or fraction having gas properties capable of transferring at least one substance from said juice into said gas. gas under pressure (such as atmospheric gas or atmospheric gas supplemented or stripped to the desired partial pressure). A variable adjustable flow generator (303) maintains the gas flow (302) at a level sufficient to maintain the gas characteristics (partial pressure gas, gas volume , gas residence time, gas velocity, etc.) A gas discharge element (304) enables gas containing material diverted from the juice to vent to the atmosphere or be carried to a desired location or into a desired process or into a desired process step. Gas flow (302) may be formed through a single gas discharge location or multiple gas discharge locations (305). In some embodiments of the invention, the gas first enters a gas distribution element (310), such as a gas distribution ring (with many openings (313) in the ring) as shown in Figure 13 . The gas distribution elements are used to create the desired convection or other form of gas flow characteristics in the container (312).

For example, juice (301 ), leach juice, beet spent juice, extractor liquid, or juice production liquid dispersed at about 60 to about 100 cubic feet per minute (about 500 to 133 gallons per minute) Dispersion into the gas stream generated at a rate of about 450 to 850 cubic feet per minute, which allows certain substances to be transferred from the juice to the gas stream, such as alcohols, aldehydes, ketones, esters, nitriles, thioethers, pyridines Azine, carbon dioxide, carbonic acid, sulfur dioxide, phosphoric acid, hydrochloric acid, sulfuric acid, sulfurous acid, citric acid, oxalic acid, succinic acid, fumaric acid, lactic acid, glycolic acid, pyrrolidone-carboxylic acid, formic acid, acetic acid, butyric acid (butyric acid) , maleic acid, propionic acid, 3-methylbutanoic acid, butanoic acid, pentanoic acid, 5-methylhexanoic acid, hexanoic acid, heptanoic acid and lactic acid, etc. For embodiments of the invention configured such as those shown in Figures 12 and 13, an airflow (302) (in cubic feet) four times the amount of dispersed sugar juice (301) is used to reduce leached sugar from sugar beets The amount of various substances in the juice. See Examples 1 to 3. Similarly, juice obtained from crushing sugarcane can be similarly treated with similar results. Depending on the amount of juice dispersed and airflow generated, the configuration is sized accordingly, and multiple assemblies comprising the present invention can be used in series or in parallel to typical sugar beet processing equipment (typically 1000 to 5000 gallons per minute leached sugar Juice) produced sugar juice is processed.

Certain embodiments of the invention further include a supplemental gas flow generator (306) to generate a supplemental gas flow (307), which may contain oxygen, ozone, air stripped of certain partial pressure gases, capable of An oxidizing agent for the conversion of primary alcohols to the corresponding aldehyde or carboxylic acid. Alternatively, embodiments of the invention further include a supplemental oxidizing agent (308) capable of being dispersed into the dispersed juice through nozzles (311).

As mentioned above, when said juice (301) is dispersed into said gas (302) having gas properties such that at least one substance is transferred from said juice into said gas, heater (309) may The juice is brought to or maintained at a substantially constant temperature selected from the range of 60°C to 80°C. For various embodiments of the invention, when said juice (301) is dispersed into said gas (302) having gas properties such that at least one substance is transferred from said juice into said gas, the juice having a temperature selected from about 60°C, about 61°C, about 62°C, about 63°C, about 64°C, about 65°C, about 66°C, about 67°C, about 68°C, about 69°C, about 70°C, about 71°C , about 72°C, about 73°C, about 74°C, about 75°C, about 76°C, about 77°C, about 78°C, about 79°C, and about 80°C.

Some embodiments of the invention may further include a baffle (311) to separate the dispersed juice (301) from the gas (302) having gas properties that transfer at least one substance from the juice to the gas. The interface area between them increases.

