CN110295073B - Biogas purification membrane bioreactor and use method thereof - Google Patents

Biogas purification membrane bioreactor and use method thereof Download PDF

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CN110295073B
CN110295073B CN201910614931.3A CN201910614931A CN110295073B CN 110295073 B CN110295073 B CN 110295073B CN 201910614931 A CN201910614931 A CN 201910614931A CN 110295073 B CN110295073 B CN 110295073B
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concentration
liquid
water inlet
gas
biogas
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CN110295073A (en
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赵磊
王子寒
任南琪
陈川
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Harbin Institute of Technology
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Harbin Institute of Technology
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/84—Biological processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/104—Carbon dioxide
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Abstract

A biogas purification membrane bioreactor and a use method thereof relate to a biogas purification reactor and a use method thereof. The invention aims to solve the problems of high energy and equipment investment requirements and environmental pollution in the existing biogas purification process. The biogas purification membrane bioreactor comprises a water inlet device, a hydrogen gas supply device, a biogas supply device, a reactor, a circulating device and a gas outlet liquid sealing device. The using method comprises the following steps: firstly, a starting stage: injecting a biogas purification biological culture medium into the reactor main body until the liquid level of the biogas purification biological culture medium reaches the position of the water outlet of the reflux device, introducing nitrogen, sealing, and inoculating biogas purification seed liquid; opening a hydrogen pressure reducing valve, a methane pressure reducing valve and a circulating pump to purify methane; II, a continuous operation stage: and (4) closing the hydrogen pressure reducing valve, the methane pressure reducing valve and the circulating pump for 1 time and starting the water inlet pump for 1 time every 12 hours of operation. The advantages are that: the purity of the biogas reaches over 93 percent, and the yield of the ethanol reaches 1.5 g/L.d.

Description

Biogas purification membrane bioreactor and use method thereof
Technical Field
The invention relates to a biogas purification reactor and a using method thereof.
Background
With the increasing population and the increasing development of industrialization in the world, the demand for energy is continuously expanded, so that the global fossil fuel reserves are reduced, and meanwhile, the fossil fuel is combusted to release a large amount of greenhouse gases to face the dual crisis of energy and environment. Promoting the revolution of energy production structure and utilization mode, and promoting the multi-element clean development of energy is the urgent priority for realizing sustainable development in China. The biogas is used as a clean gas energy source, and has the characteristics of environmental protection, availability of byproducts, low cost, mature technology, easy popularization and the like, thereby having great application prospect in the aspect of supplementing the energy shortage of China.
Biogas refers to fuel gas which is converted from biomass and takes methane as a main component, and mainly refers to biogenic methane obtained by purifying biogas at present. The methane is a mixture of various gases generated by organic substances through microbial fermentation under anaerobic conditions, and mainly contains methane and carbon dioxide, wherein the methane accounts for 55-70% and the carbon dioxide accounts for 30-45%. China's republic of ChinaThe biogas resource is very abundant, but the utilization mode is more traditional, except a few enterprises obtaining power generation internet subsidies, the biogas resource mainly is used by burning boilers and generating power. In recent years, more high-yield biogas projects are provided, and the daily biogas yield reaches 10000Nm3～150000Nm3And the gas quantity is far greater than the gas quantity required by enterprises, and the redundant biogas is often introduced into a boiler and is not completely combusted or even directly discharged, so that the environmental pollution and the resource waste are caused. Under the current severe trend of energy conservation and emission reduction, the biogas purification and the biogas utilization can effectively reduce the greenhouse effect caused by emptying due to insufficient biogas utilization in biogas engineering while the biogas is used at a high value, and has the double benefits of environmental protection and energy.
The traditional method for purifying the biogas by an adsorption method, an absorption method, a membrane separation method and a low-temperature separation method needs expensive instruments or equipment and has higher energy requirement, and a large amount of carbon dioxide is accompanied by 2 to 10 percent of CH in the purification process4Is discharged into the atmosphere, increases the emission of greenhouse gases and causes secondary pollution to the environment. In order to meet the industrial production requirement of biogas purification, an efficient and clean biogas purification method is imperative to be developed.
Disclosure of Invention
The invention aims to solve the problems of high energy and equipment investment requirements and environmental pollution in the existing biogas purification process, and provides a biogas purification membrane bioreactor and a use method thereof.
