HK1151552B

HK1151552B - Method and device for photochemical process

Info

Publication number: HK1151552B
Application number: HK11105452.7A
Authority: HK
Inventors: Martin Mohr; Franz Emminger
Original assignee: Ecoduna Og
Priority date: 2008-01-31
Filing date: 2009-01-27
Publication date: 2016-01-29

Description

Method and device for photochemical processes

The invention relates to a method for photochemical (e.g. photocatalytic and/or photosynthetic) processes, in particular for the propagation and preparation or hydroponic (preferably phototrophic) cultivation of microorganisms, wherein a reaction medium (e.g. an aqueous solution or suspension) is introduced into a reactor in a meandering manner.

A bioreactor for phototrophic microorganisms is known from DE 4134813 a1, which is made of glass or plastic. Culture medium is pumped or directed downwards through the bioreactor in a meandering manner through horizontally positioned wall panels (stegpatte). Furthermore, a turbulence generating means is located in the wall (stem). According to this method, carbon dioxide is introduced at the top, operating with natural or artificial light. The bioreactor is positioned or tracked at right angles to the light source.

Furthermore, bioreactors for phototrophic microorganisms or for photocatalytic processes are also known from GB 2235210A and DE 19644992C 1.

Photocatalytic purification of waste water in a bioreactor is known from EP 738686 a1, in which the liquid to be cleaned is guided through a multi-wall panel (stegmehrfachplane) made of transparent plastic. For temperature regulation, conventional translucent multi-wall panels can be used.

Furthermore, in WO 98/18903 an active or passive temperature-adjustable solar element made of a multi-wall sheet with at least three ribbons (Gurt) is described. The layers within the reactor are alternately used for photochemical or photosynthetic processes. The culture medium is thus introduced in a meandering manner downwards into a sealed reactor with a sealed front and horizontally positioned wall plates.

Of course also from e.g. Florian Manfred“Teilautomatische Generierung von Stromlauf-und Archimedes (Archimedisch) helix and DaVinci (Da Vinci) helix are known from fur mechnisch System "(article 2006, Munchen Tech. Univ.) ISBN 103-8316-0643-9.

Furthermore, a hydraulic screw with a trough and a generator for generating electricity is known from DE 19507149C 2. A hydraulic screw for energy conversion is known from DE 4139134C 2.

Naturally, the hydrostatic balance of the force is referred to as the hydrostatic paradox, also known as the Pascal (Pascal) paradox. The paradox describes the phenomenon that the liquid generates a gravitational pressure at the bottom of the container depending on the filling level of the liquid, but the shape of the container is not affected.

Open-topped and bottom-connected vessels are referred to as communicating vessels or tubes. The homogeneous fluid has the same height in these because the air pressure and gravity have equal effect on the container. In the case of heterogeneous liquids, the height of the liquid column is inversely proportional to its specific gravity.

Typically, the transport in the solar reactor is by conventional pumping methods, as in some of the methods described above. This procedure stresses the microorganisms in the reaction medium due to high pressure, negative pressure, strong acceleration or squeezing. Most phototrophic microorganisms lose their potential photosynthetic capacity under the action of this stress. The cells are destroyed, damaged and or the microorganisms require time and/or metabolites for regeneration before they can fully restore the process assigned to them. Likewise, most photochemical processes are also reduced in their potential photocatalytic capacity under such stress because the molecules are destroyed or damaged and/or require time and/or additional oxidizing agents before they can fully restore the process to which they are assigned.

Furthermore, a solar generator is known from DE 2951700C 2, which is fixed to a boom shaft suspended from a building.

The object of the present invention is to produce a process of the above-mentioned type which on the one hand avoids the above-mentioned disadvantages and on the other hand enables the yield or yield (Ernte) to be increased qualitatively and in particular quantitatively.

The method according to the invention is characterized in that the meandering conveyance of the reaction medium takes place at least once vertically or obliquely at an angle from top to bottom or in the direction of gravity and from bottom to top or against the direction of gravity, and that the introduction and removal of the reaction medium into and from the reactor take place preferably continuously, without pressure or freely to the atmosphere at the upper surface of the reaction medium, wherein a reaction medium flow which is stress-free for the microorganisms is produced as a result of the hydrostatic pressure compensation and levelling compensation. With the present invention, smooth transport of microorganisms can be achieved for the first time, so that damage during the process for preparing the same is prevented. By controlled introduction of the reaction medium into the upper liquid surface region, the flow-through velocity of the reaction medium through the reactor unit can be defined, provided of course that the reactor unit is full. The reaction medium flows in a meandering manner through the reactor units which are in vertical communication with one another. The reactor units are connected to each other in such a way that both the inlet and the outlet are located above. The reactor unit is fully or partially open towards the top. This flow-through is achieved by using hydrostatic pressure compensation with minimal height loss throughout the reactor. Since the reaction medium is transported largely pressureless and gravimetrically in the biological solar reactor, the influence on the reaction process is as small as possible.

For example, the method according to the invention can be used in the following fields of application:

photochemical and/or photosynthetic purification of wastewater

CO removal by phototrophic microorganisms₂Photosynthetic metabolism into oxygen

Propagation and preparation of phototrophic microorganisms for research purposes

Investigating photochemical and/or photosynthetic processes

Propagation and preparation of phototrophic microorganisms for food and food material raw materials

Phototrophic microorganisms for the propagation and production of raw materials for the pharmaceutical industry

-propagation and production of phototrophic microorganisms for fuels and feedstocks for fuel production and power generation

Phototrophic microorganisms for the propagation and production of raw materials for the chemical industry

Propagation and production of phototrophic microorganisms which emit usable gas (e.g. hydrogen) during the photosynthetic process

The stress-free transport of the optionally co-transported microorganisms can be approximated by using hydrostatic compensation during the flow of the reaction medium through the reactor unit. Furthermore, optimization of the energy, specific light transmission, optimization of the space, supply of additives, specific temperature control, targeted regulation and improvement of the gas recovery can be achieved.

