DE2504249A1 - High protein prod for fodder - made from lucerne by compression-expansion disintegration and ultra-filtration of liq phase - Google Patents

Abstract

High-protein prods. are manufactured from vegetable matter (lucerne) which has been cut up by feeding it by a worm conveyor to a disintegrator which operates on the compression-expansion principle. The pulp is separated in a filter centrifuge into a solid and a liq. phase. The liq. phase is separated by ultrafiltration; the concd. high-protein liq. is preheated and dried in a vacuum dryer. This process achieves a maximum recovery of the cellular fluid which contains most of the proteins. The albuminous extract is concentrated with little detriment to its contents by reducing the residence times. The process is a profitable and practical method of concentrating proteins for animal fodder. The power consumption is low.

Description

Procedure for of vegetable origin With the help of the method according to the invention, such separation tasks, which have become particularly topical in recent years, have been solved, which allow a relatively cheap and running without material damage from separation of some phases in colloidal solutions from disrupted materials - especially of vegetable origin - by the fact that after the According to the invention, the material is separated into several phases and the valuable phase, for example the concentrated solution, is dried off by a filtration carried out in two steps, preferably in a rotating field, following the digestion process.

It is known that some plants are very rich in protein. These Because of their high biological and nutritional value, proteins can be found in various standards serve as feed or food. For extraction, concentration and processing for the desired purposes, several methods are already known and patented. This is how vegetable proteins are made according to the Brit. U.S. Patent No. 705,365 without prior crushing by pressing out the starting materials and then thermal coagulation gained.

According to U.S. Patent No. 600.9o3 make proteins alkaline and subsequent thermal treatment of the squeezed out alfalfa juice for coagulation brought.

According to another method (C.H. Hartmann: J. Agr.

Food Chem. 1967, 74-9), the vegetable juices are spray-dried subjected to isolate the protein concentrates.

The one described in the Hungarian patent HO-1202 (DOS. 2.038.258) Process consists of squeezing out the comminuted raw materials, coagulation at 80-850C and separation of the coagulate. In the separated liquid phase, the still contains important nitrogenous and other nutrients, becomes a yeast culture inoculated and the yeast milk obtained after the progeneration thermolysed and spray-dried together with the previously separated coagulate (green sludge ").

According to U.S. Patent application No. 147.947 (DOS. 2.224.790) are carotenoids, Xantophylle and Ohlorophyll by changing the pH value and then Heating to So0C eliminated. The proteins that are after such treatment are also already suitable for human consumption, but are due to thermal Treatment at 80 ° C and separation of the coagulate obtained.

However, the previous methods also have some shortcomings; so ignore the fact that green plants - especially the protein-rich ones - during usually contain a great deal of water during the period of maximum protein content (65-90 °, on average 80%), i.e. during this period there is the possibility of Depreciation of raw materials greater.

The transport of raw materials, the thermal treatments of the water-rich Vegetable saps, water evaporation, liquid transport are very energy-intensive and elaborate operations; the degree of protein extraction of the processed Raw materials is significantly affected by the duration of access and storage. The above-mentioned processes do not strive for the possibility of protein production, which includes the process of juice preparation as a crucial factor that Amount of the resulting product increases significantly and in the further work phases plays a determining role.

According to the previously known method, after the comminution and pressing the plants obtained press juice thermally treated, whereupon the Proteins coagulate.

Coagulation thus effected has a deleterious effect on the Properties of the precipitated proteins, there is also a decrease their biological value.

The digestion carried out according to the previously known methods of the plant tissue, separation of cell fluids, coagulation and then Evaporation, i.e. thermal water removal, or in a word, protein extraction, are characterized by high investment and operating costs; the high energy expenditure, the Depreciation of the water-rich raw materials through storage and Transport costs are not real in relation to the degree of protein extraction.

The subject of this invention is a method, which is characterized is that a maximum recovery of the cell fluids mainly containing the proteins, a concentration of the protein-containing extract and little damage, or depreciation of the substances by reducing their residence times, economically and made possible in a practical way.

The method developed according to the above invention is based on Realization that the water content of protein, in the form of colloidal solutions occurring green cell fluids, which by continuously acting ultra-frequency Compression - expansion open-minded and from the pastes of vegetable raw materials separated by centrifugation which is continuous and has a great effect are, continuously and easily, to a relatively high degree optimal (but also arbitrarily) can be reduced by ultrafiltration, the pressure required for this also through centrifugal force is achievable. Those obtained in this way and containing little water Protein suspensions are easily transportable as a semi-main product, and the on The drying and processing costs related to the amount of raw materials are relatively low.