Juice treatment as described above may be carried out in a first vessel (312) as shown in Figure 13, after which the treated juice is transferred from an outlet (314) to a prelimer (57) or other processing step, or it can be transferred to a second container (315). In those embodiments where the processed juice is transferred to a second container, the juice (301 ) may be redispersed by at least one second dispersing element (316). A reduced pressure generator (317) can reduce the pressure in the second container (316) to reduce the gas partial pressure of at least one substance diverted from the juice to a lower gas partial pressure (318 ).

The reduced pressure generator achieves and maintains a lower pressure in the second vessel (315) sufficient to boil the dispersed juice (102). The lower pressure (318) in the second container (315) can be changed or adjusted (automatically or manually) according to the temperature and composition of the dispersed juice (301). A desorption gas flow generator (319) may add a desorption gas flow (320) to the second vessel (315) to transfer volatilized species to the atmosphere. Stripping gas (320) includes air, atmospheric gases, nitrogen, oxygen, other specified gases.

Certain embodiments of the present invention further include an auxiliary gas reduction generation (321) to assist the gas reduction generation (317) in boiling the dispersed juice (301) in the second vessel (315) Or keep it boiling.

Similar to the first vessel (312), a baffle (311) may also be included in the second vessel (315) to increase the interface area between the juice (301) and the reduced partial pressure gas (318).

Certain embodiments of the invention also include a third vessel (322) in which a reduced pressure can be established or maintained as described above. Juice (301) may be transferred from the second container (315) through outlet (323) and dispersed into a third container by similar juice distribution elements as in the first and second containers. Alternatively, the juice (301 ) exiting the second vessel (315) may be transferred directly to a preliming step or filtration step or other steps or processes as desired.

These examples of specific embodiments of the invention serve specifically to illustrate the general concept of taking advantage of the reduced solubility of certain substances, gases, volatile compounds, acids or similar substances by heated sugar juice, by Controlling the partial pressure of gas present at the surface of the heated leach juice and/or increasing the surface area of the heated juice in contact with the desired partial pressure of gas positively monitors, evaluates or controls the concentration of these substances. An advantage of the present invention is believed to be that the addition of a small amount of alkali such as lime can control the foaming phenomenon during the processing of the juice prior to the preliming step.

Example 1

Sugar juice is obtained by traditional tower extraction of sugar beet silk. Control and experimental groups were formed, each consisting of six substantially identical 500 ml aliquots of the extract juice. Aliquots from the control and experimental groups were analyzed to determine their pH. For each aliquot of extracted juice in the control group, the pH was about 6.3. Aliquots in the control group were titrated without further treatment with 50% wt./vol. caustic soda solution to an endpoint of 11.2 pH. Aliquots from the experimental group were treated according to the invention, the pH of each aliquot was subsequently determined, and each experimental aliquot was treated with a 50% wt./vol. caustic soda solution to Titrate to a 11.2 pH endpoint in almost the same manner as the control.

The results are listed in Table 1 below. As can be seen from the table, the pH of the juice aliquots prior to any treatment was approximately 6.3. Compared with the control group, the pH value of the experimental group treated according to the present invention increases without adding any alkali, and requires a small amount of caustic soda to reach the end point of pH 11.2.

Table 1

pH value of untreated juice Caustic ML pH of treated juice Caustic mL % reduction in caustic 6.3 1.8 6.5 1.5 16.6 6.3 1.8 6.6 1.4 22.2 6.3 1.8 6.6 1.4 22.2 6.3 1.9 6.6 1.6 15.8 6.3 1.9 6.5 1.5 21.0 6.3 1.9 6.5 1.6 15.8

The amount of caustic required to reach the 11.2 pH endpoint was reduced by about 15.8% to About 22.2%.

Example 2

Sugar juice is obtained by traditional tower extraction of sugar beet silk. Control and experimental groups were formed, each consisting of 5 substantially identical 500 ml aliquots of the leachate. Aliquots from the control and experimental groups were analyzed to determine pH. For each aliquot of extracted juice in the control group, the pH was about 6.1. Aliquots in the control group were titrated without further treatment to a 11.2 pH endpoint with 30 brix of milk of lime solution. Aliquots from the experimental group were treated according to the invention, the pH of each aliquot was subsequently determined, and each experimental aliquot was treated with a 30 Brix milk of lime solution to compare with the control group. Titrate to a pH endpoint of 11.2 in much the same manner.