The biogas purification membrane bioreactor comprises a water inlet device, a hydrogen gas supply device, a biogas supply device, a reactor, a circulating device and a gas outlet liquid sealing device;
the reactor comprises a reactor main body and a hollow fiber membrane assembly, wherein the hollow fiber membrane assembly consists of a hollow fiber membrane tow, a membrane assembly end enclosure and a membrane assembly fixing piece, the membrane assembly end enclosure is arranged at two ends of the hollow fiber membrane tow, the hollow fiber membrane tow is fixed in the reactor main body through the membrane assembly end enclosure by using the membrane assembly fixing piece, a reactor water inlet is arranged at the lower part of the reactor main body, and a reactor water outlet is arranged at the upper part of the reactor main body;
the water inlet device consists of a water inlet pump, a water inlet tank and a water inlet air bag, the water inlet tank is communicated with a reactor water inlet of the reactor through a water inlet pipeline, the water inlet pump is arranged on the water inlet pipeline, and one end of the water inlet pipeline extends to be below the liquid level in the water inlet tank; the water inlet tank is communicated with the water inlet air bag through an air supply pipeline, and one end of the air supply pipeline extends to be above the liquid level in the water inlet tank;
the hydrogen gas supply device comprises a hydrogen gas high-pressure cylinder, a hydrogen pressure reducing valve and a gas pressure meter, the hydrogen gas high-pressure cylinder is communicated with the hollow fiber membrane tow through a gas pipeline, and the hydrogen pressure reducing valve and the gas pressure meter are arranged on the gas pipeline;
the circulating device comprises a circulating pump, a backflow device, a circulating water outlet, a backflow device air inlet, a backflow device water outlet, a circulating water inlet and a pH electrode; the circulating water outlet and the air inlet of the reflux device are arranged at the lower part of the reflux device, the water outlet of the reflux device is arranged at the middle part of the reflux device, the circulating water inlet is arranged at the upper part of the reflux device, the pH electrode is arranged at the top of the reflux device, one end of the pH electrode extends to the position below the liquid level in the reflux device, the circulating water inlet is communicated with the water outlet of the reactor by a pipeline, the circulating water outlet is communicated with the water inlet of the reactor by a pipeline, and a circulating pump is arranged on the pipeline for communicating the circulating water outlet with the water inlet;
the gas outlet liquid sealing device comprises a gas outlet liquid sealing bottle and a gas collecting bag, and the gas outlet liquid sealing bottle is communicated with the reflux device through a water outlet of the reflux device by using a pipeline; the gas-liquid outlet sealed bottle is communicated with the gas collecting bag through a gas pipe, one end of the gas pipe extends to be above the liquid level in the gas-liquid outlet sealed bottle, and a liquid outlet is formed in the lower part of the gas-liquid outlet sealed bottle;
the methane gas supply device comprises a methane high-pressure gas cylinder, a methane pressure reducing valve and a gas flowmeter, the methane high-pressure gas cylinder is communicated with the reflux device through a gas inlet of the reflux device by utilizing a gas pipeline, and the methane pressure reducing valve and the gas flowmeter are arranged on the gas pipeline.
The use method of the biogas purification membrane bioreactor is specifically completed according to the following steps:
firstly, a starting stage: opening a water inlet pump, injecting a biogas purification liquid fermentation culture medium filled in a water inlet tank into a reactor main body through a reactor water inlet, after the reactor main body is filled with the biogas purification liquid fermentation culture medium, flowing into a backflow device through a reactor water outlet and a circulating water inlet, closing the water inlet pump when the liquid level of the biogas purification liquid fermentation culture medium in the backflow device reaches the position of the backflow device water outlet, introducing nitrogen with the purity of 99.99% into the reactor main body, sealing the reactor main body, then inoculating a biogas purification seed liquid into the reactor main body, wherein the volume ratio of the biogas purification seed liquid to the biogas purification liquid fermentation culture medium is 1:10, the strain in the biogas purification seed liquid is Clostridium sp 11(Clostridium ragsdalei P11), and the concentration of Clostridium P11 in the biogas purification seed liquid is 1.8 g/L; opening a hydrogen pressure reducing valve, a methane pressure reducing valve and a circulating pump, purifying methane under the conditions that the circulating speed is 65mL/min, the hydrogen pressure is 1.25atm and the methane flow is 10mL/min, discharging residual liquid into a gas-liquid sealed bottle after purification, and collecting the purified methane in a gas collecting bag;
II, a continuous operation stage: and (3) closing the hydrogen pressure reducing valve, the methane pressure reducing valve and the circulating pump for 1 time and opening the water inlet pump for 1 time every 12 hours of operation of the methane purification membrane bioreactor, and injecting a methane purification liquid fermentation culture medium into the reactor main body, wherein the addition amount of the methane purification liquid fermentation culture medium is one half of that of the methane purification liquid fermentation culture medium in the step one.
The principle and the advantages of the invention are as follows:
firstly, pumping a biogas purification liquid fermentation culture medium in a water inlet device into a reactor main body through a water inlet of the reactor arranged at the lower part of the reactor main body by a water inlet pump; the biogas purification bacteria in the reaction zone of the reactor main body are uniformly mixed under the action of the circulating pump, and the hydrogen dissolved into the liquid by the hollow fiber membrane component through the osmosis is fully utilized to be in full contact reaction with the biogas introduced into the circulating device in a liquid phase; after the reaction is completed, a water inlet device pumps fresh biogas purification liquid fermentation culture medium into the reactor main body through a water inlet pump, fermentation residual liquid enters a gas-liquid outlet sealed bottle from a water outlet of a reflux device of a circulating device, wherein the concentration of hydrogen is realized by controlling a hydrogen pressure reducing valve and a gas pressure meter, and the concentration of biogas in liquid is controlled by the biogas pressure reducing valve and a gas flow meter.
Secondly, the invention adopts a biological method to realize the purification of the methane, thereby effectively avoiding the expensive equipment investment and energy consumption.
The membrane bioreactor for purifying the biogas has the advantages of simple structure, simple working process and convenient operation, can adjust the partial pressure of hydrogen according to the purification condition of the biogas, can avoid strain loss to the maximum extent while improving the gas utilization rate, and realizes efficient biogas purification.
The invention can maximize the utilization rate of the biogas, the carbon dioxide in the biogas generates ethanol by taking hydrogen as an electron donor through the action of microorganisms, and meanwhile, the biogas is purified, so that the added value of products is greatly improved.
Fifthly, the biogas purification membrane bioreactor is adopted to obtain the biogas with the purity of more than 93 percent, and the ethanol yield reaches 1.5 g/L.d.
Drawings
Fig. 1 is a schematic structural diagram of a biogas purification membrane bioreactor of the present invention, in which 1 represents a hydrogen high-pressure gas cylinder, 2 represents a hydrogen pressure reducing valve, 3 represents a reactor main body, 4 represents a hollow fiber membrane bundle, 5 represents a membrane module end enclosure, 6 represents a reactor water outlet, 7 represents a membrane module fixing member, 8 represents a reactor water inlet, 9 represents a water inlet pump, 10 represents a water inlet tank, 11 represents a water inlet air bag, 12 represents a circulating pump, 13 represents a backflow device, 14 represents a circulation water outlet, 15 represents a backflow device air inlet, 16 represents a backflow device water outlet, 17 represents a circulation water inlet, 18 represents a pH electrode, 19 represents a gas collection bag, 20 represents a gas-liquid sealed cylinder, 21 represents a gas flow meter, 22 represents a biogas pressure reducing valve, 23 represents a biogas high-pressure gas cylinder, 24 represents a magnetic stirrer, and 25 represents a.
