WO2022082813A1 - 处理硫酸盐有机废水的方法和系统 - Google Patents

处理硫酸盐有机废水的方法和系统 Download PDF

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WO2022082813A1
WO2022082813A1 PCT/CN2020/123562 CN2020123562W WO2022082813A1 WO 2022082813 A1 WO2022082813 A1 WO 2022082813A1 CN 2020123562 W CN2020123562 W CN 2020123562W WO 2022082813 A1 WO2022082813 A1 WO 2022082813A1
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tank
biogas
liquid
gas
acidification
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PCT/CN2020/123562
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English (en)
French (fr)
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赵全保
俞汉青
吴小琼
郑煜铭
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中国科学院城市环境研究所
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Publication of WO2022082813A1 publication Critical patent/WO2022082813A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/286—Anaerobic digestion processes including two or more steps
    • 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
    • B01D53/14—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 by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2866—Particular arrangements for anaerobic reactors
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F7/00—Aeration of stretches of water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/101—Sulfur compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/04—Flow arrangements
    • C02F2301/043—Treatment of partial or bypass streams
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
    • 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
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the invention relates to a method and a system for treating sulfate organic wastewater, belonging to the technical field of wastewater treatment.
  • Some food production wastewater, medical wastewater, papermaking wastewater, leather wastewater and aquaculture wastewater contain relatively high concentrations of sulfate. Since these wastewaters often contain high concentrations of organic matter at the same time, they are usually treated with anaerobic techniques.
  • Chinese patent CN108821429A discloses a device system for sulfate wastewater treatment and its treatment method, the device system includes an anaerobic reaction unit, a stripping unit, an absorption unit, and a biological desulfurization unit. and gas storage unit. Since this treatment method adopts a single-phase anaerobic method, the toxic effect of H 2 S on methanogens and the inhibitory effect on methanogenic reaction cannot be avoided, resulting in poor anaerobic treatment effect.
  • the H 2 S removal process in either the single-phase anaerobic method or the two-phase anaerobic method is relatively complicated, involving the addition of additional alkaline chemical reagents or desulfurizing agents, resulting in the existing H 2 S removal process.
  • the S removal process is difficult, costly or inefficient, and it will cause pollution.
  • the sulfur-containing biogas generated by the anaerobic reaction unit and the sulfur-containing degassing generated by the stripping unit enter the absorption unit for processing, and produce sulfide absorption liquid and purification. after the biogas.
  • the sulfide absorbing liquid finally enters the biological desulfurization unit, and the biological sulfur is oxidized by aeration to obtain elemental sulfur and clear liquid.
  • the H 2 S removal process has high energy consumption, complex process, and the need to add additional alkaline chemical reagents, which is not conducive to reducing process costs, and the conditions of biological desulfurization are also difficult to control.
  • Chinese patent CN105776525A discloses an integrated two-phase anaerobic desulfurization reactor and a wastewater treatment method thereof.
  • the reactor includes an integrated desulfurization reaction tank and a methanogenesis reaction tank.
  • the sulfate wastewater enters the desulfurization reaction tank and the methanogenesis reaction tank for treatment in turn.
  • the desulfurization reaction tank and the methanogenesis reaction tank are only separated by a partition wall and connected by an outlet weir.
  • the bottom of the desulfurization reaction tank is provided with an aeration head, and the collected desulfurization biogas is used to aerate the desulfurization reaction tank.
  • the reactor combines and collects the gas produced by the desulfurization reaction tank and the methane-producing reaction tank through the biogas collection pipe, and conducts a unified desulfurization treatment through a specially set tail gas treatment unit, which not only increases the gas treatment capacity, but also increases the amount of gas produced. While removing H 2 S, H 2 , CO 2 and some volatile organic acids must also be treated, which increases the difficulty and cost of the H 2 S removal process.
  • the present application proposes a method and system for treating sulfate organic wastewater, which can utilize the stripped biogas slurry produced by the biogas slurry stripping tank to absorb the H 2 S released by the hydrolysis acidification tank , the method does not need to use additional alkaline chemical reagents or desulfurization agents, making the method simple, economical, efficient and environmentally friendly.
  • the present invention provides a method for treating sulfate organic wastewater, the method comprising the steps of: making the acidified gas containing H 2 S produced in the hydrolysis acidification tank enter the H 2 S absorption tank; making the hydrolysis acidification tank produce The hydrolyzed and acidified liquid enters the methane-producing tank to produce biogas and biogas liquid; the biogas liquid enters the biogas liquid stripping tank for ammonia nitrogen and carbon dioxide removal to obtain stripped biogas liquid; part of the stripped biogas liquid enters H 2 S The absorption tank is used as the absorption liquid to absorb H 2 S in the acidified gas.
  • the method also includes the following steps: making the absorbing liquid in the H 2 S absorption tank flow in a deflected manner along the direction from top to bottom, absorbing the H 2 S in the acidified gas, and producing a sulfur-containing absorbing liquid ;
  • the acidified gas containing H 2 S in the S absorption tank flows from bottom to top, and after desulfurization, desulfurized gas is formed; wherein, the flow directions of the absorbing liquid and the acid gas containing H 2 S are opposite, so that the The acidification gas and the absorbing liquid can be fully contacted.
  • the method also includes the following steps: making part of the desulfurized gas generated in the H 2 S absorption tank enter the hydrolysis and acidification tank; making the liquid in the hydrolysis and acidification tank flow along the guide device under the action of the desulfurized gas, so that the hydrolysis and acidification tank flows The mixture in the mixture was well stirred and accelerated the release of H 2 S.
  • the method further includes the following steps: returning part of the sulfur-containing absorbing liquid produced in the H 2 S absorption tank to the biogas liquid stripping tank; making part of the desulfurized gas generated in the H 2 S absorption tank enter the methane-producing tank to be used as biogas raw materials for production.
  • the method also includes using a microporous aeration head arranged at the bottom of the biogas slurry stripping tank to remove ammonia nitrogen and carbon dioxide from the biogas slurry entering the biogas liquid stripping tank to obtain stripped biogas slurry.
  • the present invention also provides a system for treating sulfate organic wastewater, the system comprising: a hydrolysis acidification tank, which is used to generate acidification gas and hydrolysis acidification liquid containing H2S ; an H2S absorption tank, which is combined with the hydrolysis acidification tank.
  • the acidification tank is connected, so that the acidification gas containing H 2 S enters the H 2 S absorption tank; the methanogenesis tank is connected with the hydrolysis acidification tank so that the hydrolysis acidification liquid enters the methanogenic tank In the methane-producing pond, the hydrolyzed and acidified liquid is used to produce biogas and biogas liquid; and the biogas liquid stripping tank is connected to the methane-producing tank so that the biogas liquid enters the biogas liquid stripping tank.
  • the biogas slurry stripping tank removes ammonia nitrogen and carbon dioxide from the biogas slurry entering it to obtain stripped biogas slurry; wherein the biogas slurry stripping tank is also connected with the H 2 S absorption tank , so that part of the stripped biogas slurry enters the H 2 S absorption tank as absorption liquid to absorb H 2 S in the acidified gas.
  • the air outlet of the H 2 S absorption tank is connected with the air inlet of the hydrolysis and acidification tank, so as to input partial desulfurization gas into the hydrolysis and acidification tank; It is used to make the liquid in the hydrolysis and acidification tank flow along the guide device under the action of desulfurization gas, so that the mixed liquid in the hydrolysis and acidification tank can be fully stirred and the release of H 2 S is accelerated.
  • the gas outlet of the H 2 S absorption tank is also connected with the gas inlet of the methane-producing tank, so as to input the partially desulfurized gas into the methane-producing tank.
  • the H 2 S absorption tank is also provided with a baffle plate assembly, and the baffle plate assembly includes a plurality of baffle plates that alternately extend from both sides of the H 2 S absorption tank, so that the absorption liquid can be moved along the The flow is baffled in the top-to-bottom direction.
  • the sulfur-containing absorbing liquid outlet of the H 2 S absorption tank is also connected with the reflux liquid inlet of the biogas slurry stripping tank and the outside, so as to input the sulfur-containing absorption liquid to the biogas liquid stripping tank, or to the outside. Sulfur-containing absorbing liquid is discharged.