According to another particular feature of the invention, liquid and/or gaseous additives, such as nutrient solutions and/or oxidizing agents and/or active substances and/or dissolved substances that promote the process, are introduced continuously or batchwise into the diverting area of the reaction medium, preferably during the process, preferably at the bottom end. In this way, the introduction of nutrient solutions and process-promoting solutions and the introduction of nutrient gases and process gases can be controlled and optimized. All interventions in the reaction medium are preferably performed at the bottom end of the reactor unit.

According to another embodiment of the invention, the additive is thoroughly mixed and homogeneously distributed in the reaction medium by introducing the additive at the bottom end of the liquid column. In this way, a vortex of the reaction medium is generated by the rising of the gas.

According to a particular further development of the invention, the incorporable additives are introduced at a specific temperature. In this way, thermal regulation is achieved by the inflowing gas and/or nutrient solution.

According to a particular feature of the invention, the liquid and/or gaseous substance or additive is introduced at the bottom end in a turn-around region of the reaction medium, wherein a greater amount of liquid and/or gaseous substance or additive is introduced in the region of the reaction medium flowing from bottom to top or against the direction of gravity than in the region of the reaction medium flowing from top to bottom or in the direction of gravity. In this way-according to the operation of a pneumatic lift (mamutpump) -the liquid level in the pipe or chamber flowing from bottom to top is raised in a "gas lift effect" manner compared to the pipe or chamber flowing from top to bottom. Such a level difference can lead to an increase in the level at the end of the last tube or chamber compared to the first tube or chamber in the case of a plurality of such units connected in series and introducing a greater amount of gas in the respective riser, if this increase in level is taken into account in the construction of the reactor. Despite the increased introduction of additives, preferably gaseous additives, the microorganisms can be transported without stress.

According to another particular feature of the invention, it is preferred that in the process, the removal of gaseous process products (e.g. oxygen) is carried out through the surface of the reaction medium.

In this way, a controlled and optimized reduction of harmful substances can be achieved, whereby the optimized removal also allows the collection of gaseous process products.

According to another particular development of the invention, the reactor is rotatably adjusted or controlled across the entire arch of the horizontal solar trajectory to be adapted to the solar irradiation (sonneneintrahlung). In this way, an optimization of the solar irradiation for the bio-solar reactor is achieved. Thus, providing optimized natural lighting for phototrophic microorganisms for a wide variety of different applications in different biological solar reactors for photosynthetic processes is suitable in terms of properties and the desired propagation sequence. Furthermore, it is possible to match and/or change the light behavior during the day. An increased and reduced exposure of the microorganisms to solar radiation can be achieved for better utilization of the light or for protection against too strong irradiation.

Furthermore, it is also an object of the present invention to provide an apparatus for carrying out the method.

The apparatus for carrying out the invention according to the method, in which a reactor, in particular a bioreactor, is provided which is composed of tubes, is characterized in that the reactor is composed of at least one reactor unit which is formed by two vertical tubes connected at the bottom, and in that the inlet and the outlet are both provided at the upper edge of the reactor.

An alternative apparatus of the invention for carrying out the method, wherein a reactor, in particular a bioreactor, is provided having elements made of wall plates or multi-wall plates, characterized in that the reactor is composed of at least one reactor unit formed by two, preferably rectangular, vertical chambers formed by wall plates or multi-wall plates, which are formed by partition walls open at the bottom, and that both inlets and outlets are provided at the upper edge of the reactor.

The reactor, in particular the bioreactor, can be made of transparent, translucent, coated and uncoated materials. Likewise, the tube or wall plate can be made of glass or a plastic transparent to light or UV light, for example polymethyl methacrylate. The reactor unit can be constructed from conventional and optionally machined and specially finished elements that meet the above requirements. The reactor units are arranged in such a way that a continuous meandering flow from top to bottom and from bottom to top is ensured. An inlet to the reactor and an outlet from the reactor are provided in the upper region.

Due to hydrostatic pressure compensation, the reaction medium flows in a vertically meandering manner through the entire reactor after entering the reactor. Once it reaches the last reactor unit, the reaction medium leaves the hydrostatic bioreactor and is introduced pressureless or not into a maturation tank or a receiving vessel or another reactor. From the receiving container, the reaction medium can be finally processed or can be stored or further processed without stress.

According to a particular feature of the invention, the partition wall for connecting two or more reactor units into a reactor panel is designed to be lower than the partition wall between the tubes or chambers of the reactor units, as a result of which an overflow or communication opening is created when the liquid level within the reactor unit is higher than the partition wall between the reactor units. The reactor unit is designed as a communicating vessel. By connecting the reactor units in this type of series into reactor panels, the option of producing a defined flow path is provided.

The optimum residence time in the entire reactor, which is adapted to the individual phototrophic microorganism or photochemical requirements and which meets the process results, can be influenced by the following parameters:

velocity of flow through

Cross section of the reactor unit

Height of the reactor unit

-the amount and conditions of the non-gaseous substance introduced; condition, quantity, density and pressure of gas blown in

Number of reactor units connected in zigzag transport

Possibility of removing process exhaust gases

Process temperature

Dwell time and position of orientation light

Residence time in maturation and or dark tanks

Optionally, in the ideal case and corresponding constructional conditions, the medium can be conveyed uniquely continuously from the inlet to the outlet for the entire process.

