Reactor for synthesizing single-cell protein and system device comprising reactor

Abstract

The utility model discloses a reactor for synthesizing single-cell protein and a system device comprising the reactor. The reactor comprises a shell, a gas-liquid mixing area, a first incremental reaction area, a second incremental reaction area, an aeration disc, a spraying opening, a bacterial liquid feeding opening, a material backflow opening, a material liquid discharging opening, a household garbage pyrolysis gas inlet, an exhaust opening and a connecting opening, according to the reactor, household garbage pyrolysis gas is introduced into the device for synthesis of single-cell protein by adopting a microbial process, and the device is efficient and economical, does not need to add a catalyst, does not need high temperature and high pressure, and can efficiently convert H2 and CO2 to synthesize the single-cell protein; the problems of low utilization efficiency of H2 and CO2, concentration gradient in the reactor and the like in the field of preparation of single-cell protein from pyrolysis gas at present are solved.

Description

Technical Field

[0001] The utility model belongs to the technical field of synthesizing single-cell protein, and more specifically relates to a reactor for efficiently converting pyrolysis gas of domestic waste into single-cell protein, and a system device including the reactor. Background Art

[0002] Pyrolysis gas from municipal solid waste is generated under oxygen-free or anoxic conditions, when the macromolecules of organic components in municipal solid waste break down, producing small gases such as H2, CO2, CO, and CH4. H2 and CO2 account for a relatively high proportion of these gases. These gases have low calorific value and are significantly affected by waste composition and pyrolysis conditions, resulting in limited practical application and low utilization efficiency. Using specialized bacterial strains to convert H2 and CO2 from municipal solid waste pyrolysis gas into single-cell proteins not only allows for direct use of the gas, reducing energy conversion and production costs, but also allows for the comprehensive utilization of the gas through microbial microbial utilization, thereby enhancing its efficiency.

[0003] Single-cell protein (SCP), also known as microbial protein or bacterial protein, is produced by culturing single-cell organisms using industrial wastewater, exhaust gas, natural gas, petroleum alkanes, agricultural and sideline products, and organic waste as culture media. After purification and drying, SCP is an important protein source for the food and feed industries. Compared to other protein sources, SCP offers advantages such as high production rates, rich nutrition, and minimal or no land use.

[0004] Therefore, it is necessary to provide an innovative system device to efficiently convert domestic waste pyrolysis gas into single-cell protein. Utility Model Content

[0005] The first technical problem addressed by this utility model is to provide a reactor for efficiently converting pyrolysis gas from household waste into single-cell protein. This device uses a microbial process to pass pyrolysis gas from household waste into the device for single-cell protein synthesis. This device is efficient and economical, requiring no catalyst, high temperature, or high pressure. It efficiently converts H2 and CO2 into single-cell protein, resolving issues currently encountered in the field of single-cell protein production from pyrolysis gas, such as low H2 and CO2 utilization efficiency and concentration gradients within the reactor.

[0006] The second technical problem to be solved by the present invention is to provide a system device including the above reactor.

[0007] In order to solve the above-mentioned first technical problem, the present invention adopts the following technical solution:

[0008] A reactor for efficiently converting domestic waste pyrolysis gas into single-cell protein, the reactor comprising a shell, a gas-liquid mixing zone, a first incremental reaction zone, a second incremental reaction zone, an aeration plate, a spray port, a bacterial liquid feed port, a material reflux port, a material discharge port, a domestic waste pyrolysis gas inlet port, an exhaust port, and a connection port;

[0009] The gas-liquid mixing zone, the first incremental reaction zone, the second incremental reaction zone, the aeration plate and the spray port are arranged inside the shell;

[0010] The bacterial liquid feed port, material reflux port, material discharge port, domestic waste pyrolysis gas inlet port, exhaust port and connection port are arranged on the shell;

[0011] The gas-liquid mixing zone is arranged at the bottom of the shell;