Detailed Description
The first embodiment is as follows: the embodiment is a biogas purification membrane bioreactor, which comprises a water inlet device, a hydrogen gas supply device, a biogas supply device, a reactor, a circulating device and a gas outlet liquid sealing device;
the reactor comprises a reactor main body 3 and a hollow fiber membrane component, wherein the hollow fiber membrane component consists of a hollow fiber membrane tow 4, a membrane component seal head 5 and a membrane component fixing part 7, the membrane component seal heads 5 are arranged at two ends of the hollow fiber membrane tow 4, the hollow fiber membrane tow 4 is fixed in the reactor main body 3 through the membrane component seal heads 5 by utilizing the membrane component fixing part 7, a reactor water inlet 8 is arranged at the lower part of the reactor main body 3, and a reactor water outlet 6 is arranged at the upper part of the reactor main body 3;
the water inlet device consists of a water inlet pump 9, a water inlet tank 10 and a water inlet air bag 11, the water inlet tank 10 is communicated with a reactor water inlet 8 of the reactor through a water inlet pipeline, the water inlet pump 9 is arranged on the water inlet pipeline, and one end of the water inlet pipeline extends to a position below the liquid level in the water inlet tank 10; the water inlet tank 10 is communicated with the water inlet air bag 11 through an air supply pipeline, and one end of the air supply pipeline extends to be above the liquid level in the water inlet tank 10;
the hydrogen gas supply device comprises a hydrogen gas high-pressure gas cylinder 1, a hydrogen pressure reducing valve 2 and a gas pressure meter 25, wherein the hydrogen gas high-pressure gas cylinder 1 is communicated with the hollow fiber membrane tows 4 through a gas pipeline, and the hydrogen pressure reducing valve 2 and the gas pressure meter 25 are arranged on the gas pipeline;
the circulating device comprises a circulating pump 12, a reflux device 13, a circulating water outlet 14, a reflux device air inlet 15, a reflux device water outlet 16, a circulating water inlet 17 and a pH electrode 18; a circulating water outlet 14 and a reflux device air inlet 15 are arranged at the lower part of the reflux device 13, a reflux device water outlet 16 is arranged at the middle part of the reflux device 13, a circulating water inlet 17 is arranged at the upper part of the reflux device 13, a pH electrode 18 is arranged at the top part of the reflux device 13, one end of the pH electrode 18 extends to the position below the liquid level in the reflux device 13, the circulating water inlet 17 is communicated with the reactor water outlet 6 by a pipeline, the circulating water outlet 14 is communicated with the reactor water inlet 8 by a pipeline, and a circulating pump 12 is arranged on the pipeline for communicating the circulating water outlet 14 with the reactor water inlet 8;
the gas outlet liquid sealing device comprises a gas outlet liquid sealing bottle 20 and a gas collecting bag 19, and the gas outlet liquid sealing bottle 20 is communicated with the reflux device 13 through a water outlet 16 of the reflux device by a pipeline; the gas outlet and liquid sealing bottle 20 is communicated with the gas collecting bag 19 through a gas pipe, one end of the gas pipe extends to be above the liquid level in the gas outlet and liquid sealing bottle 20, and a liquid outlet is arranged at the lower part of the gas outlet and liquid sealing bottle 20;
the biogas supply device comprises a biogas high-pressure gas cylinder 23, a biogas pressure reducing valve 22 and a gas flowmeter 21, the biogas high-pressure gas cylinder 23 is communicated with the reflux device 13 through the reflux device gas inlet 15 by using a gas pipeline, and the biogas pressure reducing valve 22 and the gas flowmeter 21 are arranged on the gas pipeline.
The second embodiment is as follows: the present embodiment differs from the first embodiment in that: the reactor water inlet 8 and the reactor water outlet 6 are arranged on two sides of the hollow fiber membrane component. The rest is the same as the first embodiment.
The third concrete implementation mode: the present embodiment differs from the first or second embodiment in that: the biogas purification membrane bioreactor also comprises a magnetic stirrer 24, and the reflux device 13 is arranged on the magnetic stirrer 24. The others are the same as in the first or second embodiment.
The fourth concrete implementation mode: the difference between this embodiment and one of the first to third embodiments is as follows: the liquid contained in the water inlet tank 10 is a biogas purification liquid fermentation culture medium. The others are the same as the first to third embodiments.