  • a microporous aeration head is installed at the bottom of the biogas liquid stripping tank, and an air pump is installed on the air supply pipeline of the microporous aeration head; the biogas liquid stripping tank is also connected to the water outlet tank and the waste gas treatment device respectively .
  • the system also includes an automatic control mechanism, the automatic control mechanism includes: a sulfate and sulfide analyzer, a biogas composition analyzer, and a controller, the controller is respectively connected with the sulfate and sulfide analyzer, the biogas analyzer
  • the composition analyzer is electrically connected; the sulfate and sulfide analyzer is arranged on the pipeline connecting the hydrolysis acidification tank and the methanogenic tank to analyze the hydrolysis acidification liquid output from the hydrolysis acidification tank; the biogas The composition analyzer is arranged on the methanogenic tank and communicated with the inside of the methanogenic tank to analyze the biogas produced in the methanogenic tank; the controller is based on the sulfate and sulfide analyzer and the biogas
  • the real-time data obtained by the composition analyzer automatically controls the flow rate of the air pump and the flow rate of the desulfurized gas entering the hydrolysis acidification tank.
  • the present invention can utilize the stripped biogas slurry produced by the biogas slurry stripping tank to absorb the H 2 S released by the hydrolysis and acidification tank. Since there is no need to use additional alkaline chemical reagents or desulfurization agents, the method is simple, economical and efficient. And environmentally friendly.
  • the mixed solution in the hydrolysis acidification tank can be fully stirred and the release of H 2 S is accelerated, which helps to improve the desulfurization effect of the hydrolysis acidification solution.
  • the H 2 S released from the hydrolysis and acidification tank can be fully contacted with the stripped biogas slurry produced by the biogas slurry stripping tank in the H 2 S absorption tank, so as to better and efficiently Energy efficient removal of H 2 S from acidification gas.
  • the present invention can provide more raw materials for biogas production by making part of the desulfurized gas enter the methane-producing tank, which is beneficial to increase the output of biogas.
  • part of the sulfur-containing absorbing liquid is returned to the biogas liquid stripping tank, so that the total liquid in the biogas liquid stripping tank can be prevented from being significantly decreased, which is beneficial to the stable operation of the system.
  • the present invention can provide sulfur-containing raw materials for subsequent chemical fertilizer production by collecting the sulfur-containing absorbing liquid discharged to the outside.
  • the controller of the present invention can adjust the flow of the air entering the biogas slurry stripping tank through the air pump and the desulfurization entering the hydrolysis and acidification tank through the anti-corrosion air pump according to the real-time data obtained by the sulfate and sulfide analyzer and the biogas composition analyzer.
  • the flow rate of acidification gas is conducive to ensuring the efficient and normal operation of the system.
  • microporous aeration head By setting the microporous aeration head in the present invention, it is beneficial to improve the stripping effect of ammonia nitrogen and carbon dioxide in the biogas slurry and reduce the energy consumption for stripping the biogas slurry.
  • the present invention is beneficial to improve the environmental protection performance of the system by setting the water outlet pool and the waste gas treatment device.
  • Fig. 1 shows the structural schematic diagram of the system for processing sulfate organic wastewater of the present invention
  • Figure 2 shows a schematic structural diagram of the automatic control mechanism of the present invention.
  • the present invention provides a method for treating sulfate organic wastewater, which comprises the following steps: making the acidified gas containing H 2 S generated by the hydrolysis acidification tank 1 enter the H 2 S absorption tank 4;
  • the acidified liquid enters the methane-producing tank 2 to generate biogas and biogas liquid;
  • the biogas liquid enters the biogas liquid stripping tank 3 for ammonia nitrogen and carbon dioxide removal, and the stripped biogas liquid is obtained; part of the stripped biogas liquid enters H 2 S
  • the absorption tank 4 is used as an absorption liquid to absorb H 2 S in the acidified gas.
  • the sulfate organic wastewater enters the hydrolysis acidification tank 1 through the sulfate organic wastewater inlet 101 of the hydrolysis acidification tank 1 .
  • the sulfate organic wastewater undergoes hydrolysis acidification and sulfate reduction reaction under the action of fermentation bacteria, acid-producing bacteria and sulfate reducing bacteria in the hydrolysis acidification tank 1, so that the sulfate in the wastewater is converted into H 2 S and other sulfides, and Convert organic matter in wastewater into organic acid, H2 , etc.
  • the acidification gas containing H 2 S produced by the hydrolysis and acidification tank 1 is drawn from the hydrolysis acidification tank 1 through the gas transmission pipeline and enters the H 2 S absorption tank 4 through the acidification gas inlet 403 of the H 2 S absorption tank 4, which is beneficial to avoid sulfides. Entering the methane-producing pool 2, which in turn helps to alleviate the negative impact of sulfide on methane production.
  • the desulfurized hydrolyzed and acidified liquid produced by the hydrolysis and acidification tank 1 enters the methane-producing tank 2 through the hydrolyzed and acidified liquid outlet 102 of the hydrolysis and acidification tank 1, the connecting pipeline and the hydrolyzed and acidified liquid inlet 201 of the methane-producing tank 2, and the process relies on the action of gravity.
  • the hydrolyzed acidified liquid converts the organic acids and the like into biogas, and the biogas is led out through the pipeline.
  • the biogas produced by the methane-producing tank 2 has a lower sulfur content, which greatly reduces the corrosion of equipment and pipelines during the direct utilization of biogas.
  • the biogas slurry produced in the methane-producing tank 2 enters the biogas slurry stripping tank 3 through the biogas slurry outlet 202 of the methane-producing tank 2 , the connecting pipeline and the biogas slurry inlet 301 of the biogas slurry stripping tank 3 .
  • Gases such as CO 2 and NH 3 in the biogas slurry are removed by aeration, and the pH of the biogas slurry is raised to 9.0-10.0 to form the stripped biogas slurry.
  • the stripped biogas slurry enters the H 2 S absorption tank 4 through the stripped biogas slurry reflux outlet 304 of the biogas liquid stripping tank 3, the connecting pipeline and the stripped biogas slurry inlet 401 of the H 2 S absorption tank 4,
  • the biogas slurry after stripping introduced into the H 2 S absorption tank 4 accounts for 1/6-2/3 of the total amount of biogas slurry after stripping.
  • the alkaline biogas slurry after stripping is contacted with the acidified gas phase containing H 2 S to absorb and purify the H 2 S through the acid-base reaction to produce sulfur-containing absorption liquid and desulfurized gas, wherein , and part of the sulfur-containing absorbing liquid is discharged to the outside for subsequent fertilizer production.
  • the stripped biogas slurry produced by the biogas slurry stripping tank 3 can be used to absorb the H 2 S released by the hydrolysis and acidification tank 1. Since there is no need to use additional alkaline chemical reagents or desulfurization agents, the method is simple, economical, and economical. Efficient and environmentally friendly.
  • the method also includes the following steps: making the partially desulfurized gas generated in the H 2 S absorption tank 4 enter the hydrolysis and acidification tank 1; flow, so that the mixed solution in the hydrolysis-acidification tank 1 can be fully stirred and the release of H 2 S is accelerated.
  • the H 2 S absorption tank 4 also includes an air outlet 404 at the top of the absorbing tank 4.
  • the air outlet 404 is communicated with the air inlet 104 of the hydrolysis and acidification tank 1 through a pipeline, and the air outlet 404 is connected to the air inlet 104 through a pipeline.
  • An anti-corrosion air pump 9 is arranged on the pipeline.
  • the use of the anti-corrosion air pump 9 can slow down the corrosion of the air pump by the desulfated gas.
  • the anti-corrosion gas pump 9 pumps the partially desulfated gas produced by the H 2 S absorption tank 4 into the hydrolysis acidification tank 1 to better mix the mixed liquid in the hydrolysis acidification tank 1, on the one hand, the sulfate organic wastewater is mixed with fermentation bacteria, acid-producing bacteria and The sulfate-reducing bacteria are fully contacted, and on the other hand, it promotes the transfer of H 2 S gas from the liquid phase to the gas phase and the conversion of other sulfides in the solution to H 2 S, and makes the pH value of the hydrolyzed acidified solution entering the methanogenic tank 2 higher than high, which contributes to the generation of biogas.