According to a particular embodiment of the invention, the reactor panels, which are preferably connected in series with one another, are arranged in a reactor, which are parallel to one another and are preferably fixedly mounted in a frame-like clamping device, and the reactor can be adjusted with respect to the light incidence by means of a rotating device via at least one preferably vertical axis, whereby the reactor can be provided (in particular fixed, suspended or floating) on a floating body. Due to the clamping device and the bearing, any angle of irradiation towards the sun is possible. Optimization of the light is achieved by control according to the sun's trajectory or tracking. For example, for certain applications, reducing exposure can be achieved at noon by removing or masking.

Since the phototrophic microorganisms are only subjected to an optimization of the photosynthetic process in the region close to the surface, and the absorption and splitting are influenced by excessive UV irradiation damage, it is advantageous to carry out both the outer region as well as the inner part of the reactor unit.

Too strong direct irradiation of UV light can damage or impair the growth of the microorganisms and raise the temperature of the reaction medium beyond the desired level, which must be cooled again.

Due to the thorough mixing of the reaction medium, all the phototrophic microorganisms reach to a sufficient extent the light-filled light region of the reactor unit close to the outer wall.

For photocatalytic oxidation it is advantageous if all molecules are introduced into the light-filled region of the reactor unit near the outer wall of the reactor unit interior.

In most cases a positioning almost parallel to the light source or the reactor tracking the solar radiation parallel will be sufficient, thus enabling a better utilization of the space as a whole.

Furthermore, the nearly parallel irradiated light is partially reflected by the reactor surface and is available for the opposite reactor.

In the case of weak solar radiation, poor geographical location, or in the case of phototrophic microorganisms or photocatalytic processes which require light in particular, the reactor can be selected to be positioned at any angle towards the light source.

In a preferred variant for enabling the biological solar reactor to track the sun, its top and optionally its bottom are fixedly mounted in the solar member so that the reactor panels do not change position towards each other when the solar member tracks the sun illumination, but the entire solar member is rotated. The reactor panels (which can be flat or pooled into a single tube, transparent, translucent, coated and uncoated) are arranged in a manner that makes them suitable for the propagation of microorganisms batchwise in a stationary culture medium and/or continuously in a flowing culture medium.

According to a further development of the invention, a sensor is provided to grasp the sun trajectory, by means of which the rotation for the reactor for the incidence of light is controlled. The solar trajectory is determined by suitable sensors and transmitted to the reactor as a synchronous or arbitrarily defined rotation. Naturally, the control can also be performed using data relating to coordinates, time and date.

According to a particularly further development of the invention, the light incidence for the reactor is carried out by artificial illumination. The reactor can be constructed in such a way and in such a way that it can be supplied with energy and the illumination medium, which is advantageously used for the phototrophic microorganisms, can be immobilized.

In accordance with a particular embodiment of the invention, the rotation of the light incidence in a system consisting of a plurality of reactors is preferably synchronized for all reactors. In a system consisting of a plurality of reactors, the rotation of all the reactors of the entire system can be synchronized in such a way that by positioning the reactor panels almost parallel to the solar irradiation, further reactors located behind according to a basic arrangement are not obstructed. In this way, ideal entry of sunlight can be ensured.

According to a further development of the invention, at least parts of the reactor panels and/or the reactor, in particular the outer surfaces, are designed to reflect light. In this way, the effect of natural or artificial lighting can be enhanced.

According to another particular feature of the invention, it is preferred that during the process, at least one introduction inlet is provided at the bottom of the reactor in the turning zone of the reaction medium for the purpose of introducing, continuously or batchwise, an additive, such as a nutrient solution or a nutrient gas and/or an oxidant and/or an active substance and/or a dissolved substance or gas that promotes the process.

The reaction medium can optionally be enriched with substances dissolved in the liquid before entering the reactor, which meet the requirements of the microorganism or the requirements of the process, and/or fluid nutrients or oxidants are supplied in the reactor during the passage.

The reduction of the nutrient content in the reaction medium caused by the stable growth of the microorganisms during the photosynthetic process can be compensated by the continuous and/or batchwise introduction of nutrient solutions.

It is likewise possible to compensate for the reduced efficiency of the reaction medium in the photochemical process caused by the continuous reaction by introducing further active substances continuously and/or batchwise.

For the introduction of fluid nutrients or oxidants, feeding possibilities are created at the bottom of the reactor unit by means of controllable valves. Due to the meandering transport of the reaction medium and/or due to the rise of the fluid active substance, thorough mixing and distribution is ensured throughout the reactor.

Naturally, gaseous nutrients, oxidants or active substances can also be introduced in this way.

The introduced gas causes self-cleaning of the inner surface of the reactor due to the rising of the gas bubbles. A sample removal point for detecting the progress of the process is also provided at the bottom of the reactor unit.

According to a particular feature of the invention, for introducing the additive into the turning areas of the reactor unit and/or reactor panel, a bore for a pipe, preferably a continuous pipe, in particular a gas pipe arrangement with a micro bore, is provided. The bore is arranged on the gas pipe in such a way that gas entrainment and mixing of the reactor medium in the individual reactor units of the reactor panel are ensured.

According to a particular embodiment of the invention, the gas tube has a greater number of micro-drilled holes and/or micro-drilled holes with a greater diameter in the region of the reaction medium flowing from bottom to top or against the direction of gravity than in the region of the reaction medium flowing from top to bottom or in the direction of gravity. In this way, the aforementioned "airlift effect" is achieved in terms of equipment technology.

According to another development of the invention, the gas pipe has an external and/or internal thread at both ends. For example, the gas tube is designed in such a way that it can be gas-tightly isolated from the assembly using a lock nut. At least one of the locking nuts has a connection for a gas line.

Furthermore, the gas pipe can have a connection piece via its internal thread, which can in turn be screwed onto another gas pipe.

For replacement, the lock nut is unscrewed at one end, the connector is installed, and a new gas pipe is installed at the other end of the connector. Using the new gas tube, the gas tube to be replaced is pushed through the assembly and thereby simultaneously takes up its position. In this way it is ensured that the gas pipe to be replaced is pushed through the assembly with minimal gas or liquid loss using the new gas pipe. The design allows for maintenance or modification of the air intake unit without interrupting operation or with only minimal impact on the process.