The fifth concrete implementation mode: the difference between this embodiment and one of the first to fourth embodiments is: the biogas purification liquid fermentation culture medium is composed of NH4Cl、KCl、MgSO4·7H2O、NaCl、KH2PO4、CaCl2·2H2O, yeast powder, trace metal element liquid, vitamin liquid and NaHCO3A reducing agent liquid and water; NH in the biogas purification liquid fermentation culture medium4The concentration of Cl is 1.0g/L, the concentration of KCl is 0.1g/L, MgSO4·7H2The concentration of O is 0.2g/L, the concentration of NaCl is 0.8g/L, KH2PO4Has a concentration of 0.1g/L, CaCl2·2H2The concentration of O is 20mg/L, the concentration of yeast powder is 1g/L, the concentration of trace metal element stock solution is 10mL/L, the concentration of vitamin stock solution is 10mL/L, NaHCO3The concentration of the reducing agent is 2g/L, and the concentration of the reducing agent liquid is 10 ml/L;
the trace metal element liquid includes nitrilotriacetic acid and MnSO4·H2O、FeSO42NH42·6H2O、CoCl2·6H2O、ZnSO4·7H2O、CuCl2·2H2O、NiCl2·6H2O、Na2MoO4·2H2O、Na2SeO4And Na2WO4(ii) a The concentration of nitrilotriacetic acid in the trace metal element liquid storage is 2g/L, and MnSO4·H2The concentration of O is 1g/L, FeSO42NH42·6H2O concentration of 0.8g/L, CoCl2·6H2O concentration of 0.2g/L, ZnSO4·7H2O concentration of 0.2mg/L, CuCl2·2H2O concentration of 20mg/L, NiCl2·6H2The concentration of O is 20mg/L, Na2MoO4·2H2The concentration of O is 20mg/L, Na2SeO4Has a concentration of 20mg/L, Na2WO4The concentration of (A) is 20 mg/L;
the vitamin stock solution comprises biotin, folic acid, and vitamin B hydrochloride6Thiamine hydrochloride, vitamin B2Nicotinic acid, calcium pantothenate, vitamin B12P-aminobenzoic acid and lipoic acid; the concentration of biotin in the vitamin stock solution is 2mg/L, the concentration of folic acid is 2mg/L, and vitamin B hydrochloride6The concentration of (A) is 10mg/L, the concentration of thiamine hydrochloride is 5mg/L, vitamin B2The concentration of (a) is 5mg/L, the concentration of nicotinic acid is 5mg/L, the concentration of calcium pantothenate is 5mg/L, vitamin B12The concentration of the alpha-lipoic acid is 0.1mg/L, the concentration of the p-aminobenzoic acid is 5mg/L, and the concentration of the lipoic acid is 5 mg/L;
the reducing agent stock solution comprises NaOH, L-cysteine hydrochloride and Na2S·9H2O; the concentration of NaOH in the reducing agent liquid is 9g/L, the concentration of L-cysteine hydrochloride is 40g/L, Na2S·9H2The concentration of O was 40 g/L.
The rest is the same as the first to fourth embodiments.
The sixth specific implementation mode: the difference between this embodiment and one of the first to fifth embodiments is as follows: the gas contained in the water inlet air bag 11 is nitrogen. The rest is the same as the first to fifth embodiments.
The seventh embodiment: the embodiment is a use method of a biogas purification membrane bioreactor, which is specifically completed according to the following steps:
firstly, a starting stage: the water inlet pump 9 is opened, the biogas purification liquid fermentation culture medium contained in the water inlet tank 10 is injected into the reactor main body 3 through the water inlet 8 of the reactor, after the reactor main body 3 is filled with the biogas purification liquid fermentation culture medium, the biogas purification liquid fermentation culture medium flows into the reflux device 13 through the reactor water outlet 6 and the circulating water inlet 17, the water inlet pump 9 is closed when the liquid level of the biogas purification liquid fermentation culture medium in the reflux device 13 reaches the position of the reflux device water outlet 16, nitrogen with the purity of 99.99 percent is introduced into the reactor main body 3, the reactor main body 3 is sealed, then inoculating biogas purification seed liquid into the reactor main body 3, wherein the volume ratio of the biogas purification seed liquid to a fermentation culture medium of the biogas purification liquid is 1:10, the strain in the biogas purification seed liquid is clostridium P11, the concentration of the clostridium P11 in the biogas purification seed liquid is 1.8 g/L; opening the hydrogen pressure reducing valve 2, the methane pressure reducing valve 22 and the circulating pump 12, purifying the methane under the conditions that the circulating speed is 65mL/min, the hydrogen pressure is 1.25atm and the methane flow is 10mL/min, discharging the residual liquid into a gas-liquid sealed bottle 20 after purification, and collecting the purified methane in a gas collecting bag 19;
II, a continuous operation stage: and (3) closing the hydrogen pressure reducing valve 2, the methane pressure reducing valve 22 and the circulating pump 12 for 1 time and opening the water inlet pump 9 for 1 time every 12 hours of operation of the methane purification membrane bioreactor, and injecting a methane purification liquid fermentation culture medium into the reactor main body 3, wherein the addition amount of the methane purification liquid fermentation culture medium is one half of that of the methane purification liquid fermentation culture medium in the step one.
The specific implementation mode is eight: the seventh embodiment is different from the seventh embodiment in that: the biogas purification liquid fermentation culture medium in the first step and the second step is composed of NH4Cl、KCl、MgSO4·7H2O、NaCl、KH2PO4、CaCl2·2H2O, yeast powder, trace metal element liquid, vitamin liquid and NaHCO3A reducing agent liquid and water; NH in the biogas purification liquid fermentation culture medium4The concentration of Cl is 1.0g/L, the concentration of KCl is 0.1g/L, MgSO4·7H2The concentration of O is 0.2g/L, the concentration of NaCl is 0.8g/L, KH2PO4Has a concentration of 0.1g/L, CaCl2·2H2The concentration of O is 20mg/L, the concentration of yeast powder is 1g/L, the concentration of the trace metal element stock solution is 10mL/L, the concentration of the vitamin stock solution is 10mL/L, and NaHCO is3The concentration of the reducing agent is 2g/L, and the concentration of the reducing agent liquid is 10 ml/L;
the trace metal element liquid includes nitrilotriacetic acid and MnSO4·H2O、FeSO42NH42·6H2O、CoCl2·6H2O、ZnSO4·7H2O、CuCl2·2H2O、NiCl2·6H2O、Na2MoO4·2H2O、Na2SeO4And Na2WO4(ii) a The concentration of nitrilotriacetic acid in the trace metal element liquid storage is 2g/L, and MnSO4·H2The concentration of O is 1g/L, FeSO42NH42·6H2O concentration of 0.8g/L, CoCl2·6H2O concentration of 0.2g/L, ZnSO4·7H2O concentration of 0.2mg/L, CuCl2·2H2O concentration of 20mg/L, NiCl2·6H2The concentration of O is 20mg/L, Na2MoO4·2H2The concentration of O is 20mg/L, Na2SeO4Has a concentration of 20mg/L, Na2WO4The concentration of (A) is 20 mg/L;
the vitamin stock solution comprises biotin, folic acid, and vitamin B hydrochloride6Thiamine hydrochloride, vitamin B2Nicotinic acid, calcium pantothenate, vitamin B12P-aminobenzoic acid and lipoic acid; the concentration of biotin in the vitamin stock solution is 2mg/L, the concentration of folic acid is 2mg/L, and vitamin B hydrochloride6Has a concentration of 10mg/L, saltThe concentration of thiamine hydrochloride is 5mg/L, and vitamin B2The concentration of (a) is 5mg/L, the concentration of nicotinic acid is 5mg/L, the concentration of calcium pantothenate is 5mg/L, vitamin B12The concentration of the alpha-lipoic acid is 0.1mg/L, the concentration of the p-aminobenzoic acid is 5mg/L, and the concentration of the lipoic acid is 5 mg/L;
the reducing agent stock solution comprises NaOH, L-cysteine hydrochloride and Na2S·9H2O; the concentration of NaOH in the reducing agent liquid is 9g/L, the concentration of L-cysteine hydrochloride is 40g/L, Na2S·9H2The concentration of O was 40 g/L.