  • the air guide device is a guide plate 105 .
  • the deflector 105 includes a main body and two side wings, the main body is vertically arranged, the two side wings are respectively connected to the top end and the bottom end of the main body, and the included angles with the main body are both obtuse angles; the height difference between the air inlet 104 and the liquid surface is 0.5-5.5 meters.
  • the main body of the deflector 105 is arranged vertically, the top side wings extend obliquely upward, and the bottom side wings extend diagonally downward, and the liquid in the hydrolysis and acidification tank 1 flows from bottom to top along the deflector 105 under the action of the desulfurized gas, so that the The mixed solution in the hydrolysis and acidification tank 1 is fully mixed and the release of H 2 S is accelerated, which is helpful for reducing the energy consumption required for mixing and improving the desulfurization effect.
  • the height difference between the air inlet 104 and the liquid surface is 0.5-5.5 meters. If the distance is too large, it is not conducive to reducing the energy consumption of the anti-corrosion air pump 9; if the distance is too small, it is not conducive to the full stirring of the mixed liquid.
  • the diversion device can assist the desulfurization gas to blow and dehydrate the H 2 S in the acidification tank 1, so that the sulfur ions in the liquid in the hydrolysis and acidification tank 1 can be continuously converted into H 2 S, so as to achieve the purpose of high-efficiency desulfurization.
  • the mixed solution in the hydrolysis and acidification tank 1 can be fully stirred and the H 2 S release can be accelerated, which helps to reduce the energy consumption required for mixing and improve the desulfurization effect.
  • the method further includes the following steps: making the absorbing liquid in the H 2 S absorption tank 4 flow in a deflected manner along the direction from top to bottom, absorbing the H 2 S in the acidified gas, and producing a sulfur-containing absorbing liquid ; Make the acidified gas containing H 2 S entering the H 2 S absorption tank 4 to flow along the direction from bottom to top, and form the desulfurized gas after the desulfurization; wherein, the absorbing liquid is opposite to the flow direction of the acid gas containing H 2 S, with The acidified gas containing H 2 S and the absorbing liquid can be sufficiently contacted.
  • the acidification gas inlet 403 is located at the bottom of the H 2 S absorption tank 4, and the stripping biogas slurry inlet 401 is located at the top of the H 2 S absorption tank 4; the acidification gas inlet 403 and the stripping biogas slurry inlet 403
  • a baffle plate assembly is arranged between 401, and the baffle plate assembly includes a plurality of baffle plates 405 that alternately extend from both sides of the H2S absorption pool 4 , so that the absorption liquid in the absorption pool 4 can be folded from top to bottom. flow by way of flow.
  • the baffle assembly includes a plurality of baffles 405 .
  • a plurality of baffles 405 are staggered and evenly distributed from top to bottom.
  • the first baffle plate is located at the highest position, and it extends from the side wall on the side of the blow-off biogas slurry inlet 401 to the opposite side wall;
  • the second baffle plate is located below the first baffle plate, and it extends from the opposite side wall to the blow-off
  • the side wall on the side of the biogas slurry inlet 401 extends;
  • the third baffle plate is located below the second baffle plate, and it extends from the side wall on the side of the blow-off biogas slurry inlet 401 to the opposite side wall.
  • the staggered arrangement of the plurality of baffles 405 can prolong the path of the biogas slurry after stripping, that is, the absorption liquid, in the H 2 S absorption tank 4 , thereby increasing the H 2 S released by the hydrolysis and acidification tank 1 and the biogas liquid stripping tank 3
  • the contact time of the generated biogas slurry after stripping and the absorption liquid can better absorb H 2 S in the acidified gas with high efficiency and energy saving.
  • the contact time between the H 2 S released by the hydrolysis and acidification tank 1 and the stripped biogas slurry produced by the biogas slurry stripping tank 3 in the H 2 S absorption tank 4 can be increased, so that the It can remove H 2 S from acidification gas in a good, efficient and energy-saving manner.
  • the method further includes the following steps: returning part of the sulfur-containing absorbing liquid produced in the H 2 S absorption tank 4 to the biogas slurry stripping tank 3, and discharging the other part of the sulfur-containing absorbing liquid to the outside ; Part of the desulfurized gas generated in the absorption tank 4 enters the methanogenic tank 2 to be used as a raw material for biogas production.
  • the H 2 S absorption tank 4 includes a sulfur-containing absorption liquid outlet 402 at the bottom end thereof, and the sulfur-containing absorption liquid outlet 402 is respectively connected with the reflux liquid inlet 306 of the biogas liquid stripping tank 3 and the outside. Connected.
  • the sulfur-containing absorbing liquid outlet 402 of the H 2 S absorption tank 4 is communicated with the reflux liquid inlet 306 of the biogas liquid stripping tank 3 .
  • the return of the liquid to the biogas slurry stripping tank 3 can prevent the total amount of liquid in the biogas liquid stripping tank 3 from decreasing significantly, which is beneficial to the stable operation of the system.
  • the sulfur-containing absorbing liquid outlet 402 of the H 2 S absorption tank 4 is communicated with the outside world.
  • sulfur-containing raw materials can be provided for subsequent fertilizer production, which is beneficial to improve the environmental performance of the system. and economic value.
  • Part of the desulfurized gas produced in the H 2 S absorption tank 4 enters the methanogenic tank 2 as a raw material for biogas production.
  • the air outlet 404 of the H 2 S absorption tank 4 is communicated with the return air inlet 204 of the methanogenic tank 2 through pipelines, so as to transport organic acids and H 2 etc. into the methanogenic tank 2. , as a feedstock for methanogenic bacteria to generate more biogas.
  • by recycling the desulfurized gas it is possible to avoid discharging the desulfurized gas to the atmosphere, which is beneficial to improve the environmental protection performance of the method.
  • the height difference between the return air inlet 204 and the liquid level is 0.2-2.0 meters. If the distance is too large, the H 2 S absorption tank 4 needs to provide a larger pressure, so that the H 2 S absorption tank 4 has to have a higher pressure bearing level, which is not conducive to reducing the cost. If the distance is too small, when the liquid level in the methane-producing tank 2 fluctuates, it is easy for the biogas to enter the H 2 S absorption tank 4 .
  • the sulfur-containing absorbing liquid is returned to avoid the obvious decrease of the total liquid in the biogas slurry stripping tank 3 , which is beneficial to the stable operation of the system;
  • Subsequent fertilizer production provides sulfur-containing raw materials; by passing part of the desulfurized gas generated in the H 2 S absorption tank 4 into the methane-producing tank 2 , the desulfurized gas can be used as a raw material for biogas production, which is beneficial to increase the output of biogas.
  • the method uses the microporous aeration head 303 disposed at the bottom of the biogas slurry stripping tank 3 to remove ammonia nitrogen and carbon dioxide from the biogas slurry entering the biogas slurry stripping tank 3 to obtain stripped biogas slurry.
  • ammonia nitrogen and carbon dioxide are removed from the biogas slurry entering the biogas slurry stripping tank 3 through the microporous aeration head 303, which can increase the gas-liquid contact area, improve the mass transfer efficiency and stripping effect, and help reduce the stripping energy. consumption.
  • the microporous aeration head 303 has the advantages of strong corrosion resistance, and the pores are not easily blocked, which is conducive to maintaining the stripping effect of the biogas slurry stripping tank for a long time.
  • the present invention also provides a system for treating sulfate organic wastewater, the system comprising: a hydrolysis acidification tank 1 , which is used to generate acidification gas and hydrolysis acidification liquid containing H2S ; H2S absorption Pool 4, which is connected with hydrolysis and acidification pool 1, so that acidified gas containing H 2 S enters H 2 S absorption pool 4; Methanogenic pool 2 is connected with hydrolysis acidification pool 1 so that the hydrolysis acidification liquid enters methane production pool 2 In the methane-producing pond 2, the hydrolyzed and acidified liquid is used to produce biogas slurry; and the biogas slurry stripping tank 3 is connected to the methane-producing pond 2 so that the biogas slurry enters the biogas slurry stripping tank 3, and the biogas slurry stripping tank 3 3.