These low-water thick juices are indirectly referred to as 30 heated to 80 0C, and dried by the vacuum fluid, or in the conventional way.

The carotenoids, xanthophylls and chlorophylls can be extracted from the ultrafiltrate by using suitable methods extracted, where the separated water can be sprayed back onto the fields and thus a promotional one Can have an effect on the further growth of vegetation.

The fibrous plant debris can be in a number of ways can be further processed and used as desired - as a quantity enlarger for concentrated products; possibly mixed back additive in protein-rich liquid concentrates (Semi-product) - as green fodder by grinding into flour or by pelleting - as raw materials for the cellulose industry - as natural fertilizers The process enables the two main operations (separation Drying) at two different locations. In this way you can get the very water-rich vegetable raw materials with the help of several smaller movable devices in the manner described in the first part of the procedure directly at the location of the Process the harvest by using the shortest possible transport routes.

The already highly concentrated semi-finished products obtained are used in continuously processed in a central drying system.

This solution increases the flexibility of the process, his Applicability is also possible under the most extreme conditions.

The following scheme is used to explain the procedure.

0 1 2 0.1 or 2 0.3 1.1 1.2 1.3 1.4 1.5 1.6 2.1 2.2 2.3 2.4 2.5 2.6 o) Harvest 0.1 Mow 0.2 Chop 0.3 Transport 1) Separate 1.1 Feed 1.2 Material supply 1.3 Digestion 1.4 Defiber removal 1.5 Water separation 1.6 Transport 2) Drying 2.1 Storage 2.2 Preparation 2.3 Water evaporation 2.4 Powder separation 2.5 Storage 2.6 Transport The raw material (in this case the green plants) is harvested during its maximum protein content with the help of a chopper and pneumatically conveyed into a means of transport.

The profitability of the process is due to the harvesting possibilities, as well as the distance of the harvest fields to the processing plant. thats why to strive for such a solution to the problem that also distant harvesting areas are exploited can be.

In the method according to the invention, this problem is solved by that in the process step - 1 separation - one or more movable devices can be used. The invention is not concerned with the question of whether the devices of this kind, mechanically, hydrodynamically, directly with the help of an internal combustion engine or electrically (provisional remote control or, advantageously, one by one Diesel engine powered generator) should be operated.

Based on calculations and experience, the required special one would be Energy requirements in the case of a moving system are around 8-12 kWh per ton used Raw material.

If the local conditions allow it, there is also the possibility the construction of a separation block with a larger capacity next to the drying plant. The principle of the procedure for both solutions is the same.

1) Separation 1.1 The raw material transported to the device arrives in the feed unit, where the various solid impurities, in particular the iron and Metal contamination by an electromagnet or possibly also be removed by gravitational separation.

1.2 The material is fed into a multi-screw conveyor with the help of an air separator transported, which has two functions. The first is feeding a relatively thin even material layer, the second the prevention of penetration possibly unwanted solid impurities not retained (frequency level 1-2), which at the same time causes the multi-screw conveyor to come to a standstill will. This also automatically brings this facility to a standstill serving task unit.

1.3 The radially fed raw material is thereby in the digestion device promoted. This consists of a closed rotor with a large moment of inertia, the several, advantageously six or eight equally heavy and long, wedge-shaped Contains profiled knives, whereby for the purpose of easy assembly and maintenance all rotary and fasteners are secured with the aid of centrifugal force.

The stator of the disintegration device consists of a row inclined grooved insert rings, which are in pairs, proportionally spaced from each other, shifted in the direction of the movement of the material and mirror-symmetrical to each other are relocated. (These insert rings can be made of tough, wear-resistant steel will). This results in a serpentine movement of the material the meeting points of the displaced grooves. With this technical solution becomes the possibility of clogging of the plant, which is easily caused by the fibrous, moist parts of the plant could be caused, practically impossible. The short-term expansion effect created in the numerous grooves of the stator, as well as the short-term openings that came about at the openings following the grooves shock-like, but relatively high-level compression, which is dependent on repeat the movement of material 10,000 to 90,000 times per second actually represents an optimal fatigue, against the effect of which even the toughest plant fibers, or cell walls become incapable of resistance.

1.4 The digested material is then transferred to the defibering unit promoted. This advantageously consists of a continuously operating, conical solid-liquid in the form of an infinite spiral Filter centrifuge. The speed of rotation of the upper screw barrel regulating the movement of the material can be varied based on the filter drum. In order to increase the efficiency the centrifuge is the digested material with that circulated back during the filtration Water continuously washable.