According to another particular feature of the invention, for the removal of gaseous process products, preferably gaseous process products produced in the process, such as oxygen, a removal outlet is provided which is provided above the surface of the reaction medium or above the upper surface of the reactor unit. Due to the pressure-free state in the reactor unit, gaseous process products (e.g. metabolites) formed during the photosynthetic or photochemical process can rise freely in the reaction medium.

By the fully or partially open configuration of the reactor unit towards the top, the gaseous process products can escape and/or be evacuated.

The removal of the process off-gas is facilitated by the rise of bubbles formed in the process and/or optionally controlled by the additionally blown-in gas.

In accordance with an embodiment of the invention, for removing gaseous process products, a collecting device can be provided with a removal outlet provided above the liquid level of the reaction medium or above the upper surface of the reactor unit. Thus, the gaseous process product can be collected and optionally provided for further utilization or disposal. By means of the closed construction, it is also possible to avoid losses of the reaction medium due to evaporation and/or due to leakage and to carry out controlled discharge and collection of the gases.

According to an advantageous further development of the invention, a siphon is provided before the inlet and/or after the outlet. The inflow to the reactor is located in the upper region. The reaction medium can be introduced into the first reactor unit pressureless or pressureless, and optionally gastight, via a siphon and be conducted away after the reactor via a further siphon pressureless, and optionally gastight.

According to a particular feature of the invention, an archimedean screw or a da vinci spiral is provided for conveying the reaction medium, both inside the reactors and between the reactors. In the case of this arrangement, one or more tubes or walls are helically wound around a shaft having one or more bearings and securely mounted using any technique (e.g., screwing, bonding, etc.). The associated tube or wall is open at both ends. The transport unit is aligned and supported in such a way that the bottom end of the tube or wall draws the reaction medium from the container. However, the tube or wall is only impregnated into the reaction medium to such an extent that the tube end or wall emerges from the surface outside the reaction medium on respective rotation.

By slowly rotating in a spiral direction, which does not result in any significant centrifugal force, the reaction medium in the respective lower half of the tube or wall is conveyed to the upper end of the spiral with compensation by hydrostatic pressure. Under each rotation, the liquid contained in the upper half-turn is released and descends into the container situated at a higher level than the original container. By alternately completely or partially closing the delivery device, leakage losses and/or gas venting can be prevented.

The invention is explained in more detail on the basis of exemplary embodiments shown in the drawings.

The attached drawings show:

FIG. 1 is a bioreactor consisting of tubes,

figure 2 is a top view according to figure 1,

figure 3 is a side view according to figure 1,

FIG. 4 is a bioreactor constructed of wall panels,

figure 5 is a top view according to figure 4,

figure 6 is a side view according to figure 4,

figure 7 is a schematic view of a tube,

figure 8 is a schematic illustration of the "airlift" effect,

figures 9 and 10 are schematic diagrams of the application of this "airlift" effect,

figure 11 is a bioreactor with an archimedes screw,

figure 12 is a view of a biological solar reactor,

figures 13 and 14 are schematic illustrations of solar irradiation on the bioreactor.

According to FIGS. 1 to 3, the reactor, in particular the biological solar reactor 1, comprises at least one reactor unit 2 formed by two vertical tubes 3 connected at the bottom. At the upper edge of the reactor an inlet 4 and an outlet 5 are provided. To assemble the bio-solar reactor 1, a plurality of reactor units 2 are connected in series, whereby the outlet 5 is always connected to the inlet 4.

Such a bio-solar reactor 1 is used in a method for photochemical processes, such as photocatalytic and/or photosynthetic processes, in particular for propagating and preparing or hydroponically (preferably phototrophic) microorganisms. For its operation, the biological solar reactor 1 is filled with a reaction medium 6 (for example an aqueous solution or suspension). During operation, the bio-solar reactor 1 is fed only through its first inlet 4. The direction of transport or flow of the reaction medium 6 is vertical, preferably vertical, once from top to bottom and once from bottom to top in the reactor unit 2. If a plurality of reactor units 2 communicating with each other are connected in series, the reaction medium 6 flows through the reactor in a meandering manner. The introduction or supply of the reaction medium 6 into and removal from the biological solar reactor 1 is preferably carried out continuously, without pressure and freely into the atmosphere via the upper surface of the reaction medium or a region close to or above the upper liquid level.

The reactor units 2 are thus connected to each other in a meandering manner as communicating tubes 3, wherein the inlet 4 and the outlet 5 are located at the top. The reactor unit 2 is fully or partially open towards the top, as required. Due to the hydrostatic pressure compensation and the levelling out compensation, a flow of reaction medium 6 is created by feeding reaction medium 6 at inlet 4. For this method, this means that a flow of the reaction medium 6 is produced which is not stressed by the microorganisms. In this way, a free flow can be formed between the individual reactor units 2 without having to apply any further energy. The reaction medium 6 moves zigzag through the reactor with minimal height loss in an effort to compensate the liquid for the height difference between the inlet 4 and the outlet 5.

Alternative designs for the bio-solar reactor 1 are shown in accordance with fig. 4-6. The bio-solar reactor 1 consists of a wall plate or multi-wall plate 7. In the case of this design, the reactor unit 2 consists of two preferably rectangular vertical chambers 8 formed by wall plates or multi-wall plates 7, which are formed by partition walls 9 open at the bottom. Both an inlet 4 and an outlet 5 for introduction or supply are provided at the upper edge of the reactor. In the exemplary embodiment according to fig. 4 two reactor units 2 have been connected.