[0012] A first incremental reaction zone and a second incremental reaction zone are sequentially arranged in the middle of the shell above the gas-liquid mixing zone from top to bottom, and a feed sieve plate is provided above the first incremental reaction zone;

[0013] An aeration plate is provided below the gas-liquid mixing zone, and the aeration plate is connected to the domestic waste pyrolysis gas inlet provided on the shell;

[0014] The exhaust port is arranged at the top of the shell;

[0015] A spray port is provided above the feed sieve plate, and the spray port is connected to the bacterial liquid feed port and the material return port through a pipeline; the bacterial liquid is sprayed through the spray port and then passes through the feed sieve plate and is evenly distributed in the first incremental reaction zone and the second incremental reaction zone;

[0016] The material discharge port is divided into two branches through a pipeline, one branch is connected to the drain valve, and the other branch is connected to the material reflux port on the upper part of the shell after passing through a diaphragm pump.

[0017] As an embodiment, the first incremental reaction zone includes a first MBBR packed fluidized bed and a first sieve plate arranged on the upper and lower end surfaces of the first MBBR packed fluidized bed; the second incremental reaction zone includes a second MBBR packed fluidized bed and a second sieve plate arranged on the upper and lower end surfaces of the second MBBR packed fluidized bed.

[0018] As an embodiment, the diameter of the first MBBR packed fluidized bed is 10-25 mm; the diameter of the second MBBR packed fluidized bed is 10-25 mm.

[0019] As an embodiment, the height of the first MBBR packed fluidized bed is 0.5-0.9 m; the height of the second MBBR packed fluidized bed is 0.5-0.9 m.

[0020] As an embodiment, the aeration plate is provided with aeration holes, and the ratio of the diameter of the aeration plate to the inner diameter of the synthesis reactor is 0.91-0.92; except for the part fixed to the inner wall of the reactor on the circumference of the aeration plate, the remaining gaps enable the gas-liquid mixing and connection between the upper and lower sections of the aeration plate; the diameter of the aeration holes is 200-300 mm, and the total aeration area of ​​the aeration holes on the aeration plate accounts for 50%-80%.

[0021] As an embodiment, the aeration holes are circular or equilaterally triangular and are evenly distributed on the aeration plate.

[0022] As an embodiment, the reactor has a height of 2.0-2.5 m and a diameter of 1.0-1.5 m.

[0023] In order to solve the second technical problem mentioned above, the present invention adopts the following technical solution:

[0024] A system device comprising the above-mentioned reactor for synthesizing single-cell protein comprises at least two reactors for synthesizing single-cell protein connected in series or in parallel.

[0025] Any range described in the present invention includes the end values ​​and any numerical values ​​between the end values ​​and any sub-range formed by the end values ​​or any numerical values ​​between the end values.

[0026] Unless otherwise specified, all raw materials in the present invention can be purchased commercially, and the equipment used in the present invention can adopt conventional equipment in the relevant field or refer to the existing technology in the relevant field.

[0027] Compared with the prior art, the present invention has the following beneficial effects:

[0028] 1. The reactor of this utility model is equipped with two incremental reaction zones, which increases the contact area with microorganisms and improves the conversion rate of domestic waste pyrolysis gas;

[0029] 2. The reactor of the present invention is equipped with a diaphragm pump, which can realize the self-reflux of the bacterial liquid in the reactor and eliminate the concentration gradient in the reactor. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] The specific embodiments of the present invention will be further described in detail below with reference to the accompanying drawings.

[0031] Figure 1 It is a structural schematic diagram of the reactor of the present utility model;

[0032] Figure 2 This is a schematic structural diagram of the system device when the reactors of the present invention are connected in series;

[0033] Figure 3This is a schematic structural diagram of the system device when the reactors of the present invention are connected in parallel. DETAILED DESCRIPTION

[0034] In order to more clearly illustrate the present invention, the present invention is further described below in conjunction with preferred embodiments. Those skilled in the art should understand that the following specific description is illustrative rather than restrictive and should not limit the scope of protection of the present invention.