The results are listed in Table 2 below. As can be seen from the table, the pH of the juice aliquots prior to any treatment was approximately 6.1. Compared with the control group, the experimental group treated according to the present invention has a higher pH value without adding any alkali, and requires less milk of lime to reach the end point of pH 11.2.

Table 2

pH of untreated juice milk of lime ml pH of treated juice milk of lime ml % reduction of milk of lime 6.1 4.6 6.5 3.3 28.3 6.1 4.4 6.6 3.2 27.3 6.1 4.7 6.6 3.5 25.5 6.1 4.4 6.6 3.3 25.0 6.1 4.5 6.6 3.3 26.7

Compared to the juice aliquots in the untreated control group, the amount of milk of lime required to reach the 11.2 pH endpoint was reduced by approximately 25.0% to About 28.3%.

Likewise, the data presented in Tables 1 and 2 provide a comparison of two different types of extraction equipment and extraction methods. Importantly, the data show that different extractors or different extraction methods can produce extracted juices with significantly different pH values, even though the pH values produced by each type of extraction technique can be essentially internally consistent . For example, the initial pH value of the untreated leach juice in Table 2 was 6.1 compared to the initial pH value of the untreated leach juice in Table 1 which was 6.3.

Example 3

Extract juice is obtained by conventional tower leaching of sugar beets and according to the invention using the embodiment shown in Figures 12 and 13 with a location between the mixer and the prelimer deal with. The leach juice dispersed at a rate of approximately 100 cubic feet per minute into an atmospheric air stream generated at a rate of approximately 400 cubic feet per minute (72 inches by 72 inches of convection channels, wherein the convection channels are approximately 144 inches high) is shown in the table below As indicated by the GC/MS analysis shown in 1 and 2, a variety of substances were transferred from the dispersed sugar juice:

Table 1

Table 1 shows the gas chromatographic analysis of samples SMBSC1 and SMBSC2 (concentrates obtained from the gas stream after counter-current exchange with the sugar juice described herein), and the comparison of the chromatograms of those samples with the standards for the organic acids listed in 1-9 above. Gas chromatographic analysis of mixture samples for comparison. It can be seen that the treatment of the sugar juice according to the present invention removes various organic acids contained in different amounts of the standard mixture.

表2

Table 2

Table 2 presents the gas chromatography/mass spectrum of sample SMSBC5 D (concentrate produced from gas flow after counter-current exchange with the juice described herein without the use of reduced pressure and at a juice temperature between 60°C and 70°C) Analysis, chromatographic analysis of this sample showed various volatile compounds rising above a baseline with a curvature dominated by various alcohols.

Each of these compounds was identified by GCMS and its Kekule structures are in Table 3 below; listed:

table 3

Although different types of extraction equipment and different extraction methods exist, those of ordinary skill in the art do not realize that the pH can be changed or lowered during the extraction of sugar beet or other types of plant matter, or that There is no recognition that different extraction equipment or different methods produce juices or liquids with different pH values, or that newer types of extractors can often obtain extracted juices with lower pH values. Using the same extraction technique or a different extraction technique, the extraction technique produces an extract juice with a different pH, or an improvement in the extraction technique has changed or lowered the pH of the extract juice, in this regard, may It can be seen that these traditional methods of extracting sugar juice from plants are far from the teachings of the present invention.

From the foregoing it is readily apparent that the basic concept of the invention can be embodied in various ways. It includes analytical techniques and the equipment used to perform appropriate analyses. In this use, analytical techniques are disclosed as part of the results obtained by the various devices described, or as inherent in their use. It is simply a natural consequence of using the device intended or described. Furthermore, although some devices are disclosed, it should be understood that these devices not only implement certain methods, but can also be varied in many ways. Importantly, as with all the foregoing, all of these aspects should be considered included in their disclosure.