If two or more reactor units 2 are connected, their partition wall 10 is designed to be lower than the partition wall 9 between the pipes 3 or chambers 8 of the reactor units 2. Therefore, an overflow or a communication opening is generated when the liquid level in the reactor units 2 is higher than the partition walls 10 between the reactor units 2. In this way, energy consumption is minimized, since pumps can be largely omitted between the process steps and any number of identical or different process steps can be interconnected at the same flow level.

The individual reactor units 2 can be designed to be transparent or translucent or, if desired, also opaque. As material glass or UV-transmissive plastic can be used, for example polymethyl methacrylate.

The bio-solar reactor 1 is filled and operated in a manner similar to the design of fig. 1-3.

With respect to light incidence on the reactor unit 2, which will be described in more detail later, a tilted reactor is shown according to fig. 6. Despite the reactor being inclined at an angle, the reaction medium 6 flows once from top to bottom or in the direction of gravity and from bottom to top or against the direction of gravity.

According to fig. 1 and 4, it is preferred that during the process, for the purpose of introducing the additive 12 (e.g. nutrient solution or nutrient gas and/or oxidant and/or active substance and/or promoting the same) continuously or batchwiseDissolved substances or gases of the process), at the bottom of the reactor in the turning zone of the reaction medium 6, at least one introduction inlet 11 (e.g. a controllable valve) is provided. According to said method, the reaction medium 6 is optionally treated with CO before entering the reactor₂Or other gas saturation. Concentrating the saturation according to the needs of the process and/or feeding CO during the residence in the reactor₂Or other gases. Capable of introducing CO continuously and/or intermittently₂Compensating for CO in the reaction medium 6 due to the steady growth of microorganisms during the photosynthetic process₂And (4) reducing the content.

The reduced efficiency of the reaction medium caused by the continued reaction in the photochemical process can be compensated for by the continuous and/or intermittent introduction of further reactive gases.

By introducing the additive at the bottom of the liquid column via the introduction inlet 11 according to fig. 7, the additive is thoroughly mixed and homogeneously distributed in the reaction medium 6.

The introduction of additives 12, such as fluids and gases, also optimizes the light supply, since all molecules or phototrophic microorganisms are guided sufficiently to the light-filled light region of the reactor unit 2 close to the outer wall, indicated by the arrow 13, due to the vortex created in the reaction medium 6.

The introduction of fluid and gas creates a vortex in the reaction medium 6, whereby another advantageous effect is achieved, namely a continuous cleaning of the inner surfaces of the reactor due to the rising of gas bubbles.

Furthermore, the reaction medium 6 can also be heated or cooled by the specific introduction of fluids and gases. The introduced additive 12 can thus be used for controlled temperature regulation of the reaction medium 6.

According to FIG. 8, the liquid and/or gaseous substances or additives 12 are introduced at the bottom in the turning region of the reaction medium 6. In a particular embodiment of the reactor, a greater amount of liquid and/or gaseous substances or additives 12 is introduced in the region of the reaction medium 6 flowing from bottom to top or against the direction of gravity than in the region of the reaction medium 6 flowing from top to bottom or in the direction of gravity. In this way, as previously described and according to the operation of the air-lift, the liquid level in the pipe 3 or chamber flowing through from bottom to top is raised in a "gas-lift effect" manner compared to the pipe 3 or chamber flowing through from top to bottom. Such a level difference a can lead to that in case of a plurality of reactor units 2 connected in series and more gas is introduced in each riser 3, the level at the end of the last tube 3 or chamber is raised compared to the first tube 3 or chamber if this level rise is taken into account in the design of the reactor. Despite the increased introduction of the additive 12, preferably a gaseous additive, the microorganism can still be delivered without stress.

According to fig. 9, this increase is taken into account in a reactor design of the same structural design with reactor units 2 connected in series, for example if the base of the reactor is increased to the same extent.

In the case of the application of the "gas lift effect", the positioning of the reactor panel 18 at an angle along the panel axis provides the following advantages:

the medium is introduced into the reactor panel 18 in the inlet opening 4, whereby the reactor panel is inclined at an angle along the panel axis such that the inlet 4 is located lower than the outlet 5. Due to the "gas lift effect", it creates a higher water column in each second tube of the reactor panel 18 and the medium is able to flow to the next tube despite the higher liquid level and form a communicating vessel so raised.

The inclination is set at an angle which does not cause a back-overflow of the wall 9 separating the two liquid columns in the reactor unit 2.

If this maximum possible angle is exceeded, the medium will flow through the tube 3 after passing back into the tube through which it passed before flowing against the action of gravity in the tube 3, whereby a closed circuit with a gas-lift circulation is created.

By varying the inclination of the reactor deck 18 and the gas pressure or quantity, the desired fall of the "gas lift effect" can be adjusted, thereby resulting in control of the flow rate as the level of the upper edge of the liquid increases.

In another example of application (fig. 10), the flow rate can also be controlled by tilting a certain angle if no "gas lift effect" occurs due to little or no gas introduction.

The reaction medium 6 is introduced into the inlet 4 into a reactor panel 18 which is inclined at an angle along the panel axis such that the inlet 4 is located higher than the outlet 5.

Although the compensation of the hydrostatic pressure level of the liquid level between the individual reactor units 2 is still effective, a small drop in pressure is generated in each reactor unit 2 of the reactor panel 18, which has an accelerating effect on the flow velocity through the reactor panel 18.

The inclination is set at an angle which at the most does not result in an overflow of the wall 9 separating the two liquid columns in the reactor unit 2 in the direction from the inlet 4 to the outlet 5, since in this case no flow takes place in the pipe 3, and the medium will only flow further upwards through the wall 9, the medium in the reactor unit 2 will enter a stagnant state.

By varying the inclination of the reactor deck 18 and the gas pressure/quantity, the required head can be adjusted, thereby resulting in control of the flow rate as the level of the upper edge of the liquid decreases.