  • a hydrolysis acidification tank 1 which is used to generate acidification gas and hydrolysis acidification liquid containing H2S
  • H2S absorption Pool 4 which is connected with hydrolysis and acidification pool
  • the biogas slurry stripping tank 3 is also connected with the H2S absorption tank 4 , so that part of the stripped biogas slurry enters
  • the H 2 S absorption tank 4 is used as an absorption liquid to absorb H 2 S in the acidified gas.
  • the methane-producing tank 2 can also produce biogas, and the biogas outlet 203 of the methane-producing tank 2 is directly connected to the biogas utilization device 7 through a pipeline. Due to the pre-desulfurization, the biogas produced by the methane-producing tank 2 has a low sulfur content, which greatly reduces the corrosion of equipment and pipelines during the direct utilization of biogas. Therefore, the biogas outlet 203 of the methane-producing tank 2 can be connected with the biogas utilization device 7 . Directly communicated through the pipeline. The biogas outlet 203 of the methane-producing tank 2 is directly connected to the biogas utilization device 7, and the biogas is directly utilized, that is, combustion or power generation.
  • the stripped biogas slurry produced by the biogas slurry stripping tank 3 can be used to absorb the H 2 S released by the hydrolysis and acidification tank 1, and the method does not need to use additional alkaline chemical reagents or desulfurization agents, which makes the method simple and economical , efficient and environmentally friendly.
  • the gas outlet 404 of the H 2 S absorption tank 4 is connected to the gas inlet 104 of the hydrolysis and acidification tank 1 , so as to input the partially desulfated gas into the hydrolysis and acidification tank 1 .
  • the hydrolysis and acidification pool 1 is also provided with a diversion device, which is used to make the liquid in the hydrolysis acidification pool 1 flow along the diversion device under the action of the desulfurized gas, so that the mixed liquid in the hydrolysis acidification pool 1 can be fully stirred. And accelerate the release of H 2 S.
  • the mixed solution in the hydrolysis and acidification tank 1 can be fully stirred and the release of H 2 S can be accelerated, which helps to reduce the energy consumption required for mixing and improve the desulfurization effect.
  • the gas outlet 404 of the H 2 S absorption tank 4 is also connected to the return gas inlet 204 of the methane-producing tank 2 , so as to input the partially desulfurized gas into the methane-producing tank 2 .
  • the sulfur-containing absorbing liquid outlet 402 of the H 2 S absorption tank 4 is also respectively connected with the reflux liquid inlet 306 of the biogas slurry stripping tank 3 and the outside, so as to input the sulfur-containing absorbing liquid to the biogas liquid stripping tank 3, Or discharge sulfur-containing absorbing liquid to the outside.
  • the total liquid in the biogas liquid stripping tank 3 can be prevented from being significantly decreased, which is beneficial to the stable operation of the system; It can provide sulfur-containing raw materials for subsequent fertilizer production.
  • the H 2 S absorption tank 4 is also provided with a baffle plate assembly, and the baffle plate assembly includes a plurality of baffle plates 405 that alternately extend from both sides of the H 2 S absorption tank, so that the absorption liquid can be removed from the H 2 S absorption tank. Flow in a top-to-bottom flow.
  • the contact time between the H 2 S released by the hydrolysis and acidification tank 1 and the stripped biogas slurry produced by the biogas slurry stripping tank 3 in the H 2 S absorption tank 4 can be increased, so as to improve the It can remove H 2 S from acidification gas in a good, efficient and energy-saving manner.
  • a microporous aeration head 303 is installed at the bottom of the biogas slurry stripping tank 3, and an air pump 8 is installed on the air supply pipeline of the microporous aeration head 303; They are respectively connected with the water outlet 6 and the waste gas treatment device 5 .
  • the diameter of the aeration bubbles of the microporous aeration head 303 is small and the bubbles diffuse evenly, which increases the gas-liquid contact area, thereby improving the mass transfer efficiency and blow-off effect, and is conducive to reducing energy consumption.
  • the microporous aeration head 303 has the advantages of strong corrosion resistance, and the pores are not easily blocked, which is conducive to maintaining the stripping effect of the biogas slurry stripping tank for a long time.
  • An air pump 8 is installed on the air supply pipeline of the microporous aeration head 303, and the air pump 8 is used to control the gas-liquid volume ratio of the stripping process between 200-2000. If the ratio is too large, the gas supply of the stripping gas will be large and the energy consumption will be too high; if the ratio is too small, the gas supply of the stripping gas will be too small, and the biogas slurry after stripping may also contain a large amount of gases such as CO 2 and NH 3 . , which is not conducive to the absorption of H 2 S by the biogas slurry after stripping in the H 2 S absorption tank 4 .
  • the system also includes a waste gas treatment device 5, and the stripping gas outlet 305 located at the top of the biogas slurry stripping tank 3 communicates with the stripping gas inlet 501 at the bottom end of the waste gas treatment device 5 to remove the stripping gas.
  • the generated gas is introduced into the waste gas treatment device 5;
  • the waste gas treatment device 5 is a packed tower type waste gas treatment device 5, which is provided with a filler 504; the waste gas treatment is also provided with a spray liquid outlet 503 at the bottom and a spray liquid at the top.
  • the inlet 505 and the purified gas outlet 502 at the top are examples of the purified gas outlet 502 at the top.
  • the waste gas treatment device 5 is used to purify the gas produced by stripping discharged from the biogas slurry stripping tank 3, and discharge the purified gas to the atmosphere.
  • the spray liquid enters from the spray liquid inlet 505 at the top and then sprays from top to bottom, and fully contacts with the gas generated by stripping to remove gases such as NH 3 , CO 2 and H 2 S, and the purified gas is discharged from the purified gas.
  • the discharge of the air port 502 is up to the standard, which is beneficial to further improve the environmental protection performance of the system.
  • the system further includes a water outlet tank 6 , and an outlet 302 of the stripped-off biogas slurry in the biogas slurry stripping tank 3 is communicated with the water outlet tank 6 .
  • the effluent tank 6 is used for the subsequent advanced treatment of the biogas slurry after stripping, so as to meet the standard discharge, which is beneficial to improve the environmental protection performance of the system.
  • microporous aeration head 303 by setting the microporous aeration head 303, it is beneficial to reduce the energy consumption of biogas liquid stripping; by setting the air pump 8, it is beneficial to control the gas-liquid volume ratio of the stripping process; by setting the water outlet 6 and the waste gas treatment device 5. It is beneficial to improve the environmental performance of the system.
  • the system further includes an automatic control mechanism, the automatic control mechanism includes: a sulfate and sulfide analyzer 10, a biogas composition analyzer 11 and a controller 12, the controller 12 is respectively connected with the sulfate and sulfide analyzer 10,
  • the biogas composition analyzer 11 is electrically connected; the sulfate and sulfide analyzer 10 is arranged on the pipeline connecting the hydrolysis acidification tank 1 and the methane-producing tank 2 to analyze the hydrolysis acidification liquid output by the hydrolysis acidification tank 1; the biogas composition
  • the analyzer 11 is arranged on the methane-producing pond 2 and communicates with the interior of the methane-producing pond 2 to analyze the biogas produced in the methane-producing pond 2;
  • the controller 12 is based on the sulfate and sulfide analyzer 10 and the biogas composition analyzer.
  • the real-time data obtained at 11 automatically controls the flow rate of the air pump 8 and the flow rate of the desulfurized
  • use the biogas composition analyzer 11 to analyze the biogas produced in the methane-producing tank 2; use the sulfate and sulfide analyzer 10 to analyze the hydrolyzed and acidified liquid output from the hydrolysis and acidification tank 1; use the controller 12
  • the real-time data obtained by the biogas composition analyzer 11 and the sulfate and sulfide analyzer 10 are obtained respectively, and according to the real-time data, the flow of the air entering the biogas slurry stripping tank 3 and the flow rate of the desulfurized gas entering the hydrolysis and acidification tank 1 are automatically controlled. flow.