The discussion contained in this application serves as a basic illustration. The reader should be aware that the detailed discussion cannot explicitly describe all possible implementations; many alternatives are implied. Nor does it fully explain the general nature of the invention, nor does it expressly show how each feature or element actually represents more functionality or alternatives or equivalent elements. Again, these are implied in this disclosure. When describing the invention in device specific terminology, each component of the device implicitly serves a function. Not only are device claims to the device described, but method or process claims specifying the invention and the functioning of each element. Neither the description nor the terminology is intended to limit the scope of the claims contained herein.

It should also be understood that various changes may be made without departing from the essence of the invention. These changes may also be implicit in the description. It still falls within the scope of the present invention. This disclosure contains a broad disclosure including the explicit embodiments shown, various implicit alternative embodiments and principal methods or processes, etc., and may be relied upon for support of the claims of this application. It should be understood that any such change of language and broad claims are accomplished here. This complete patent application serves to support patents covering various aspects of the invention either individually or as a system as a whole.

Furthermore, various elements of the invention and claims may also be implemented in different ways. The present disclosure should be understood to cover every such variation as it is an implementation variation of any apparatus embodiment, method or process embodiment or merely a variation of any element of these. In particular, it should be understood that when the present disclosure refers to elements of the invention, the wording of each element may represent equivalent apparatus terms or method terms—even if only the function or result is the same. These equivalent, broad, or even more general terms should be considered to be included in the description of various elements or actions. These terms may be substituted as necessary to clarify the general scope of rights granted to the invention. By way of example only, it should be understood that all actions may be expressed as a device which causes that action or as an element which causes that action. Similarly, each physical element disclosed should be understood to include a disclosure of what that physical element contributes to. With this last aspect in mind, as just one example, disclosure of a "syringe" should be understood to include disclosure of the effect of "injecting"—whether explicitly stated or not—and conversely, effective disclosure of the effect of "injecting" should be understood to include Disclosure of "syringes" or even "device for injecting". Such changes and alternative terms are deemed to be expressly included in this specification.

Any patents, publications, or other references mentioned in this patent application are hereby incorporated by reference. In addition, as for the various terms used, it should be understood that unless its use in this application is inconsistent with the translation, each term contains a general dictionary definition, and as in Random House Webster's Unabridged Dictionary (Random House Webster's Unabridged Dictionary) All definitions, alternative terms and synonyms contained in Abridged Dictionary) Second Edition are hereby incorporated by reference. However, to the foregoing, such information or statements incorporated by reference may be inconsistent with the patent content of this invention, and in this regard, such statements are expressly not deemed to have been made by the applicant.

Accordingly, applicants claim at least the following: i) each of the juice processing systems disclosed and described herein, ii) the associated methods disclosed and described, iii) similar and equivalent claims to each of these devices and methods and even implied changes; iv) alternative designs for implementing the functions shown as disclosed and described; v) alternative designs and methods for implementing the functions disclosed and described as implied; vi) the various features, components and steps shown as separate and independent inventions; vii) uses enhanced by the various systems or components disclosed; viii) products derived from these systems or components; ix) essentially methods and apparatus as previously described and with reference to any of the accompanying embodiments; x) various combinations and permutations of the foregoing disclosed elements; xi) the above various methods performed by means of or on a computer; xii) as above A programmable device as discussed above; (xiii) a computer readable memory encoded with data directing a computer comprising a device or element having functions as discussed above; xiv) a computer configured in accordance with the disclosure and description herein; xv) individual or combined subroutines and programs as disclosed and described herein; xvi) related methods disclosed and described; xvii) similar, equivalent and even implied variations to the respective systems and methods; xviii) implementing Alternative designs for the disclosed and described functions; xix) Alternative designs and methods for implementing the disclosed and described functions as implied; xx) Each shown as a separate and independent invention xxi) various combinations and permutations of the above items; and xxii) various possible dependent claims or concepts attached to each listed independent claim or concept.