1.5 The protein-containing juice separated from the plant fibers arrives continuously in an ultrafiltration apparatus, advantageously in a continuous one Ultrafilter centrifuge, in which the pressure created by the juice on the ultrafiltration layer laid with a small distance inwards from the inner transverse cover, or ultrafiltration layers, the pressure difference exerted can be varied.

The possible regeneration of the ultrafiltration layer or layers can be carried out during the work process or at a standstill.

1.6 The plants produced during the defiber removal cease still usable material because of the remaining protein content (0.5-1.5 based on the starting material used) and low water content advantageous and economical in a conventional system in a simple manner can be further processed by drying or pelleting. The product obtained is a suitable feed base for ruminants.

If such a use is not sought, made possible the low bulk weight of the product makes it easy and quick to transport to various other processing locations (e.g.

Cellulose industry, green manure, etc.).

The separated water is because of its purity without any further Treatment, cleaning, continuously derivable, i.e. it can be done with the Transporting raw material transports back to previously unused return journeys and spray again on the elder.

The one obtained as the main product, containing relatively little water Green juice is transported to the central drying plant as a concentrate.

2) Drying 2.1 - 2.2 The concentrated, for liquid transport Juice that is still suitable, the neutral pH of which must be observed, becomes the optimal one Drying utilization in one provided with an indirect recirculation preheater Drying device preheated to 5o to 8000. The circulation (homogenization) of the juice is made by one with one Screw conveyor provided Pump, then it gets into the buffer unit, where the deviating dry matter content of the material in an optimal way, possibly by membrane filtration in order to achieve an optimal degree of dryness adjustable to a maximum constant value is.

2.3 - 2.6 The preheated, a neutral pH value and a constant Material with dry matter content is used to adjust the dry matter content continuously in a vacuum fluid drying system, possibly in a vacuum paddle dryer, Vacuum plate dryer, or conventionally pulverized in a fluidized bed dryer. The powder obtained is separated by a cyclone duster. The weighed The main product is filled in waterproof bags, stored and possibly in containers transported.

According to the current state of the art, the method has the following advantages on: - the possibility of mobile execution of the first part (separation) of the the system representing the process - transport of smaller quantities of material - a fast, effective breakdown of the fibrous material with relatively little Energy expenditure - the continuous implementation of the water separation of the colloidal Sap in a plant that requires a relatively small space.

- the water separation performed in the first part of the process is a continuous process due to the relatively low expenditure of energy The production of the concentrates is resolved with the release of heat energy at lower temperatures that avoid the thermal degradation of proteins - the relatively short dwell times of the material in the system ensure a significant reduction in the degree of damage.

- Significantly lower investment, production and maintenance costs Apart from the aforementioned advantages, the procedure is different from others continues because the problem of creating a modern agricultural-chemical-technological Plant for the production of proteins, a big question of our time, such it is resolved that it is realizable in a very short time, and that the character of the farm, what the various agricultural conditions and circumstances is very flexible because of the possible mobility.

The method continues to differ from the previously known ones in that there is a high degree of defiber removal in an individual device opened green vegetable pulp in a specially constructed for this purpose Filter centrifuge, as well as the introduction of a new work step, ultrafiltration, advantageously the ultrafiltration centrifugation, which allows the Water content of the colloidal solutions is easily separable. The procedure enables in the further phase of drainage in order to improve the quality the Products use a modified, working at low temperatures Vacuum dryer.

The following examples serve to explain the process, where the first example was carried out according to the previously known method, the second, however, according to the method according to the invention: example 1 loo N of coarsely chopped alfalfa harvested during the maximum protein content were crushed and then squeezed in a press, with 52 N green juice and 48 N press cakes were recovered. The liquid phase was drained with water heated directly to 80 ° C, whereby a green, sludge-like coagulate separated. To the deposition of the coagulate and subsequent drying gave 3.2N of a green powdery product, which had the following composition: raw material Product water 78.90 N o, 11 N crude protein + 4.71 N 1.24 N fibers 5.26 N o, 31 N nitrogen-free Extract 7.96 N 1.35 N, mineral substances 3.17 N o.39 N + nitrogen content x 6.25 Example 2 100 N of alfalfa harvested during the maximum protein content were chopped into Form mechanically opened in the apparatus described above. It remained a Slurry which had the following composition: water 78.96 N dry substance 21.04 N consisting of crude protein + (X.p.) 4.68 N fibers (F) 5.21 N nitrogen-free extract (N.f.Ex) 8, o2 N minerals (M.s.) 3.13 N + N content x 6.25 after digestion the pulp was separated into two components in a Xegel screw filter centrifuge: 21.76 N fibrous residue and loss and 78.24 N colloid solution with the following Composition: water 69.69 N dry matter 8.55 N R.p. 3.31 N F. o, 15 N N.f.Ex 3.56 N M.s. 1.53 N The solution was divided into two more using a membrane filter Phases separated, namely: 62.18 N ultrafiltrate and loss (thin liquid, T.S. 2,7jo) and 16, o6 N concentrate (concentrated solution, T.S. 42.9), which was preheated to 4500 and then dried, whereby 7.18 N of a powdery end product with the following composition was obtained: water 0.31 N dry matter 6.87 N R.p. 3.18 N F. o, 14 N i.f.Ex 3.13 N M.s. o, 42 N.