The rest is the same as the seventh embodiment.
The invention is not limited to the above embodiments, and one or a combination of several embodiments may also achieve the object of the invention.
The following tests are adopted to verify the effect of the invention:
example 1: the biogas purification membrane bioreactor comprises a water inlet device, a hydrogen gas supply device, a biogas supply device, a reactor, a circulating device and a gas outlet liquid sealing device;
the reactor comprises a reactor main body 3 and a hollow fiber membrane component, wherein the hollow fiber membrane component consists of a hollow fiber membrane tow 4, a membrane component seal head 5 and a membrane component fixing part 7, the membrane component seal heads 5 are arranged at two ends of the hollow fiber membrane tow 4, the hollow fiber membrane tow 4 is fixed in the reactor main body 3 through the membrane component seal heads 5 by utilizing the membrane component fixing part 7, a reactor water inlet 8 is arranged at the lower part of the reactor main body 3, and a reactor water outlet 6 is arranged at the upper part of the reactor main body 3;
the water inlet device consists of a water inlet pump 9, a water inlet tank 10 and a water inlet air bag 11, the water inlet tank 10 is communicated with a reactor water inlet 8 of the reactor through a water inlet pipeline, the water inlet pump 9 is arranged on the water inlet pipeline, and one end of the water inlet pipeline extends to a position below the liquid level in the water inlet tank 10; the water inlet tank 10 is communicated with the water inlet air bag 11 through an air supply pipeline, and one end of the air supply pipeline extends to be above the liquid level in the water inlet tank 10;
the hydrogen gas supply device comprises a hydrogen gas high-pressure gas cylinder 1, a hydrogen pressure reducing valve 2 and a gas pressure meter 25, wherein the hydrogen gas high-pressure gas cylinder 1 is communicated with the hollow fiber membrane tows 4 through a gas pipeline, and the hydrogen pressure reducing valve 2 and the gas pressure meter 25 are arranged on the gas pipeline;
the circulating device comprises a circulating pump 12, a reflux device 13, a circulating water outlet 14, a reflux device air inlet 15, a reflux device water outlet 16, a circulating water inlet 17 and a pH electrode 18; a circulating water outlet 14 and a reflux device air inlet 15 are arranged at the lower part of the reflux device 13, a reflux device water outlet 16 is arranged at the middle part of the reflux device 13, a circulating water inlet 17 is arranged at the upper part of the reflux device 13, a pH electrode 18 is arranged at the top part of the reflux device 13, one end of the pH electrode 18 extends to the position below the liquid level in the reflux device 13, the circulating water inlet 17 is communicated with the reactor water outlet 6 by a pipeline, the circulating water outlet 14 is communicated with the reactor water inlet 8 by a pipeline, and a circulating pump 12 is arranged on the pipeline for communicating the circulating water outlet 14 with the reactor water inlet 8;
the gas outlet liquid sealing device comprises a gas outlet liquid sealing bottle 20 and a gas collecting bag 19, and the gas outlet liquid sealing bottle 20 is communicated with the reflux device 13 through a water outlet 16 of the reflux device by a pipeline; the gas outlet and liquid sealing bottle 20 is communicated with the gas collecting bag 19 through a gas pipe, one end of the gas pipe extends to be above the liquid level in the gas outlet and liquid sealing bottle 20, and a liquid outlet is arranged at the lower part of the gas outlet and liquid sealing bottle 20;
the biogas supply device comprises a biogas high-pressure gas cylinder 23, a biogas pressure reducing valve 22 and a gas flowmeter 21, the biogas high-pressure gas cylinder 23 is communicated with the reflux device 13 through the reflux device gas inlet 15 by using a gas pipeline, and the biogas pressure reducing valve 22 and the gas flowmeter 21 are arranged on the gas pipeline.
The reactor water inlet 8 and the reactor water outlet 6 are arranged on two sides of the hollow fiber membrane component.
The biogas purification membrane bioreactor also comprises a magnetic stirrer 24, and the reflux device 13 is arranged on the magnetic stirrer 24.