It should be understood that, for practical reasons and to avoid adding potentially hundreds of claims, the applicant lists only the claims with the earliest dependencies at the end. It should be understood that, under new matter laws (new matter laws) - including but not limited to European Patent Convention Article 123 (2) (European Patent Convention Article 124 item 2) and United States Patent Law (United States Patent Law) 35U.S.C §132 or other similar law—there is the level of support required to allow the incorporation of dependencies or other elements recited under one independent claim or concept to a dependency under any other independent claim or concept or other elements as well.

Furthermore, the use of the transitional phrase "comprises" preserves claims that "extend" according to traditional claim interpretation, if or when used. Therefore, unless the context requires otherwise, it should be understood that the term "comprise", or variations such as "comprises" or "comprising", implies the inclusion of stated elements or steps or groups of elements or group of steps but not to the exclusion of any other element or step or group of elements or steps. These terms should be construed in their broadest terms so as to give applicants the broadest coverage legally permitted.

The claims set forth in this specification are hereby incorporated by reference into part of this specification of the present invention, and the applicant expressly reserves the right to use all or part of the claims contained in these claims as supplementary statements in support of any one or all of the claims or The applicant further expressly reserves the right to remove any part or all of the content contained in these claims or any element or component thereof from the description to the claims (and vice versa) as required. the right to delineate the scope of protection claimed in this application or any of its whole continuation, sub-applications or part- continuation applications, or to obtain the benefit of a reduction in fees under the patent laws, rules or regulations of any country or treaty, and these The incorporated matter should exist throughout the pendency of this application (including any fully continuation, divisional or part-continuation application or any rearrangement or extension thereof).

Claims (68)