Claims (15)

Claims O Process for the production of protein-rich products of vegetable origin characterized in that the during the maximum protein content harvested coarsely chopped vegetable parts with the help of a multi-screw conveyor perpendicular to the axis in a thin layer and continuous with the disintegration device are fed on the principle of compression - expansion in the area of high frequencies works. The opened pulpy material ends up in a Filter centrifuge, with the speeds of the screw drum and the filter drum are different; thereby the material in the rotating field is in two phases, separated into a solid and a liquid. The liquid phase is with the help of a or several selected depending on the molecular weights of the proteins to be separated Ultrafiltration layers, advantageously deposited in a rotating field. the concentrated protein-rich i'liquid is preheated and in the drying device, advantageously dried in a vacuum dryer. 2) Method according to claim 1, characterized in that the method steps Material supply, separation of fibers and water separation in one compact system, advantageously in a mobile system, carried out directly on the front panel will. 3) Method according to claim 1 - 2, characterized in that the Digestion of the coarsely comminuted material in a very short time with a Frequency of 1o, ooo to 9o, ooo is reached, namely in the opening device, which consists of a rotor and a stator. The one with a large moment of inertia closed Rotor contains several equally heavy and long on the cylinder jacket in the vertical direction attached, wedge-shaped profiled knives fixed with the help of centrifugal force, where the ratio between the diameter and the guide line direction of the rotor c is 1. The stator consists of a row in the direction of material movement displaced obliquely grooved, in pairs proportionally more distant from each other Mirror-symmetrically laid tough and abrasion-resistant crown rings. Such a solution of the stator and rotor allows a serpentine, in one to 1.5 t Radians belonging path in an active way taking place material advancement, whereby opening up through compression and expansion on the groove-shaped surface arises. 4) Method according to claim 1 - 3, characterized in that the defibering takes place in a field of rotation, the ratio between the diameter and the axial length dimension of the device is C 1. 5) Method according to claims 1-4, characterized in that the weight The ratio of the defibrated material to the raw material fed in is from 0.6 to 0.8. 6) Method according to claims 1-5, characterized in that the concentration of the defibered, protein-containing juice carried out in an ultrafiltration device will. 7) Method according to claim 1-6, characterized in that the Concentration, water separation of the defibered protein-containing juice, advantageously in a continuous ultrafilter centrifuge, whereby the pressure of the penetrating juice to that of the inner transverse envelope Ultrafiltration layers or ultrafiltration layers not laid inside with a small gap exerted pressure difference is variable. 8) Method according to claim 7, characterized in that the surface the rotating membrane envelope is orthogonal to the radius of the rotating field, and the particles of the material to be separated, i.e. to be concentrated, which in a space with an even larger radius than that of the rotating membrane envelope move in a spiral and in the direction of the guide line. 9) Method according to claim 6-7, characterized in that for the ultrafiltration of the juice such membranes are used, the substances with molecular weights hold back from 500 to loo.ooo. lo) Method according to claim 6-7, characterized in that the causing the ultrafiltration process on both sides of the membrane surface The resulting pressure difference to a value of 104 to 1o6 Pa in the function the degree of separation is adjustable. 11) Method according to claim 6-7, characterized in that the Dry matter content of the separated, i.e. concentrated juice to a value of 1o - 90, advantageously can be set to 20 - 50. 12) Method according to claim 1-11, characterized in that the when making juice at 3o to So0C a fixed dry matter content homogenized juices are preheated to 3o - 8o0 0. 13) Method according to claim 1, characterized in that the preheated Dried juices between 20 and 2000C, advantageously between 30 and 10,000 will. 14) Method according to claim 4'7,8'1o characterized in that the deposition of some, preferably in solid or liquid form Dietary fiber, in particular water, without supply of heat energy and in a rotating manner Space is carried out. 15) The method according to claim 1-13, characterized in that the Increase in the protein-rich, powdery concentrate quantities through the admixture the separated fibrous residues suitable as ballast material for animal feed, to the protein-rich liquid concentrate and by drying and possibly Pelleting the new product is achieved.