The liquid contained in the water inlet tank 10 is a biogas purification liquid fermentation culture medium; the biogas purification liquid fermentation culture medium is composed of NH4Cl、KCl、MgSO4·7H2O、NaCl、KH2PO4、CaCl2·2H2O, YeastPowder, trace metal element liquid, vitamin liquid and NaHCO3A reducing agent liquid and water; NH in the biogas purification liquid fermentation culture medium4The concentration of Cl is 1.0g/L, the concentration of KCl is 0.1g/L, MgSO4·7H2The concentration of O is 0.2g/L, the concentration of NaCl is 0.8g/L, KH2PO4Has a concentration of 0.1g/L, CaCl2·2H2The concentration of O is 20mg/L, the concentration of yeast powder is 1g/L, the concentration of the trace metal element stock solution is 10mL/L, the concentration of the vitamin stock solution is 10mL/L, and NaHCO is3The concentration of the reducing agent is 2g/L, and the concentration of the reducing agent liquid is 10 ml/L; the trace metal element liquid includes nitrilotriacetic acid and MnSO4·H2O、FeSO42NH42·6H2O、CoCl2·6H2O、ZnSO4·7H2O、CuCl2·2H2O、NiCl2·6H2O、Na2MoO4·2H2O、Na2SeO4And Na2WO4(ii) a The concentration of nitrilotriacetic acid in the trace metal element liquid storage is 2g/L, and MnSO4·H2The concentration of O is 1g/L, FeSO42NH42·6H2O concentration of 0.8g/L, CoCl2·6H2O concentration of 0.2g/L, ZnSO4·7H2O concentration of 0.2mg/L, CuCl2·2H2O concentration of 20mg/L, NiCl2·6H2The concentration of O is 20mg/L, Na2MoO4·2H2The concentration of O is 20mg/L, Na2SeO4Has a concentration of 20mg/L, Na2WO4The concentration of (A) is 20 mg/L; the vitamin stock solution comprises biotin, folic acid, and vitamin B hydrochloride6Thiamine hydrochloride, vitamin B2Nicotinic acid, calcium pantothenate, vitamin B12P-aminobenzoic acid and lipoic acid; the concentration of biotin in the vitamin stock solution is 2mg/L, the concentration of folic acid is 2mg/L, and vitamin B hydrochloride6The concentration of (A) is 10mg/L, the concentration of thiamine hydrochloride is 5mg/L, vitamin B2The concentration of (a) is 5mg/L, the concentration of nicotinic acid is 5mg/L, the concentration of calcium pantothenate is 5mg/L, vitamin B12Concentration of (2)The concentration of 0.1mg/L, the concentration of p-aminobenzoic acid is 5mg/L, and the concentration of lipoic acid is 5 mg/L; the reducing agent stock solution comprises NaOH, L-cysteine hydrochloride and Na2S·9H2O; the concentration of NaOH in the reducing agent liquid is 9g/L, the concentration of L-cysteine hydrochloride is 40g/L, Na2S·9H2The concentration of O was 40 g/L.
The gas contained in the water inlet air bag 11 is nitrogen
Example 2: the use method of the biogas purification membrane bioreactor in the embodiment 1 is specifically completed according to the following steps:
firstly, a starting stage: the water inlet pump 9 is opened, the biogas purification liquid fermentation culture medium contained in the water inlet tank 10 is injected into the reactor main body 3 through the water inlet 8 of the reactor, after the reactor main body 3 is filled with the biogas purification liquid fermentation culture medium, the biogas purification liquid fermentation culture medium flows into the reflux device 13 through the reactor water outlet 6 and the circulating water inlet 17, the water inlet pump 9 is closed when the liquid level of the biogas purification liquid fermentation culture medium in the reflux device 13 reaches the position of the reflux device water outlet 16, nitrogen with the purity of 99.99 percent is introduced into the reactor main body 3, the reactor main body 3 is sealed, then inoculating biogas purification seed liquid into the reactor main body 3, wherein the volume ratio of the biogas purification seed liquid to a fermentation culture medium of the biogas purification liquid is 1:10, the strain in the biogas purification seed liquid is clostridium P11, the concentration of the clostridium P11 in the biogas purification seed liquid is 1.8 g/L; opening the hydrogen pressure reducing valve 2, the methane pressure reducing valve 22 and the circulating pump 12, purifying the methane under the conditions that the circulating speed is 65mL/min, the hydrogen pressure is 1.25atm and the methane flow is 10mL/min, discharging the residual liquid into a gas-liquid sealed bottle 20 after purification, and collecting the purified methane in a gas collecting bag 19;
II, a continuous operation stage: and (3) closing the hydrogen pressure reducing valve 2, the methane pressure reducing valve 22 and the circulating pump 12 for 1 time and opening the water inlet pump 9 for 1 time every 12 hours of operation of the methane purification membrane bioreactor, and injecting a methane purification liquid fermentation culture medium into the reactor main body 3, wherein the addition amount of the methane purification liquid fermentation culture medium is one half of that of the methane purification liquid fermentation culture medium in the step one.
The purified biogas collected in the gas collection bag 19 of the embodiment 2 is detected, and the purity of the biogas is over 93.2 percent; when the liquid in the gas-sealed bottle 20 of example 2 was measured, it was found that the ethanol yield of example 2 was 1.56 g/L.d.