[0035] See also Figure 1 As shown, as one aspect of the present invention, the present invention provides a reactor 100 for efficiently converting domestic waste pyrolysis gas into single-cell protein. The reactor 100 includes a shell 10, a gas-liquid mixing zone 20, a first incremental reaction zone 40, a second incremental reaction zone 30, an aeration plate 50, a spray port 60, a bacterial liquid feed port 91, a material reflux port 92, a material discharge port 93, a domestic waste pyrolysis gas inlet port 94, an exhaust port 95, and a connection port 96.

[0036] The gas-liquid mixing zone 20, the first incremental reaction zone 40, the second incremental reaction zone 30, the aeration plate 50 and the spray port 60 are arranged inside the shell 10;

[0037] The bacterial liquid feed port 91, the material return port 92, the material discharge port 93, the domestic waste pyrolysis gas inlet 94, the exhaust port 95 and the connection port 96 are arranged on the housing 10;

[0038] The gas-liquid mixing zone 20 is arranged at the bottom of the shell 10;

[0039] A first incremental reaction zone 40 and a second incremental reaction zone 30 are sequentially arranged in the middle of the shell above the gas-liquid mixing zone 10 from top to bottom, and a feed sieve plate 70 is further arranged above the first incremental reaction zone 40;

[0040] An aeration plate 50 is provided below the gas-liquid mixing zone 20 , and the aeration plate 50 is connected to the domestic waste pyrolysis gas inlet 94 provided on the housing 10 ;

[0041] The exhaust port 95 is provided at the top of the housing 10;

[0042] A spray port 60 is provided above the feed sieve plate 70 and is connected to the bacterial liquid feed port 91 and the material return port 92 via a pipe. The bacterial liquid is sprayed through the spray port 60 and then passes through the feed sieve plate 70 and is evenly distributed in the first incremental reaction zone 40 and the second incremental reaction zone 30.

[0043] The material discharge port 93 is divided into two branches through a pipeline, one branch is connected to the drain valve 200, and the other branch is connected to the material reflux port 92 on the upper part of the shell after passing through the diaphragm pump 300.

[0044] As an embodiment, the first incremental reaction zone 40 includes a first MBBR packed fluidized bed 401 and a first sieve plate 402 arranged on the upper and lower end surfaces of the first MBBR packed fluidized bed 401; the second incremental reaction zone 30 includes a second MBBR packed fluidized bed 301 and a second sieve plate 302 arranged on the upper and lower end surfaces of the second MBBR packed fluidized bed 301.

[0045] As an embodiment, the diameter of the first MBBR packed fluidized bed 401 is 10-25 mm; the diameter of the second MBBR packed fluidized bed 301 is 10-25 mm.

[0046] As an embodiment, the height of the first MBBR packed fluidized bed 401 is 0.5-0.9 m; the height of the second MBBR packed fluidized bed 301 is 0.5-0.9 m.

[0047] As an embodiment, the aeration plate 50 is provided with aeration holes (not shown in the figure), and the ratio of the diameter of the aeration plate 50 to the inner diameter of the synthesis reactor is 0.91-0.92; except for the part fixed to the inner wall of the reactor 100 on the circumference of the aeration plate 50, the remaining gaps allow the gas-liquid mixing in the upper and lower sections of the aeration plate 50 to be connected; the diameter of the aeration holes is 200-300 mm, and the total aeration area of ​​the aeration holes on the aeration plate 50 accounts for 50%-80%.

[0048] As an embodiment, the aeration holes are circular or equilaterally triangular and are evenly distributed on the aeration plate.

[0049] As an embodiment, the reactor 100 has a height of 2.0-2.5 m and a diameter of 1.0-1.5 m.

[0050] As another aspect of the present invention, the present invention provides a system device including the above-mentioned reactor for synthesizing single-cell protein, comprising at least two reactors 100 for synthesizing single-cell protein connected in series or in parallel.