  • the sulfate and sulfide analyzer 10 is arranged on the pipeline connecting the hydrolysis acidification liquid outlet 102 of the hydrolysis acidification tank 1 and the hydrolysis acidification liquid inlet 201 of the methane-producing tank 2, and the biogas composition analyzer 11 is arranged on the pipeline.
  • the top of the methanogenesis tank 2 is in communication with its interior.
  • the sulfate and sulfide analyzer 10 is used to monitor the desulfurization effect in the hydrolysis-acidification tank 1 in real time.
  • the biogas composition analyzer 11 is used to monitor the composition of the biogas produced by the methanogen pond 2 in real time.
  • the controller 12 can also understand the operating conditions of the system by analyzing the collected data.
  • the flow of the air entering the biogas slurry stripping tank 3 through the air pump 8 and the anti-corrosion air pump can be adjusted.
  • the flow rate of the desulfurized gas entering the hydrolysis and acidification tank 1 is beneficial to ensure the efficient and normal operation of the system.
  • the sulfate organic waste water enters the hydrolysis acidification tank 1 through the sulfate organic waste water inlet 101 at a flow rate of 35 liters/min, and the waste water undergoes hydrolysis acidification and sulfate reduction reaction in the hydrolysis acidification tank 1 .
  • S acidification gas of volatile organic acids and other sulfides, and hydrolyzed acidification liquid after desulfurization.
  • the acidified gas containing H2S enters the H2S absorption tank 4 through the acidified gas outlet 103 of the hydrolysis acidification tank 1 , the gas delivery pipeline and the acidified gas inlet 403 of the H2S absorption tank 4 to carry out the H2S removal purification. .
  • the desulfurized hydrolyzed and acidified liquid produced in the hydrolysis and acidification tank 1 enters the methane-producing tank 2 through the hydrolyzed and acidified liquid outlet 102 of the hydrolyzed and acidified tank 1 , the connecting pipeline and the hydrolyzed and acidified liquid inlet 201 of the methane-producing tank 2 .
  • Biogas slurry and biogas whose main component is methane are produced by the action of methanogenic bacteria in the methanogenic pond 2 .
  • the biogas enters the biogas utilization device 7 through the biogas outlet 203 and the pipeline of the methane-producing tank 2 for direct utilization, that is, combustion or power generation.
  • the biogas slurry produced in the methane-producing tank 2 enters the biogas slurry stripping tank 3 through the biogas slurry outlet 202 of the methane-producing tank 2 , the connecting pipeline and the biogas slurry inlet 301 of the biogas slurry stripping tank 3 for air aeration.
  • a microporous aeration head 303 is installed at the bottom of the biogas slurry stripping tank 3 , and an air pump 8 is installed on the air supply pipeline of the microporous aeration head 303 .
  • the microporous aeration head 303 is used to strip dissolved gases such as CO 2 and NH 3 in the biogas slurry, so that the pH value of the stripped biogas slurry rises to 9.9.
  • the stripping biogas slurry outlet 302 and the pipeline of the liquid stripping tank 3 enter the effluent tank 6 for subsequent advanced treatment and finally discharge up to the standard.
  • the other 1/2 of the stripped biogas slurry enters H 2 S through the stripped biogas slurry reflux outlet 304 of the biogas stripping tank 3 , the connecting pipeline and the stripped biogas slurry inlet 401 of the H 2 S absorption tank 4
  • the absorption tank 4 is used to absorb the H 2 S produced by the hydrolysis and acidification tank 1 .