1. A method for purifying the sugar juice obtained by plant body, comprising the following steps: a) obtaining plant matter; b) removing juice from at least a portion of said plant matter, wherein said juice contains sucrose, non-sucrose matter and water, and wherein an amount of said non-sucrose matter includes dissolved matter; c) exposing said juice to a gas mixture while adding an antifoaming agent; d) transferring a portion of said lysates from said juice to said gas mixture prior to alkali addition; e) creating an increased interfacial surface area between said juice and said gas mixture; f) increasing the rate of transfer of said solutes from said juice to said gas mixture; g) regenerating said gas mixture, or adjusting the partial pressure of gas continuously or intermittently over an increased interfacial surface area with said juice to prevent equilibrium between said gas mixture and said dissolved matter; and h) Reducing said dissolved matter in said juice. 2. A method of purifying juice obtained from plant matter as claimed in claim 1, wherein said step of removing juice from at least a portion of said plant matter comprises leaching said plant matter to obtain said plant matter Said sugar juice. 3. A method of purifying juice obtained from plant matter as claimed in claim 1, wherein said step of removing juice from at least a portion of said plant matter comprises grinding said plant matter to obtain said plant matter Said sugar juice. 4. The method of purifying sugar juice obtained from plant matter as claimed in claim 1, wherein said plant matter is selected from the group consisting of sugar cane, sugar beet and sweet sorghum. 5. The method for purifying the sugar juice obtained from plants as claimed in claim 1, wherein said non-sucrose matter comprises at least one selected from the group consisting of insoluble plants, soluble plants, soil particles, fertilizers, except sucrose. sugars, organic non-sugars, inorganic non-sugars, dissolved gases, organic acids, inorganic acids, proteins, phosphates, carbonate ions, bicarbonate ions, metal ions, pectin, colorants, saponins, Waxy, fatty and gummous substances. 6. A method of purifying juice obtained from plant matter as claimed in claim 1, wherein at least a portion of said dissolved matter in said juice comprises volatile substances. 7. A method of purifying sugar juice obtained from plant matter as claimed in claim 1, wherein said dissolved matter in said sugar juice includes dissolved gas. 8. A method of purifying sugar juice obtained from plant matter as claimed in claim 7, wherein said dissolved gas in said sugar juice is selected from carbon dioxide and sulfur dioxide. 9. A method for purifying sugar juice obtained from plants as claimed in claim 7, wherein the dissolved gas in the sugar juice comprises a form selected from carbon dioxide gas, carbonate ions, bicarbonate ions and carbonic acid carbon dioxide present. 10. A method of purifying juice obtained from plant matter as claimed in claim 7, wherein the dissolved gas in said juice comprises sulfur dioxide in a form selected from sulfur dioxide gas, sulfuric acid and sulfurous acid. 11. A method of purifying sugar juice obtained from plant matter as claimed in claim 1, wherein the dissolved matter comprises water-soluble acids. 12. A method for purifying sugar juice obtained from plants as claimed in claim 11, wherein said water-soluble acid is selected from phosphoric acid, hydrochloric acid, sulfuric acid, citric acid, oxalic acid, succinic acid, fumaric acid, lactic acid, hydroxyl Acetic acid, pyrrolidone-carboxylic acid, formic acid, acetic acid, butyric acid, maleic acid and lactic acid. 13. A method of purifying juice obtained from plant matter as claimed in claim 1, wherein said gas mixture is selected from the group consisting of atmospheric gases, filtered atmospheric gases and filtered air. 14. A method of purifying juice obtained from plant material as recited in claim 1, wherein said step of increasing the interfacial surface area between said juice and said gaseous mixture comprises agitating said juice. 15. A method of purifying juice obtained from plant material as recited in claim 1, wherein said step of increasing the interfacial surface area between said juice and said gaseous mixture comprises spraying said juice. 16. A method of purifying juice obtained from plant matter as recited in claim 1, wherein said step of increasing the interfacial surface area between said juice and said gaseous mixture comprises blowing said gaseous mixture into the juice. 17. A method of purifying juice obtained from plant matter as recited in claim 1, wherein said step of increasing the interfacial surface area between said juice and said gaseous mixture comprises injecting said gaseous mixture into The sugar juice. 18. A method of purifying juice obtained from plant matter as recited in claim 1, wherein said step of increasing the interfacial surface area between said juice and said gaseous mixture comprises vaporizing said gaseous mixture Lift the sugar juice. 19. A method of purifying sugar juice obtained from plants as claimed in claim 1, wherein: a) contacting said juice with a gas mixture; b) transferring a portion of said lysate from said juice to said gas mixture prior to addition of base; c) increasing the interfacial surface area between said juice and said gas mixture; d) increasing the transfer rate of said solutes from said juice to said gas mixture; and e) Reduction of dissolved matter in the juice. The steps above include injecting said gaseous mixture into a juice stream to form a mixed stream of said juice and said gaseous mixture whereby at least a portion of said dissolved material is transferred from said juice stream into said injected gaseous mixture . 