[0051] See also Figure 2 As shown, when two or more reactors 100 for synthesizing single-cell protein are connected in series, the connection port of the first-stage reactor is connected to the feed port of the second-stage reactor through a pipeline; the connection port of the last-stage reactor is connected to the reflux port of the first stage through a pipeline.

[0052] See also Figure 3 As shown, when two or more reactors 100 for synthesizing single-cell protein are connected in parallel, the bacterial liquid enters the two-stage reactors at the same time, the bacterial liquid refluxes in each reactor, and the pyrolysis gas reacts simultaneously in the two reactors. After the reaction is completed, it is discharged from the respective liquid discharge ports and exhaust ports. This is suitable for situations where the gas volume is large.

[0053] The working principle of the utility model is as follows :

[0054] The function of the gas-liquid mixing zone in the reactor is to introduce the pyrolysis gas of domestic waste into the gas-liquid mixing zone to achieve gas-liquid mixing and to connect to the next reactor through the connecting port; wherein the gas flow rate introduced into the gas-liquid mixing zone is controlled at 0.9-1.2m 3 / h, so that the gas can be fully captured and utilized by microorganisms; the gas is decomposed into tiny bubbles through the aeration disk 50 and rises to the incremental reaction zone for reaction;

[0055] The cross section of the aeration holes in the aeration plate in the gas-liquid mixing zone is circular, equilateral triangle or parallelogram; the ratio of the aeration plate diameter to the reactor inner diameter is 0.91-0.92; the aeration hole diameter is 200-300mm, and the gas volume of a single aeration hole is 0-0.3m 3 / h, the total aeration area of ​​the aeration holes on the aeration plate accounts for 50%-80%;

[0056] The function of the incremental reaction zone in the reactor is to add microbial liquid to the upper part of the zone to react with the rising gas to improve the conversion efficiency of H2 and CO2, and discharge the residual gas at the top of the reactor. MBBR filler fluidized bed is used in the incremental reaction zone to use the microorganisms in the reactor to carry out biological conversion of H2, CO2, NH3 and O2. The reaction is 21.36H2+6.21O2+4.09CO2+0.76NH3→C 4.09 H 7.13 O 1.89 N 0.76 +18.70H2O, generates C 4.09 H 7.13 O 1.89 N 0.76 Single cell protein as the main component;

[0057] Compared with existing single-cell protein synthesis reactors, the reactor described in the present invention has two incremental reaction zones set up in the shell. MBBR fillers are used in the incremental reaction zones to provide an environment suitable for the growth of microorganisms. The incremental reaction zones use a fluidized bed to increase the contact area between gas and microorganisms. The movement of fluid and particles makes the bed have good heat transfer performance, and the temperature inside the bed is uniform and easy to control. A diaphragm pump is connected to the bottom of the reactor to achieve self-reflux of the bacterial liquid in the reactor, eliminate the concentration gradient in the reactor, enhance the mixing uniformity of the bacterial liquid and gas, and improve the reaction efficiency.

[0058] Furthermore, a single synthesis reactor of the present invention can be connected to the gas-liquid mixing zone of other synthesis reactors through the connection port at the upper part of the gas-liquid mixing zone to form a series reactor system device, and reflux to the upper part of the first reactor at the lower side interface of the last-stage reactor to continue the reaction, thereby improving the conversion rate of H2 and CO2 in the thermal decomposition gas of domestic waste.

[0059] Furthermore, a single synthesis reactor of the present invention can also be combined with other synthesis reactors to form a parallel reactor, and reactions can be carried out separately to increase protein production.

[0060] The advantages of the utility model are that the reactors can be connected in series or in parallel, and can be flexibly changed; not only can the reactors be connected in series to form a reactor system to improve the conversion rate of H2 and CO2 in the pyrolysis gas of domestic waste, but they can also be connected in parallel to form a reactor system to increase protein production; using the system device of the utility model, the pyrolysis gas of domestic waste can be directly introduced into the reactor, and the H2 and CO2 therein can be converted into single-cell protein under the action of microorganisms.