  • a part of the sulfur-containing absorption liquid produced by the H 2 S absorption tank 4 is discharged to the outside through the sulfur-containing absorption liquid outlet 402 for subsequent fertilizer production, and the other part is discharged through the sulfur-containing absorption liquid outlet 402 , pipelines and biogas slurry stripping tank 3
  • the backflow inlet 306 of the backflow is returned to the biogas slurry stripping tank 3.
  • the desulfurized gas stirs the mixed solution in the hydrolysis and acidification tank 1 by means of the deflector 105 to promote the release of H 2 S in the acid-producing phase and the conversion of sulfur ions to H 2 S.
  • the baffle 105 can control the flow state, improve the stirring effect and save energy.
  • the desulfurized gas produced by another part of the H 2 S absorption tank 4 is returned to the methane-producing tank 2 through the gas outlet 404, the pipeline and the return air inlet 204 of the methane-producing pond 2, for providing the hydrogen raw material for the methane-producing pond 2, wherein
  • the depth of the return air inlet 204 is 0.2 meters.
  • the gas produced by the biogas slurry stripping tank 3 is discharged to the waste gas treatment device 5 for purification treatment, and the gases such as NH 3 , CO 2 and H 2 S are removed, and the purified gas is discharged up to the standard.

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Abstract

本申请提供了一种处理硫酸盐有机废水的方法和系统，该方法包括以下步骤：使水解酸化池产生的含有H2S的酸化气进入H2S吸收池；使水解酸化池产生的水解酸化液进入产甲烷池产生沼气和沼液；使沼液进入沼液吹脱池进行氨氮和二氧化碳脱除，获得吹脱后的沼液；使部分吹脱后的沼液进入H2S吸收池作为吸收液吸收酸化气中的H2S。该方法能够利用沼液吹脱池产生的吹脱后的沼液吸收水解酸化池释放的H2S，由于无需使用额外的碱性化学试剂或生物添加剂，使得该方法简单、经济、高效且环保。

Description

处理硫酸盐有机废水的方法和系统
相关申请的交叉引用
本申请要求享有于2020年10月19日提交的名称为“处理硫酸盐有机废水的方法和系统”的中国专利申请CN202011120418.8的优先权，该申请的全部内容通过引用并入本文中。
技术领域
本发明涉及一种处理硫酸盐有机废水的方法和系统，属于废水处理技术领域。
背景技术
一些食品生产废水、医药废水、造纸废水、皮革废水以及养殖废水中含有较高浓度的硫酸盐。由于这些废水往往同时含有高浓度的有机物，因此通常采用厌氧技术对其进行处理。
在采用厌氧技术对硫酸盐有机废水进行处理时，若有机物浓度和硫酸盐浓度的比值较小，系统中的硫酸盐还原菌会与产甲烷菌产生基质竞争，对产甲烷菌产生抑制作用。此外，还原硫酸盐生成的溶解性硫化物会对产甲烷菌产生毒害作用。上述负面作用会对厌氧消化过程产生不利影响，严重时会导致系统无法正常运行。
例如，中国专利CN108821429A(公开日期：2018-11-16)公开了一种硫酸盐废水处理的装置系统及其处理方法，该装置系统包括厌氧反应单元、吹脱单元、吸收单元、生物脱硫单元和气体存储单元。由于该处理方法采用单相厌氧法，无法避免H 2S对产甲烷菌的毒害作用以及对产甲烷反应的抑制作用，使得厌氧处理效果欠佳。
采用两相厌氧法将硫酸盐还原作用控制在产酸阶段并与产甲烷作用分开可以解决上述问题。一方面，同时进行硫酸盐还原和产酸不会对产酸过程产生负面影响；另一方面，产酸相反应器处于弱酸性状态，生成的硫化物主要以H 2S的形式存在，有利于去除硫化物。此外，硫化物不与产甲烷菌直接接触将不会对产甲烷菌产生毒害作用，有利于后续的产甲烷反应。同时，预先去除H 2S后，后续形 成的沼气中H 2S含量较低，有利于不经脱硫净化直接利用沼气。
然而，现有技术中，不论是单相厌氧法还是两相厌氧法中的H 2S脱除工艺都较为复杂，涉及添加额外的碱性化学试剂或脱硫剂，造成现有的H 2S脱除工艺难度大、成本高或效率低下，且会造成污染。
例如，上述中国专利CN108821429A(公开日期：2018-11-16)中，厌氧反应单元产生的含硫沼气和吹脱单元产生含硫吹脱气进入吸收单元进行处理，产生硫化物吸收液和净化后的沼气。硫化物吸收液最终进入生物脱硫单元，通过曝气进行生物硫氧化以获取单质硫和清液。其H 2S脱除工艺能耗高、工艺复杂，且需要添加额外的碱性化学试剂不利于降低工艺成本，同时生物脱硫的条件也较难控制。另外，中国专利CN105776525A(公开日期：2016-07-20)公开了一种一体式两相厌氧脱硫反应器及其废水处理方法，该反应器包括一体式的脱硫反应池和产甲烷反应池。硫酸盐废水依次进入脱硫反应池和产甲烷反应池进行处理，脱硫反应池和产甲烷反应池仅通过隔墙隔开并通过出水堰连通。脱硫反应池的底部设置有曝气头，并使用收集的脱硫沼气对脱硫反应池进行曝气。然而，由于该反应器将脱硫反应池和产甲烷反应池产生的气体通过沼气收集管合并收集，并通过专门设置的尾气处理单元进行统一的脱硫处理，这样不仅增加了气体的处理量，而且在脱除H 2S的同时也要处理H 2、CO 2和一些挥发性有机酸，增大了H 2S脱除工艺的难度和成本。
发明内容
针对上述现有技术中的问题，本申请提出了一种处理硫酸盐有机废水的方法和系统，其能够利用沼液吹脱池产生的吹脱后的沼液吸收水解酸化池释放的H 2S，该方法无需使用额外的碱性化学试剂或脱硫剂，使得该方法简单、经济、高效且环保。
为实现上述目的，本发明提供了一种处理硫酸盐有机废水的方法，该方法包括以下步骤：使水解酸化池产生的含有H 2S的酸化气进入H 2S吸收池；使水解酸化池产生的水解酸化液进入产甲烷池产生沼气和沼液；使沼液进入沼液吹脱池进行氨氮和二氧化碳脱除，获得吹脱后的沼液；使部分吹脱后的沼液进入H 2S吸收池作为吸收液吸收酸化气中的H 2S。
该方法还包括以下步骤：使H 2S吸收池中的吸收液沿从上至下方向以折流的 方式进行流动，吸收酸化气中的H 2S，产生含硫吸收液；使进入H 2S吸收池的含有H 2S的酸化气沿从下至上方向进行流动，脱硫后形成脱硫酸化气；其中，吸收液和含有H 2S的酸化气的流动方向相反，以使含有H 2S的酸化气与吸收液能够充分接触。
该方法还包括以下步骤：使H 2S吸收池中产生的部分脱硫酸化气进入水解酸化池；使水解酸化池中的液体在脱硫酸化气的作用下沿导流装置流动，以使水解酸化池中的混合液得到充分的搅拌并加速H 2S的释放。
该方法还包括以下步骤：使H 2S吸收池中产生的部分含硫吸收液回流至沼液吹脱池；使H 2S吸收池中产生的部分脱硫酸化气进入产甲烷池，以作为沼气生产的原料。
该方法还包括采用设置在沼液吹脱池底部的微孔曝气头对进入沼液吹脱池的沼液进行氨氮和二氧化碳脱除，获得吹脱后的沼液。
本发明还提供了一种处理硫酸盐有机废水的系统，该系统包括：水解酸化池，其用于产生含有H 2S的酸化气和水解酸化液；H 2S吸收池，其与所述水解酸化池相连，以使所述含有H 2S的酸化气进入所述H 2S吸收池中；产甲烷池，其与所述水解酸化池相连以使所述水解酸化液进入所述产甲烷池中，所述产甲烷池利用进入其中的所述水解酸化液生产沼气和沼液；以及沼液吹脱池，其与所述产甲烷池相连以使所述沼液进入所述沼液吹脱池中，所述沼液吹脱池对进入其中的沼液进行氨氮和二氧化碳脱除，获得吹脱后的沼液；其中，所述沼液吹脱池还与所述H 2S吸收池相连，从而使部分所述吹脱后的沼液进入所述H 2S吸收池作为吸收液吸收酸化气中的H 2S。