20. A method of purifying juice obtained from plant material as claimed in claim 19, wherein said juice stream comprises a continuous stream of juice. 21. A method of purifying juice obtained from plant matter as claimed in claim 20, wherein said mixed stream comprises a continuous mixed stream. 22. A method of purifying juice obtained from plant matter as claimed in claim 21 further comprising the step of creating a reduced pressure on said mixing stream. 23. A method of purifying juice obtained from plant material as recited in claim 22, further comprising the step of configuring said juice stream to generate said reduced pressure on said mixed stream. 24. A method of purifying juice obtained from plant matter as recited in claim 19, further comprising the step of separating said dissolved material transferred to said gaseous mixture from said mixed stream. 25. A method of purifying juice obtained from plant material as recited in claim 24, further comprising the step of generating said gas mixture stream separated from said mixed supply stream from a source of reduced pressure. 26. A method of purifying juice obtained from plant material as claimed in claim 19, 23 or 25, further comprising, reducing the pressure on the interface surface between said juice and said gas mixture to Step to reduce to subatmospheric pressure. 27. A method of purifying juice obtained from plant matter as claimed in claim 1, wherein said step of reducing said dissolved matter in said juice comprises reducing the concentration of hydronium ions in said juice . 28. A method of purifying juice obtained from plant matter as recited in claim 1, wherein said step of reducing said dissolved matter in said juice comprises reducing the ability of said juice to generate hydronium ions . 29. A method of purifying juice obtained from plant matter as claimed in claim 1, wherein said step of reducing said dissolved matter in said juice comprises increasing the pH of said juice selected from A certain amount of 0.1, 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, 0.9, 1.0, 1.1, 1.2, 1.3, 1.4, 1.5, 1.6, 1.7, 1.8, 1.9, 2.0. 30. A method of purifying juice obtained from plant material as claimed in claim 29, further comprising the step of: reducing the amount of alkali added to a quantity of said juice with reduced dissolved matter content so that An initial pH of between about 11.0 and about 12.0 is formed. 31. A method of purifying juice obtained from plant matter as claimed in claim 29, further comprising the step of: reducing the amount of alkali added to a quantity of said juice with reduced dissolved matter content so that An initial pH of between about 11.5 and about 12.5 is formed. 32. A method of purifying juice obtained from plant matter as claimed in claim 29, further comprising the step of: reducing the amount of alkali added to an amount of said juice with reduced dissolved matter content, to determine the pH corresponding to the isoelectric point of at least a portion of said non-sucrose material in said juice. 33. A method of purifying juice obtained from plant material as recited in claim 1, wherein said step of reducing said dissolved matter in said juice comprises reducing generation of dissolved gases in said juice of water-soluble acids. 34. A method of purifying juice obtained from plant matter as claimed in claim 1, further comprising removing at least a portion of said juice prior to said step of contacting said juice with a gaseous mixture Insoluble step. 35. A method of purifying juice obtained from plant matter as claimed in claim 1, further comprising removing at least a portion of said juice after said step of contacting said juice with a gaseous mixture Insoluble step. 36. A method of purifying juice obtained from plant matter as claimed in claim 1, further comprising adding a first amount of alkali to said juice after the step of reducing said dissolved matter in said juice Steps in sugar juice. 37. A method of purifying juice obtained from plant matter as claimed in claim 36, wherein said step of reducing said dissolved matter in said juice is followed by adding a first amount of alkali to said juice The step of said juice includes the step of preliming said juice. 38. A method of purifying juice obtained from plant matter as claimed in claim 36, wherein said step of reducing said solutes in said juice is followed by adding a first amount of alkali to said juice The step in the sugar juice includes the step of ashing the cold juice of the sugar juice. 39. A method of purifying juice obtained from plant matter as claimed in claim 36, wherein said step of reducing said solutes in said juice is followed by adding a first amount of alkali to said juice The step in the syrup includes the step of ashing the hot juice of the syrup. 40. A method of purifying juice obtained from plant matter as claimed in claim 36, wherein said step of reducing said dissolved matter in said juice is followed by adding a first amount of alkali to The step in the juice includes adding a reduced amount of alkali to the juice based on the reduction of the dissolved matter in the juice. 41. A method of purifying juice obtained from plant matter as recited in claim 36, further comprising adding a second amount of alkali to said juice after said step of reducing said dissolved matter in said juice The step in the sugar juice includes the step of adding ash to the cold juice of the sugar juice. 