This "gas lift effect" can therefore be exploited by means of the examples listed below:

elevation of the upper edge with water:

additional height for the settler

Additional height to overcome flow paths between reactors or process steps

-operating the hydrocyclone with water flowing downwards.

Flow-through filters

-separating the product from the reaction medium.

Flow through a preparation system for reusing the medium

No additional pump energy is used in the overall system

Invariance of the upper edge with water:

no height is lost for overcoming in this phase of the process.

Good control of the flow rate.

Moderate turbulence (supply light and prevention of film formation) and economic operation if just little gas is needed in the process.

With a smaller reduction of the upper edge of the water:

without significant loss of height for overcoming in this phase of the process (downstream airlift)

Good control of the flow rate

The gas required for the vortex is minimized (supply light and prevention of film formation) and therefore economical to operate if just little gas is required in the process.

The aim is to control the entire system in such a way that no additional energy has to be used for the flow of the medium in the entire system, apart from the gas lift at an economically sensible location.

In order to introduce the additive 12 into the reactor unit 2 and/or into the turning zones in the reactor panels 18, a bore 20 is provided for a pipe, preferably a continuous pipe, in particular a gas pipe 21 arrangement with a micro bore 22. In order to increase the introduction of the gas additive 12, the gas tube 21 has a greater number of micro-drilled holes 22 and/or micro-drilled holes with a greater diameter in the region of the reaction medium 6 flowing from bottom to top or against the direction of gravity than in the region of the reaction medium 6 flowing from top to bottom or in the direction of gravity.

In order to quickly replace the gas tube 21 (fig. 8), it has external and/or internal threads 23 at both ends. The gas tube 21 is designed, for example, in such a way that it can be gas-tightly isolated from the assembly using a union nut. At least one of the locking nuts has a connection for a gas line.

Furthermore, the gas tube can have a connection 24 via its internal thread, which can in turn be screwed onto the other gas tube 21.

For replacement, the lock nut is unscrewed at one end, the connector 24 is installed, and a new gas pipe 21 is installed to the other end of the connector 24. Using the new gas tube 21, the gas tube 21 to be replaced is pushed through the assembly and thereby simultaneously takes its position. In this way it is ensured that the gas tube 21 to be replaced is pushed through the assembly with minimal gas or liquid loss using the new gas tube 21. The design may allow for maintenance or modification of the air intake apparatus without halting operation or with only minimal impact on the process.

As an alternative or in addition to the above-mentioned "gas lift", the bio-solar reactor 1 can have an archimedean spiral 14 according to fig. 11. The archimedean screw 14 or the da vinci helix is used to transport the reaction medium 6 within the reactor and between reactor components or reactors. Before the inlet 4 and after the outlet 5 a siphon 15 is provided, respectively.

Naturally, the siphon 15 can also be located before the inlet 4 or after the outlet 5 of the reactor independently of the archimedean screw 14. The reaction medium 6 can be introduced into the first reactor unit 2 pressureless or pressureless via a siphon 15.

In the method for continuous photocatalytic and photosynthetic processes and transport in the bio-solar reactor 1, the archimedes screw 14 or the da vinci spiral is preferably used. In particular if the transport of the reaction medium 6 requires overcoming the height difference. One or more non-stress deliveries are achieved using the archimedes screw 14 or the da vinci helix. The device can be used for the following applications:

transport for passing the reaction medium 6 through the same reactor a plurality of times.

-between a series of optionally different one or more passes of the reactor and/or maturation tank.

Alternating single or multiple transfers of reaction medium 6 between tanks and bioreactors of any type.

Single or multiple transfers of reaction medium between tanks.

As briefly mentioned above, before and/or after the bio-solar reactor 1, a maturation tank (not shown) can be provided for in particular a continuous photochemical or photosynthetic process. The hydrostatic maturation tank has a meandering reactor unit 2 of similar design to the hydrostatic bioreactor, which is capable of vertical flow. The maturation tank can be made of a material that is not transparent to light, since the phototrophic microorganisms only need the right temperature, nutrients and the possibility of discharging metabolic waste during the resting phase. Also, that in the reactor unit 2 uses a larger cross section in proportion to the bioreactor to adjust the rest time and save space.

The desired substantially pressureless or pressureless transport of reaction medium 6 is achieved as follows:

throughout the transport process, the reaction medium 6 is not subjected to any other pressure than that generated inside the transport unit due to the own weight of the reaction medium 6. Due to the low rotational speed, the reaction medium 6 is not subjected to any centrifugal forces worth mentioning. The development of the microorganism or the progress of the process is not interrupted or disturbed by the transport. This pressure-free state is ensured by using hydrostatic pressure compensation with "archimedes screw" or da vinci spiral. This process can be performed without stress, acceleration and stress.

Throughout the transport process, the reaction medium 6 does not experience any higher gravitational sensation than that produced inside the transport unit due to the free flow of the reaction medium. The development of the microorganism or the progress of the process is not interrupted or disturbed by the transport. Abrasive damage and damage to the cell wall of the microorganism or molecule, for example by a pump, is precluded. This gravity-free state is ensured by using hydrostatic pressure compensation with "archimedes' spirals" or da vinci spirals.

Preferably in the process, in order to remove gaseous process products, such as oxygen, a removal outlet 16 is provided, which is provided above the surface of the reaction medium or above the upper surface of the reactor unit. For the removal of the gaseous process products, a collecting device 17 with a removal outlet 16 can be provided, which is provided above the liquid level of the reaction medium 6 or above the upper surface of the reactor unit.

According to fig. 12, it is possible to design the bio-solar reactor 1 adjustable to the light incidence. In the case of weak solar irradiation, poor geographical location, or in the case of light being particularly needed by phototrophic microorganisms or photocatalytic processes, the bio-solar reactor 1 is adjusted or controlled in a rotating manner across the entire arch of the horizontal solar trajectory to be adapted to the solar irradiation.