[0061] Obviously, the above embodiments of the present invention are merely examples for the purpose of clearly illustrating the present invention and are not intended to limit the embodiments of the present invention. Those skilled in the art will readily appreciate that other variations or modifications based on the above description are possible. This list of all possible embodiments is not exhaustive. Any obvious variations or modifications arising from the technical solution of the present invention remain within the scope of protection of the present invention.

Claims

1. A reactor for synthesizing single cell protein, characterized in that: The reactor comprises a shell, a gas-liquid mixing zone, a first incremental reaction zone, a second incremental reaction zone, an aeration plate, a spray port, a bacterial liquid feed port, a material reflux port, a material discharge port, a domestic waste pyrolysis gas inlet port, an exhaust port and a connection port; The gas-liquid mixing zone, the first incremental reaction zone, the second incremental reaction zone, the aeration plate and the spray port are arranged inside the shell; The bacterial liquid feed port, material reflux port, material discharge port, domestic waste pyrolysis gas inlet port, exhaust port and connection port are arranged on the shell; The gas-liquid mixing zone is arranged at the bottom of the shell; A first incremental reaction zone and a second incremental reaction zone are sequentially arranged from top to bottom in the middle of the shell above the gas-liquid mixing zone, and a feed sieve plate is arranged above the first incremental reaction zone; An aeration plate is arranged below the gas-liquid mixing zone, and the aeration plate is connected to an air inlet for pyrolysis gas of domestic waste arranged on the shell; The exhaust port is arranged at the top of the shell; A spray port is arranged above the feed sieve plate, and the spray port is connected to the bacterial liquid feed port and the material return port through a pipeline; the bacterial liquid is sprayed through the spray port and then evenly distributed in the first incremental reaction zone and the second incremental reaction zone through the feed sieve plate; The material discharge port is divided into two branches through a pipeline, one branch is connected to the drain valve, and the other branch is connected to the material reflux port on the upper part of the shell after passing through a diaphragm pump.

2. The reactor for synthesizing single cell protein according to claim 1, characterized in that: The first incremental reaction zone includes a first MBBR packed fluidized bed and a first sieve plate arranged on the upper and lower end surfaces of the first MBBR packed fluidized bed.

3. The reactor for synthesizing single cell protein according to claim 2, characterized in that: The diameter of the first MBBR filler fluidized bed is 10-25 mm.

4. The reactor for synthesizing single cell protein according to claim 2, characterized in that: The height of the first MBBR filler fluidized bed is 0.5-0.9 m.

5. The reactor for synthesizing single cell protein according to claim 1, characterized in that: The second incremental reaction zone includes a second MBBR packed fluidized bed and a second sieve plate arranged on the upper and lower end surfaces of the second MBBR packed fluidized bed.

6. The reactor for synthesizing single cell protein according to claim 5, characterized in that: The diameter of the second MBBR filler fluidized bed is 10-25 mm.

7. The reactor for synthesizing single cell protein according to claim 5, characterized in that: The height of the second MBBR filler fluidized bed is 0.5-0.9 m.

8. The reactor for synthesizing single cell protein according to claim 1, characterized in that: The aeration plate is provided with aeration holes, and the ratio of the diameter of the aeration plate to the inner diameter of the synthesis reactor is 0.91-0.92; except for the fixed part on the circumference of the aeration plate to the inner wall of the reactor, the remaining gaps enable the gas-liquid mixing and connection between the upper and lower sections of the aeration plate; the diameter of the aeration holes is 200-300mm, and the total aeration area of ​​the aeration holes on the aeration plate accounts for 50%-80%; the aeration holes are circular or equilateral triangles, and are evenly distributed on the aeration plate.

9. The reactor for synthesizing single cell protein according to claim 1, characterized in that: The reactor has a height of 2.0-2.5 m and a diameter of 1.0-1.5 m.

10. A system device comprising a reactor for synthesizing a single cell protein according to any one of claims 1 to 9, characterized in that: The invention comprises at least two reactors for synthesizing single cell protein which are connected in series or in parallel.

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