42. A method of purifying juice obtained from plant matter as claimed in claim 41 , wherein a second amount of alkali is added to said juice after said step of reducing said dissolved matter in said juice. Said step in juice comprises the step of ashing said juice. 43. A method of purifying sugar juice obtained from plant matter as claimed in claim 41, wherein, after said step of reducing said dissolved matter in said sugar juice, said first amount of The step of adding base to said juice includes adding a reduced amount of base to said juice based on the reduction of said dissolved matter in said juice. 44. A method of purifying juice obtained from plant matter as recited in claim 41, further comprising adding a third amount of alkali to said juice after said step of reducing said dissolved matter in said juice The step in the sugar juice includes the step of adding ash to the hot juice of the sugar juice. 45. A method of purifying juice obtained from plant matter as claimed in claim 44, wherein a third amount of alkali is added to said juice after said step of reducing said dissolved matter in said juice The step in the sugar juice, which includes the step of adding ash to the middle of the sugar juice. 46. A method of purifying juice obtained from plant matter as claimed in claim 44, further comprising, after said step of reducing said dissolved matter in said juice, adding A fourth amount of base. 47. A method of purifying sugar juice obtained from plant matter as claimed in claim 36, 41 , 44 or 46, wherein the base is selected from calcium oxide, calcium hydroxide and milk of lime. 48. A method of purifying juice obtained from plant material as claimed in claim 36 or 41, further comprising the step of carbonating said juice with a first amount of gas. 49. A method of purifying juice obtained from plant matter as claimed in claim 48, wherein said first amount of gas is selected from the group consisting of atmospheric gases, air and carbon dioxide. 50. A method of purifying juice obtained from plant matter as recited in claim 48, further comprising the step of forming a precipitate from said base and said first amount of gas. 51. A method of purifying juice obtained from plant material as claimed in claim 41 or 44, further comprising the step of carbonating said juice with a second amount of gas. 52. A method of purifying juice obtained from plant matter as claimed in claim 51, wherein said gas is selected from the group consisting of atmospheric gases, air and carbon dioxide. 53. A method of purifying juice obtained from plant matter as recited in claim 51, further comprising the step of forming a precipitate from said base and said second amount of gas. 54. A method of purifying juice obtained from plant material as claimed in claim 44 or 46, further comprising the step of carbonating said juice with a third quantity of gas. 55. A method of purifying juice obtained from plant matter as claimed in claim 54, wherein said gas is selected from the group consisting of atmospheric gases, air and carbon dioxide. 56. A method of purifying juice obtained from plant matter as recited in claim 54, further comprising the step of forming a precipitate from said base and said third amount of gas. 57. A method of purifying juice obtained from plant matter as recited in claim 50, further comprising capturing at least a portion of said non-sucrose species in said juice with said sedimentation. 58. A method of purifying juice obtained from plant matter as recited in claim 53, further comprising capturing at least a portion of said non-sucrose species in said juice with said sedimentation. 59. A method of purifying juice obtained from plant matter as recited in claim 56, further comprising capturing at least a portion of said non-sucrose species in said juice with said sedimentation. 60. A method of purifying juice obtained from plant matter as recited in claim 57, further comprising the step of separating said precipitate entrapping said non-sucrose species from said juice. 61. A method of purifying juice obtained from plant matter as claimed in claim 58, further comprising the step of separating said precipitate trapping said non-sucrose species from said juice. 62. A method of purifying juice obtained from plant matter as claimed in claim 59, further comprising the step of separating said precipitate trapping said non-sucrose species from said juice. 63. A method of purifying juice obtained from plant matter as claimed in claim 60, further comprising the step of reducing the amount of water in said juice. 64. A method of purifying juice obtained from plant matter as claimed in claim 61, further comprising the step of reducing the amount of water in said juice. 65. A method of purifying juice obtained from plant matter as claimed in claim 62, further comprising the step of reducing the amount of water in said juice. 66. A method of purifying juice obtained from plant matter as claimed in claim 63, further comprising the step of crystallizing sucrose in said juice. 67. A method of purifying juice obtained from plant matter as claimed in claim 64, further comprising the step of crystallizing sucrose in said juice. 68. A method of purifying juice obtained from plant matter as claimed in claim 65, further comprising the step of crystallizing sucrose in said juice.

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