所述H 2S吸收池的出气口与所述水解酸化池的进气口相连，以向所述水解酸化池中输入部分脱硫酸化气；所述水解酸化池中还设置有导流装置，其用于使所述水解酸化池中的液体在脱硫酸化气的作用下沿导流装置流动，以使所述水解酸化池中的混合液得到充分的搅拌并加速H 2S的释放。
所述H 2S吸收池的出气口还与所述产甲烷池的进气口相连，以向所述产甲烷池输入部分脱硫酸化气。
所述H 2S吸收池中还设置有折流板组件，所述折流板组件包括多个交替从所述H 2S吸收池的两侧延伸出的折流板，从而使吸收液沿从上至下方向以折流的方式进行流动。
所述H 2S吸收池的含硫吸收液出口还分别与所述沼液吹脱池的回流进液口以及外界相连，以向所述沼液吹脱池输入含硫吸收液，或向外界排出含硫吸收液。
所述沼液吹脱池的底部安装有微孔曝气头，所述微孔曝气头的供气管路上安装有空气泵；所述沼液吹脱池还分别与出水池及废气处理装置相连。
该系统还包括自动控制机构，所述自动控制机构包括：硫酸盐和硫化物分析仪、沼气成分分析仪和控制器，所述控制器分别与所述硫酸盐和硫化物分析仪、所述沼气成分分析仪电连接；所述硫酸盐和硫化物分析仪设置在连接所述水解酸化池和所述产甲烷池之间的管路上，以对水解酸化池输出的水解酸化液进行分析；所述沼气成分分析仪设置在所述产甲烷池上并与所述产甲烷池内部连通，以对产甲烷池中产生的沼气进行分析；所述控制器根据所述硫酸盐和硫化物分析仪和所述沼气成分分析仪获得的实时数据自动控制空气泵的流量和进入水解酸化池的脱硫酸化气的流量。
本发明由于采取以上技术方案，其具有以下优点：
1、本发明能够利用沼液吹脱池产生的吹脱后的沼液吸收水解酸化池释放的H 2S，由于无需使用额外的碱性化学试剂或脱硫剂，使得该方法简单、经济、高效且环保。
2、本发明通过设置导流装置，能够使水解酸化池中的混合液得到充分的搅拌并加速H 2S的释放，有助于提高水解酸化液的脱硫效果。
3、本发明通过使用折流板组件，能够使得水解酸化池释放的H 2S与沼液吹脱池产生的吹脱后的沼液在H 2S吸收池内充分接触，以更好地、高效节能地脱除酸化气中的H 2S。
4、本发明通过使部分脱硫酸化气进入产甲烷池，能够为沼气生产提供更多的原料，有利于提高沼气的产量。
5、本发明通过使部分含硫吸收液回流至沼液吹脱池，能够避免沼液吹脱池内液体总量明显下降，有利于系统的稳定运行。
6、本发明通过收集排至外界的含硫吸收液，能够为后续的化肥生产提供含硫原料。
7、本发明的控制器能够根据硫酸盐和硫化物分析仪以及沼气成分分析仪实时获取的数据，调节经空气泵进入沼液吹脱池的空气的流量以及经防腐气泵进入水解酸化池的脱硫酸化气的流量，有利于保证系统的高效、正常运行。
8、本发明通过设置微孔曝气头，有利于提高沼液中氨氮和二氧化碳的吹脱效果、降低沼液吹脱的能耗。
9、本发明通过设置出水池及废气处理装置，有利于提高系统的环保性能。
本发明的其它特征和优点将在随后的说明书中阐述，并且，部分的从说明书中变得显而易见，或者通过实施本发明而了解。本发明的目的和其他优点可通过在说明书、权利要求书以及附图中所特别指出的结构来实现和获得。
附图说明
在下文中将基于实施例并参考附图来对本发明进行更详细的描述。
图1显示了本发明的处理硫酸盐有机废水的系统的结构示意图；
图2显示了本发明自动控制机构的结构示意图。
具体实施方式
下面将结合附图对本发明作进一步说明。
本发明提供了一种处理硫酸盐有机废水的方法，该方法包括以下步骤：使水解酸化池1产生的含有H 2S的酸化气进入H 2S吸收池4；使水解酸化池1产生的水解酸化液进入产甲烷池2产生沼气和沼液；使沼液进入沼液吹脱池3进行氨氮和二氧化碳脱除，获得吹脱后的沼液；使部分吹脱后的沼液进入H 2S吸收池4作为吸收液吸收酸化气中的H 2S。
硫酸盐有机废水通过水解酸化池1的硫酸盐有机废水进口101进入水解酸化池1。硫酸盐有机废水在水解酸化池1中发酵细菌、产酸细菌以及硫酸盐还原菌的作用下进行水解酸化和硫酸盐还原反应，使废水中的硫酸盐转化为H 2S和其它硫化物，并将废水中的有机物转化为有机酸、H 2等。水解酸化池1产生的含有H 2S的酸化气通过气体输送管道从水解酸化池1引出经H 2S吸收池4的酸化气进气口403进入H 2S吸收池4，有利于避免硫化物进入产甲烷池2，继而有利于缓解硫化物对产甲烷的负面影响。
水解酸化池1产生的脱硫后的水解酸化液经水解酸化池1的水解酸化液出口102、连接管路及产甲烷池2的水解酸化液进口201进入产甲烷池2，该过程依靠重力作用。水解酸化液在产甲烷池2中产甲烷细菌的作用下，其中的有机酸等转化为沼气，沼气通过管路引出。另外，由于预先脱硫，产甲烷池2产生的沼气含 硫量较低，极大地降低了沼气直接利用过程中对设备和管路的腐蚀。
产甲烷池2产生的沼液在重力作用下，经产甲烷池2的沼液出口202、连接管路及沼液吹脱池3的沼液进口301进入沼液吹脱池3。通过曝气吹脱沼液中的CO 2和NH 3等气体，使沼液的pH升高至9.0-10.0形成吹脱后的沼液。
部分吹脱后的沼液经沼液吹脱池3的吹脱沼液回流出液口304、连接管路及H 2S吸收池4的吹脱沼液进口401进入H 2S吸收池4，其中引入H 2S吸收池4的吹脱后的沼液占吹脱后沼液总量的1/6-2/3。
在H 2S吸收池4中，吹脱后的碱性沼液与含有H 2S的酸化气相接触通过酸碱反应对H 2S进行吸收、净化，产生含硫吸收液和脱硫酸化气，其中，部分含硫吸收液排至外界以备后续的化肥生产。
本实施方式能够利用沼液吹脱池3产生的吹脱后的沼液吸收水解酸化池1释放的H 2S，由于无需使用额外的碱性化学试剂或脱硫剂，使得该方法简单、经济、高效且环保。
可选地，该方法还包括以下步骤：使H 2S吸收池4中产生的部分脱硫酸化气进入水解酸化池1；使水解酸化池1中的液体在脱硫酸化气的作用下沿导流装置流动，以使水解酸化池1中的混合液得到充分的搅拌并加速H 2S的释放。
如图1所示，H 2S吸收池4还包括位于其顶端的出气口404，出气口404与水解酸化池1的进气口104通过管路连通，且出气口404与进气口104的管路上设置有防腐气泵9。
采用防腐气泵9可以减缓脱硫酸化气对气泵的腐蚀。防腐气泵9将H 2S吸收池4产生的部分脱硫酸化气泵入水解酸化池1以更好地混合水解酸化池1中的混合液，一方面使硫酸盐有机废水与发酵细菌、产酸细菌以及硫酸盐还原菌充分接触，另一方面促进H 2S气体由液相至气相的转移以及溶液中其它硫化物至H 2S的转化，且使得进入产甲烷池2的水解酸化液的pH值较高，有助于沼气的生成。
为了在提高混合效果的同时加速H 2S的释放，在水解酸化池1中设置了导流装置。可选地，导流装置为导流板105。导流板105包括主体和两个侧翼，主体竖直设置，两个侧翼分别连接在主体的顶端和底端且与主体的夹角均为钝角；进气口104与液面间的高度差为0.5-5.5米。
导流板105的主体竖直设置，顶部侧翼斜向上延伸，底部侧翼斜向下延伸，水解酸化池1中的液体在脱硫酸化气的作用下沿导流板105从下往上流动，以使 水解酸化池1中的混合液得到充分的混合并加速H 2S释放，有助于降低混合所需能耗并提高脱硫效果。
进气口104与液面间的高度差为0.5-5.5米。该距离过大，不利于降低防腐气泵9的能耗；该距离过小，不利于混合液的充分搅拌。
导流装置能够协助脱硫酸化气吹脱水解酸化池1中的H 2S，进而使水解酸化池1内液体中的硫离子不断转化成H 2S，从而达到高效脱硫的目的。
本实施方式通过设置导流装置，能够使水解酸化池1中的混合液得到充分的搅拌并加速H 2S释放，有助于降低混合所需的能耗、提高脱硫效果。
可选地，该方法还包括以下步骤：使H 2S吸收池4中的吸收液沿从上至下方向以折流的方式进行流动，吸收酸化气中的H 2S，产生含硫吸收液；使进入H 2S吸收池4的含有H 2S的酸化气沿从下至上方向进行流动，脱硫后形成脱硫酸化气；其中，吸收液和含有H 2S的酸化气的流动方向相反，以使含有H 2S的酸化气与吸收液能够充分接触。
如图1所示，酸化气进气口403位于H 2S吸收池4的底部，吹脱沼液进口401位于H 2S吸收池4的顶部；酸化气进气口403与吹脱沼液进口401之间设置有折流板组件，折流板组件包括多个交替从H 2S吸收池4的两侧延伸出的折流板405以使吸收池4中的吸收液以从上至下折流的方式进行流动。