The reactor panels 18, which are preferably connected to each other in series, are arranged within the reactor in such a way that they are almost parallel to each other and are preferably fixedly mounted in frame-like clamping means 25. The bio-solar reactor 1 can be adjusted with respect to the light incidence by means of a rotation device via at least one preferably vertical axis 26, wherein the reactor can be provided (in particular fixed, suspended or floating) on a floating body.

In order to grasp the solar trajectory, sensors can be provided, or data relating to coordinates, time and date can be used, by means of which the rotation of the light incidence for the reactor is controlled.

Formally, it has to be noted that the light incidence for the reactor can also be performed by artificial illumination.

In a system consisting of a plurality of reactors, the rotation can be synchronized for light incidence, preferably for all reactors.

In order to be able to make better use of the light rays, it is also possible to design the reactor panel 18 and/or at least a part of the reactor, in particular the outer surface, to reflect light.

According to fig. 13, the reactor panel 18 formed by the reactor unit 2 is arranged in such a way that the schematically indicated light or solar rays 19 are incident at about right angles to the panel axis.

According to fig. 14, a plurality of reactor panels 18 are provided, preferably connected to each other, and arranged in such a way that the light or solar rays 19 run almost parallel to the axis of the solar panels.

In a special design variant, the reactor panels 18 are arranged suspended and/or fixed standing in upper and/or lower holders or in the clamping devices 25.

The holder or clamping device 25 is able to fulfill the following functions:

-as a rotating unit to follow the solar irradiation.

-raising or lowering the reactor relative to other components of the overall system.

-a tilting function for tilting the reactor towards the sun.

-fixing the reactor panel 18.

For connecting the reactor panels 18 in a zigzag manner.

For enabling a gas-tight sealing of the individual reactor units.

For tilting at least one reactor panel 18 at an angle along the panel axis.

The holder is capable of accommodating at least two to any number of reactor panels 18 as a single reactor.

This enables close positioning and/or adjacent positioning of the reactors, which maximizes the use of space.

The method enables an optimal combination of reactor conditions in light and dormant conditions in the dark and stress-free delivery.

In this way, a continuous single-cycle process or modular controlled multiple passes of a single component can be established.

Before the actual reaction, the reaction medium 6 can be supplied primarily with nutrients and nutrient gases that support the biological reaction starting from the enrichment tank. In the case of wastewater treatment or contaminant removal, the relevant contaminant can be used to produce the maximum initial enrichment in the reaction medium that is appropriate for the phototrophic microorganism.

The reaction medium 6 can be ideally temperature-controlled and the relevant phototrophic microorganisms or chemicals for the reaction can be introduced in specific amounts.

The temperature, process fluid content, process gas content, circulation, thorough mixing, light provision, metabolite discharge can be controlled and regulated in the reaction medium 6 to maintain the desired reaction conditions.

The above method solves the following problems in an advantageous manner:

continuous photocatalytic and photosynthetic process and transport in solar reactors

-controlling and optimizing energy consumption in the process

-controlling and optimizing the introduction of nutrient solutions and solutions facilitating the process

-controlling and optimizing the introduction of nutrient gas and process gas

Control and optimization of the reduction of harmful substances

Optimization of removal and collection of gaseous process products

-controlling and optimizing the provision of light

Minimizing the space used for light guidance

Control and optimization of process temperature

No stress transport of the microorganisms in the reaction medium 6.

-controlling the flow rate.

Claims

1. Method for photochemical processes, wherein a reaction medium is introduced into a reactor in a vertically meandering manner, characterized in that: the meandering conveyance of the reaction medium (6) takes place at least once vertically or obliquely at an angle from top to bottom or in the direction of gravity and from bottom to top or against the direction of gravity, and the introduction and removal of the reaction medium (6) into and from the reactor takes place continuously, without pressure and freely through the upper surface of the reaction medium to the atmosphere, wherein a flow of the reaction medium (6) which is stress-free for the microorganisms is produced as a result of the hydrostatic pressure compensation and levelling compensation,

wherein the reactor is formed by at least one reactor unit (2) formed by two vertical tubes (3) connected at the bottom, and the inlet (4) and the outlet (5) are both provided at the upper edge of the reactor, or

The reactor is formed by at least one reactor unit (2) which is formed by two rectangular, vertical chambers (8) formed by walls or multi-walls (7) and formed by a partition wall (9) which is open at the bottom, and the inlet (4) and the outlet (5) are both provided at the upper edge of the reactor.

2. The method of claim 1, characterized in that: the photochemical process is a photosynthetic process.

3. The method of claim 2, characterized in that: the photosynthetic process is a photocatalytic process.

4. The method of claim 1, characterized in that: the photochemical process is used to propagate and produce microorganisms.

5. The method of claim 1, characterized in that: the photochemical process is used for the propagation and hydroponic cultivation of microorganisms.

6. The method of claim 4 or 5, characterized in that: the microorganism is a phototrophic microorganism.

7. The method of claim 1, characterized in that: the reaction medium is an aqueous solution or suspension.

8. The method of claim 1, characterized in that: in the process, the introduction of liquid and/or gaseous additives (12) is carried out continuously or batchwise in the bottom end of the reactor in the region of the turn-around of the reaction medium (6).

9. The method of claim 8, wherein: the liquid and/or gas additive (12) is a nutrient solution and/or an oxidant and/or an active substance and/or a dissolved substance that facilitates the process.

10. The method of claim 8, wherein: by introducing the additive (12) at the bottom end of the liquid column, the additive (12) is thoroughly mixed and homogeneously distributed in the reaction medium (6).