Claims (6)

1. The biogas purification membrane bioreactor is characterized by comprising a water inlet device, a hydrogen gas supply device, a biogas gas supply device, a reactor, a circulating device and a gas outlet liquid sealing device;
the reactor comprises a reactor main body (3) and a hollow fiber membrane assembly, wherein the hollow fiber membrane assembly consists of a hollow fiber membrane tow (4), a membrane assembly end enclosure (5) and a membrane assembly fixing piece (7), the membrane assembly end enclosure (5) is arranged at two ends of the hollow fiber membrane tow (4), the hollow fiber membrane tow (4) is fixed in the reactor main body (3) through the membrane assembly end enclosure (5) by using the membrane assembly fixing piece (7), a reactor water inlet (8) is arranged at the lower part of the reactor main body (3), and a reactor water outlet (6) is arranged at the upper part of the reactor main body (3); the reactor main body (3) is inoculated with biogas purification seed liquid, and the strain in the biogas purification seed liquid is clostridium P11;
the water inlet device consists of a water inlet pump (9), a water inlet tank (10) and a water inlet air bag (11), the water inlet tank (10) is communicated with a reactor water inlet (8) of the reactor through a water inlet pipeline, the water inlet pump (9) is arranged on the water inlet pipeline, and one end of the water inlet pipeline extends to a position below the liquid level in the water inlet tank (10); the water inlet tank (10) is communicated with the water inlet air bag (11) through an air supply pipeline, and one end of the air supply pipeline extends to be above the liquid level in the water inlet tank (10); the liquid contained in the water inlet tank (10) is a biogas purification liquid fermentation culture medium, and the gas contained in the water inlet air bag (11) is nitrogen;
the hydrogen gas supply device comprises a hydrogen gas high-pressure gas cylinder (1), a hydrogen pressure reducing valve (2) and a gas pressure meter (25), the hydrogen gas high-pressure gas cylinder (1) is communicated with the hollow fiber membrane tows (4) through a gas pipeline, and the hydrogen pressure reducing valve (2) and the gas pressure meter (25) are arranged on the gas pipeline;
the circulating device comprises a circulating pump (12), a reflux device (13), a circulating water outlet (14), a reflux device air inlet (15), a reflux device water outlet (16), a circulating water inlet (17) and a pH electrode (18); a circulating water outlet (14) and a backflow device air inlet (15) are arranged at the lower part of the backflow device (13), a backflow device water outlet (16) is arranged at the middle part of the backflow device (13), a circulating water inlet (17) is arranged at the upper part of the backflow device (13), a pH electrode (18) is arranged at the top of the backflow device (13), one end of the pH electrode (18) extends to the position below the liquid level in the backflow device (13), the circulating water inlet (17) is communicated with a reactor water outlet (6) by a pipeline, the circulating water outlet (14) is communicated with a reactor water inlet (8) by a pipeline, and a circulating pump (12) is arranged on the pipeline for communicating the circulating water outlet (14) with the reactor water inlet (8);
the gas outlet liquid sealing device comprises a gas outlet liquid sealing bottle (20) and a gas collecting bag (19), and the gas outlet liquid sealing bottle (20) is communicated with the reflux device (13) through a water outlet (16) of the reflux device by a pipeline; the gas-liquid outlet sealed bottle (20) is communicated with the gas collecting bag (19) through a gas pipe, one end of the gas pipe extends to be above the liquid level in the gas-liquid outlet sealed bottle (20), and a liquid outlet is arranged at the lower part of the gas-liquid outlet sealed bottle (20);
the biogas supply device comprises a biogas high-pressure gas cylinder (23), a biogas pressure reducing valve (22) and a gas flowmeter (21), the biogas high-pressure gas cylinder (23) is communicated with the reflux device (13) through a reflux device gas inlet (15) by utilizing a gas pipeline, and the biogas pressure reducing valve (22) and the gas flowmeter (21) are arranged on the gas pipeline.
2. The membrane bioreactor for purifying biogas according to claim 1, wherein the water inlet (8) and the water outlet (6) are disposed on both sides of the hollow fiber membrane module.
3. The membrane bioreactor for purifying biogas according to claim 1, wherein the membrane bioreactor for purifying biogas further comprises a magnetic stirrer (24), and the backflow device (13) is arranged on the magnetic stirrer (24).
4. The membrane bioreactor for purifying biogas as recited in claim 1, wherein the biogas purification liquid fermentation medium is composed of NH4Cl、KCl、MgSO4·7H2O、NaCl、KH2PO4、CaCl2·2H2O, yeast powder, trace metal element liquid, vitamin liquid and NaHCO3A reducing agent liquid and water; NH in the biogas purification liquid fermentation culture medium4The concentration of Cl is 1.0g/L, the concentration of KCl is 0.1g/L, MgSO4·7H2The concentration of O is 0.2g/L, the concentration of NaCl is 0.8g/L, KH2PO4Has a concentration of 0.1g/L, CaCl2·2H2The concentration of O is 20mg/L, the concentration of yeast powder is 1g/L, the concentration of the trace metal element stock solution is 10mL/L, the concentration of the vitamin stock solution is 10mL/L, and NaHCO is3The concentration of the reducing agent is 2g/L, and the concentration of the reducing agent liquid is 10 ml/L;
the trace metal element liquid includes nitrilotriacetic acid and MnSO4·H2O、Fe(SO4)2(NH4)2·6H2O、CoCl2·6H2O、ZnSO4·7H2O、CuCl2·2H2O、NiCl2·6H2O、Na2MoO4·2H2O、Na2SeO4And Na2WO4(ii) a The concentration of nitrilotriacetic acid in the trace metal element liquid storage is 2g/L, and MnSO4·H2O concentration of 1g/L, Fe (SO)4)2(NH4)2·6H2O concentration of 0.8g/L, CoCl2·6H2O concentration of 0.2g/L, ZnSO4·7H2O concentration of 0.2mg/L, CuCl2·2H2O concentration of 20mg/L, NiCl2·6H2The concentration of O is 20mg/L, Na2MoO4·2H2The concentration of O is 20mg/L, Na2SeO4Has a concentration of 20mg/L, Na2WO4The concentration of (A) is 20 mg/L;
the vitamin stock solution comprises biotin, folic acid, and vitamin B hydrochloride6Thiamine hydrochloride, vitamin B2Nicotinic acid, calcium pantothenate, vitamin B12P-aminobenzoic acid and lipoic acid; the concentration of biotin in the vitamin stock solution is 2mg/L,the concentration of folic acid is 2mg/L, and vitamin B hydrochloride6The concentration of (A) is 10mg/L, the concentration of thiamine hydrochloride is 5mg/L, vitamin B2The concentration of (a) is 5mg/L, the concentration of nicotinic acid is 5mg/L, the concentration of calcium pantothenate is 5mg/L, vitamin B12The concentration of the alpha-lipoic acid is 0.1mg/L, the concentration of the p-aminobenzoic acid is 5mg/L, and the concentration of the lipoic acid is 5 mg/L;
the reducing agent stock solution comprises NaOH, L-cysteine hydrochloride and Na2S·9H2O; the concentration of NaOH in the reducing agent liquid is 9g/L, the concentration of L-cysteine hydrochloride is 40g/L, Na2S·9H2The concentration of O was 40 g/L.