11. The process according to any one of claims 9 to 10, characterized in that: the liquid and/or gaseous additive (12) is introduced at the bottom end of the reactor in a turning region of the reaction medium (6), wherein a larger amount of liquid and/or gaseous additive (12) is introduced in the region of the reaction medium (6) flowing from bottom to top or against the direction of gravity than in the region of the reaction medium (6) flowing from top to bottom or in the direction of gravity.

12. The method according to any one of claims 1 to 5, characterized in that: in the process, the removal of gaseous process products takes place through the surface of the reaction medium.

13. The method of claim 12, wherein: the gaseous process product is oxygen.

14. The process according to any one of claims 1 to 5, characterized in that: the reactor is adjusted or controlled in a rotational manner across the entire arch of the horizontal solar trajectory to accommodate the solar exposure.

15. Apparatus for carrying out the process according to any one of claims 1 to 14, wherein a reactor is provided which is formed by tubes, characterized in that: the reactor is composed of at least one reactor unit (2) formed by two vertical tubes (3) connected at the bottom, and the inlet (4) and outlet (5) are both provided at the upper edge of the reactor,

the partition walls (10) for connecting two or more reactor units (2) into reactor panels (18) are designed to be lower than the partition walls (9) between the tubes (3) or chambers (8) of the reactor units (2), as a result of which overflow or communication openings are produced when the liquid level in the reactor units (2) is higher than the partition walls (10) between the reactor units (2), the reactor panels (18) connected in series to one another are arranged into the reactor parallel to one another and by being fixedly mounted in frame-like clamping means (25), the reactor can be adjusted with respect to the incidence of light by means of a rotating device by means of at least one vertical axis (26), wherein the reactor is provided on a floating body,

for the continuous or batchwise introduction of the additive (12), in the course of which at least one introduction inlet (11) is provided in the bottom of the reactor in the region of the diversion of the reaction medium,

in the process, for the removal of gaseous process products, a removal outlet (16) is provided, which is provided above the surface of the reaction medium or above the upper surface of the reactor unit (2).

16. The apparatus of claim 15, characterized in that the reactor is a bioreactor.

17. The apparatus as claimed in any of claims 15 to 16, characterized in that "providing the reactor on a float" means fixing, suspending or floating the reactor on a float.

18. The device according to claim 15, characterized in that the additive (12) is a nutrient solution or a nutrient gas and/or an oxidizing agent and/or an active substance and/or a dissolved substance that promotes the process.

19. The apparatus of claim 18, wherein the dissolved substance that promotes the process is a dissolved gas that promotes the process.

20. The apparatus of claim 15, characterized in that the gaseous process product is oxygen.

21. Apparatus for carrying out the method according to any one of claims 1 to 14, whereby a reactor with elements made of wall plates or multi-wall plates is provided, characterized in that the reactor is composed of at least one reactor unit (2) which is formed by two rectangular vertical chambers (8) formed by wall plates or multi-wall plates (7) which are formed by partition walls (9) which are open at the bottom, and that the inlet (4) and the outlet (5) are both provided at the upper edge of the reactor,

22. The apparatus of claim 21, characterized in that the reactor is a bioreactor.

23. The apparatus as claimed in any of claims 21 to 22, characterized in that "providing the reactor on a float" means fixing, suspending or floating the reactor on a float.

24. The device according to claim 21, characterized in that the additive (12) is a nutrient solution or a nutrient gas and/or an oxidizing agent and/or an active substance and/or a dissolved substance that promotes the process.

25. The apparatus of claim 24, wherein the dissolved substance that promotes the process is a dissolved gas that promotes the process.

26. The apparatus of claim 21, wherein said gaseous process product is oxygen.

27. The apparatus of claim 15 or 21, wherein: a sensor is provided to grasp the sun trajectory, by which the rotation for the reactor for light incidence is controlled.

28. The apparatus of claim 15 or 21, wherein: the light injection into the reactor is carried out by artificial illumination.

29. The apparatus of claim 15 or 21, wherein: the rotation against the incidence of light is synchronized in a system consisting of a plurality of reactors.

30. The apparatus of claim 29, wherein: the rotation against the incidence of light in a system consisting of a plurality of reactors is synchronized for all reactors.

31. The apparatus of claim 15 or 21, wherein: the reactor panel (18) and/or at least a part of the reactor is designed to reflect light.

32. The apparatus of claim 31, wherein: the reactor panel (18) and/or the outer surface of the reactor are designed to reflect light.

33. The apparatus of claim 15 or 21, wherein: for introducing additives into the reactor unit (2) and/or the turning areas of the reactor panels (18), a bore (20) for the pipe-making apparatus is provided.

34. The apparatus of claim 33, wherein: for introducing additives into the reactor unit (2) and/or the turning area of the reactor panel (18), a bore (20) for the continuous pipe apparatus is provided.

35. The apparatus of claim 33, wherein: the tube is a gas tube (21) with a micro-drilled hole (22).

36. The apparatus of claim 35, wherein: in the region of the reaction medium (6) flowing from bottom to top or against the direction of gravity, the gas tube (21) has a greater number of micro-drilled holes and/or micro-drilled holes with a greater diameter than in the region of the reaction medium (6) flowing from top to bottom or in the direction of gravity.

37. The apparatus of claim 35, wherein: the gas pipe (21) has external and/or internal threads (23) at both ends.

38. The apparatus of claim 15 or 21, wherein: for removing gaseous process products, a collecting device (17) with a reactor unit removal outlet (16) is provided, which is provided above the surface of the reaction medium or above the upper surface of the reactor unit.

39. The apparatus of claim 15 or 21, wherein: a siphon (15) is provided before the inlet (4) and/or after the outlet (5).

40. The apparatus of claim 15 or 21, wherein: inside the reactors and between the reactors, archimedes' screws (14) are provided to convey the reaction medium (6).