5. The use method of the biogas purification membrane bioreactor according to any one of claims 1 to 4, characterized in that the method is completed by the following steps:
firstly, a starting stage: opening a water inlet pump (9), injecting a biogas purification liquid fermentation culture medium contained in a water inlet tank (10) into a reactor main body (3) through a reactor water inlet (8), after the reactor main body (3) is filled, allowing the biogas purification liquid fermentation culture medium to flow into a reflux device (13) through a reactor water outlet (6) and a circulating water inlet (17), closing the water inlet pump (9) when the liquid level of the biogas purification liquid fermentation culture medium in the reflux device (13) reaches the position of a reflux device water outlet (16), introducing nitrogen with the purity of 99.99% into the reactor main body (3), sealing the reactor main body (3), then inoculating biogas purification seed liquid into the reactor main body (3), wherein the volume ratio of the biogas purification seed liquid to the biogas purification liquid fermentation culture medium is 1:10, and the strain in the biogas purification seed liquid is clostridium sp 11, the concentration of the clostridium P11 in the biogas purification seed liquid is 1.8 g/L; opening a hydrogen pressure reducing valve (2), a methane pressure reducing valve (22) and a circulating pump (12), controlling the circulating speed to be 65mL/min, the hydrogen pressure to be 1.25atm and the methane flow to be 10mL/min, purifying the methane, feeding the purified residual liquid into a gas-liquid outlet sealed bottle (20), and collecting the purified methane in a gas collecting bag (19);
II, a continuous operation stage: and (3) closing the hydrogen pressure reducing valve (2), the methane pressure reducing valve (22) and the circulating pump (12) for 1 time and opening the water inlet pump (9) for 1 time every 12 hours of operation of the methane purification membrane bioreactor, and injecting a methane purification liquid fermentation culture medium into the reactor main body (3), wherein the addition amount of the methane purification liquid fermentation culture medium is one half of that of the methane purification liquid fermentation culture medium in the step one.
6. The method of claim 5, wherein the fermentation medium of the biogas purification membrane bioreactor is NH4Cl、KCl、MgSO4·7H2O、NaCl、KH2PO4、CaCl2·2H2O, yeast powder, trace metal element liquid, vitamin liquid and NaHCO3A reducing agent liquid and water; NH in the biogas purification liquid fermentation culture medium4The concentration of Cl is 1.0g/L, the concentration of KCl is 0.1g/L, MgSO4·7H2The concentration of O is 0.2g/L, the concentration of NaCl is 0.8g/L, KH2PO4Has a concentration of 0.1g/L, CaCl2·2H2The concentration of O is 20mg/L, the concentration of yeast powder is 1g/L, the concentration of the trace metal element stock solution is 10mL/L, the concentration of the vitamin stock solution is 10mL/L, and NaHCO is3The concentration of the reducing agent is 2g/L, and the concentration of the reducing agent liquid is 10 ml/L;
the trace metal element liquid includes nitrilotriacetic acid and MnSO4·H2O、Fe(SO4)2(NH4)2·6H2O、CoCl2·6H2O、ZnSO4·7H2O、CuCl2·2H2O、NiCl2·6H2O、Na2MoO4·2H2O、Na2SeO4And Na2WO4(ii) a The concentration of nitrilotriacetic acid in the trace metal element liquid storage is 2g/L, and MnSO4·H2O concentration of 1g/L, Fe (SO)4)2(NH4)2·6H2O concentration of 0.8g/L, CoCl2·6H2O concentration of 0.2g/L, ZnSO4·7H2O concentration of 0.2mg/L, CuCl2·2H2O concentration of 20mg/L, NiCl2·6H2The concentration of O is 20mg/L, Na2MoO4·2H2The concentration of O is 20mg/L, Na2SeO4Has a concentration of 20mg/L, Na2WO4The concentration of (A) is 20 mg/L;
the vitamin stock solution comprises biotin, folic acid, and vitamin B hydrochloride6Thiamine hydrochloride, vitamin B2Nicotinic acid, calcium pantothenate, vitamin B12P-aminobenzoic acid and lipoic acid; the concentration of biotin in the vitamin stock solution is 2mg/L, the concentration of folic acid is 2mg/L, and vitamin B hydrochloride6The concentration of (A) is 10mg/L, the concentration of thiamine hydrochloride is 5mg/L, vitamin B2The concentration of (a) is 5mg/L, the concentration of nicotinic acid is 5mg/L, the concentration of calcium pantothenate is 5mg/L, vitamin B12The concentration of the alpha-lipoic acid is 0.1mg/L, the concentration of the p-aminobenzoic acid is 5mg/L, and the concentration of the lipoic acid is 5 mg/L;
the reducing agent stock solution comprises NaOH, L-cysteine hydrochloride and Na2S·9H2O; the concentration of NaOH in the reducing agent liquid is 9g/L, the concentration of L-cysteine hydrochloride is 40g/L, Na2S·9H2The concentration of O was 40 g/L.
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CN104962333A (en) * 2015-05-29 2015-10-07 西安建筑科技大学 Membrane separation biogas biological desulfurization method and device
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104962333A (en) * 2015-05-29 2015-10-07 西安建筑科技大学 Membrane separation biogas biological desulfurization method and device
CN207684974U (en) * 2017-12-26 2018-08-03 哈尔滨工业大学 New membrane is aerated membrane bioreactor

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