折流板组件包括多个折流板405。可选地，多个折流板405交错设置，从上到下均匀分布。第一折流板位于最高处，其从吹脱沼液进口401侧的侧壁向相对的侧壁延伸；第二折流板位于第一折流板下方，其从相对的侧壁向吹脱沼液进口401侧的侧壁延伸；第三折流板位于第二折流板的下方，其从吹脱沼液进口401侧的侧壁向相对的侧壁延伸。多个折流板405交错设置能够延长吹脱后的沼液，即吸收液，在H 2S吸收池4内的路径，从而增加水解酸化池1释放的H 2S与沼液吹脱池3产生的吹脱后的沼液及吸收液的接触时间，以更好地、高效节能地吸收酸化气中的H 2S。
本实施方式通过使用折流板组件，能够增加水解酸化池1释放的H 2S与沼液吹脱池3产生的吹脱后的沼液在H 2S吸收池4内的接触时间，以更好地、高效节能地脱除酸化气中的H 2S。
可选地，该方法还包括以下步骤：使H 2S吸收池4中产生的部分含硫吸收液回流至沼液吹脱池3，另一部分含硫吸收液则排放至外界；使H 2S吸收池4中产 生的部分脱硫酸化气进入产甲烷池2，以作为沼气生产的原料。
H 2S吸收池4中产生的部分含硫吸收液回流至沼液吹脱池3，另一部分含硫吸收液排放至外界以备后续利用。可选地，如图1所示，H 2S吸收池4包括位于其底端的含硫吸收液出口402，含硫吸收液出口402分别与沼液吹脱池3的回流进液口306和外界连通。
H 2S吸收池4的含硫吸收液出口402与沼液吹脱池3的回流进液口306连通，在吹脱后的沼液大量流入H 2S吸收池4的情况下，含硫吸收液回流至沼液吹脱池3能够避免沼液吹脱池3内液体总量明显下降，有利于系统的稳定运行。
H 2S吸收池4的含硫吸收液出口402与外界连通，通过收集H 2S吸收池4生成的含硫吸收液，能够为后续的化肥生产提供含硫原料，有利于提高系统的环保性能和经济价值。
H 2S吸收池4中产生的部分脱硫酸化气进入产甲烷池2，以作为沼气生产的原料。可选地，如图1所示，H 2S吸收池4的出气口404与产甲烷池2的回流进气口204通过管路连通，以向产甲烷池2内输送有机酸和H 2等，作为产甲烷细菌的原料以使其生成更多的沼气。同时，通过回收利用脱硫酸化气，能够避免将脱硫酸化气排放至大气，有利于提高方法的环保性能。
可选地，回流进气口204与液面间的高度差为0.2-2.0米。该距离过大，需要H 2S吸收池4提供更大的压力，使得H 2S吸收池4不得不具有更高的承压水平，不利于降低成本。该距离过小，当产甲烷池2中的液位波动时，容易使沼气进入H 2S吸收池4。
本实施方式通过含硫吸收液回流，能够避免沼液吹脱池3内液体总量明显下降，有利于系统的稳定运行；通过收集剩余H 2S吸收池4生成的含硫吸收液，能够为后续的化肥生产提供含硫原料；通过使H 2S吸收池4中产生的部分脱硫酸化气进入产甲烷池2，能够使脱硫酸化气作为沼气生产的原料，有利于提高沼气的产量。
可选地，该方法采用设置在沼液吹脱池3底部的微孔曝气头303对进入沼液吹脱池3的沼液进行氨氮和二氧化碳脱除，以获得吹脱后的沼液。
本实施方式通过微孔曝气头303对进入沼液吹脱池3的沼液进行氨氮和二氧化碳脱除，可以增大气液接触面积，提高传质效率和吹脱效果，有利于降低吹脱能耗。此外，微孔曝气头303具有耐腐蚀性强，孔眼不易堵塞的优点，有利于长 期维持沼液吹脱池的吹脱效果。
如图1所示，本发明还提供了一种处理硫酸盐有机废水的系统，该系统包括：水解酸化池1，其用于产生含有H 2S的酸化气和水解酸化液；H 2S吸收池4，其与水解酸化池1相连，以使含有H 2S的酸化气进入H 2S吸收池4；产甲烷池2，其与水解酸化池1相连以使水解酸化液进入产甲烷池2中，产甲烷池2利用进入其中的水解酸化液生产沼液；以及沼液吹脱池3，其与产甲烷池2相连以使沼液进入沼液吹脱池3中，沼液吹脱池3对进入其中的沼液进行氨氮和二氧化碳脱除，获得吹脱后的沼液；其中，沼液吹脱池3还与H 2S吸收池4相连，从而使部分吹脱后的沼液进入H 2S吸收池4作为吸收液吸收酸化气中的H 2S。
可选地，产甲烷池2还可生产沼气，产甲烷池2的沼气出气口203与沼气利用装置7通过管路直接连通。由于预先脱硫，产甲烷池2产生的沼气含硫量较低，极大地降低了沼气直接利用过程中对设备和管路的腐蚀，因此产甲烷池2的沼气出气口203能够与沼气利用装置7通过管路直接连通。产甲烷池2的沼气出气口203与沼气利用装置7直接连通，对沼气进行直接利用即燃烧或发电。
本实施方式能够利用沼液吹脱池3产生的吹脱后的沼液吸收水解酸化池1释放的H 2S，该方法无需使用额外的碱性化学试剂或脱硫剂，使得该方法简单、经济、高效且环保。
可选地，H 2S吸收池4的出气口404与水解酸化池1的进气口104相连，以向水解酸化池1中输入部分脱硫酸化气。水解酸化池1中还设置有导流装置，其用于使水解酸化池1中的液体在脱硫酸化气的作用下沿导流装置流动，以使水解酸化池1中的混合液得到充分的搅拌并加速H 2S的释放。
本实施方式通过设置导流装置，能够使水解酸化池1中的混合液得到充分的搅拌并加速H 2S的释放，有助于降低混合所需的能耗并提高脱硫效果。
可选地，H 2S吸收池4的出气口404还与产甲烷池2的回流进气口204相连，以向产甲烷池2输入部分脱硫酸化气。
本实施方式通过使部分脱硫酸化气进入产甲烷池2，能够为沼气生产提供更多的原料，有利于提高沼气的产量。
可选地，H 2S吸收池4的含硫吸收液出口402还分别与沼液吹脱池3的回流进液口306以及外界相连，以向沼液吹脱池3输入含硫吸收液，或向外界排出含硫吸收液。
本实施方式通过使部分含硫吸收液回流至沼液吹脱池3，能够避免沼液吹脱池3内液体总量明显下降，有利于系统的稳定运行；通过收集排至外界的含硫吸收液，能够为后续的化肥生产提供含硫原料。
可选地，H 2S吸收池4中还设置有折流板组件，折流板组件包括多个交替从H 2S吸收池的两侧延伸出的折流板405，从而使吸收液以从上至下折流的方式进行流动。
本实施方式通过设置折流板组件，能够增加水解酸化池1释放的H 2S与沼液吹脱池3产生的吹脱后的沼液在H 2S吸收池4内的接触时间，以更好地、高效节能地脱除酸化气中的H 2S。
可选地，如图1所示，沼液吹脱池3的底部安装有微孔曝气头303，微孔曝气头303的供气管路上安装有空气泵8；沼液吹脱池3还分别与出水池6及废气处理装置5相连。
微孔曝气头303的曝气气泡直径小、气泡扩散均匀，使气液接触面积增大，进而提高传质效率和吹脱效果，且有利于降低能耗。此外，微孔曝气头303具有耐腐蚀性强，孔眼不易堵塞的优点，有利于长期维持沼液吹脱池的吹脱效果。
微孔曝气头303的供气管路上安装有空气泵8，空气泵8用于将吹脱过程的气液体积比控制在200-2000之间。该比值过大，吹脱气体供气量大，能耗过高；而该比值过小，吹脱气体供气量过小，吹脱后的沼液可能还包含大量CO 2和NH 3等气体，不利于H 2S吸收池4中吹脱后的沼液对H 2S的吸收。
如图1所示，所述系统还包括废气处理装置5，位于沼液吹脱池3顶部的吹脱气出气口305与废气处理装置5底端的吹脱气进气口501连通以将吹脱产生的气体引入废气处理装置5；废气处理装置5为填料塔式废气处理装置5，其内设置有填料504；废气处理上还开设有位于底部的喷淋液出口503、位于顶部的喷淋液进口505以及位于顶端的净化气出气口502。
废气处理装置5用于净化沼液吹脱池3排出的吹脱产生的气体，并将净化后的气体排至大气环境中。喷淋液从顶部的喷淋液进口505进入后从上往下喷洒，与吹脱产生的气体充分接触，以去除NH 3、CO 2和H 2S等气体，净化后的气体从净化气出气口502达标排放，有利于进一步地提高系统的环保性能。
如图1所示，所述系统还包括出水池6，沼液吹脱池3的吹脱沼液出口302与出水池6连通。出水池6用于对吹脱后的沼液进行后续的深度处理，以达标排 放，有利于提高系统的环保性能。
本实施方式通过设置微孔曝气头303，有利于降低沼液吹脱的能耗；通过设置空气泵8，有利于控制吹脱过程的气液体积比；通过设置出水池6及废气处理装置5，有利于提高系统的环保性能。
可选地，该系统还包括自动控制机构，自动控制机构包括：硫酸盐和硫化物分析仪10、沼气成分分析仪11和控制器12，控制器12分别与硫酸盐和硫化物分析仪10、沼气成分分析仪11电连接；硫酸盐和硫化物分析仪10设置在连接水解酸化池1和产甲烷池2之间的管路上，以对水解酸化池1输出的水解酸化液进行分析；沼气成分分析仪11设置在产甲烷池2上并与产甲烷池2的内部连通，以对产甲烷池2中产生的沼气进行分析；控制器12根据硫酸盐和硫化物分析仪10和沼气成分分析仪11获得的实时数据自动控制空气泵8的流量和进入水解酸化池1的脱硫酸化气的流量。
如图2所示，使用沼气成分分析仪11对产甲烷池2中产生的沼气进行分析；使用硫酸盐和硫化物分析仪10对水解酸化池1输出的水解酸化液进行分析；使用控制器12分别获取沼气成分分析仪11和硫酸盐和硫化物分析仪10所获得的实时数据，并根据实时数据自动控制进入沼液吹脱池3的空气的流量和进入水解酸化池1的脱硫酸化气的流量。
硫酸盐和硫化物分析仪10设置在连接水解酸化池1的水解酸化液出口102和产甲烷池2的水解酸化液进口201之间的输送水解酸化液的管路上，沼气成分分析仪11设置在产甲烷池2的顶部并与其的内部连通。
硫酸盐和硫化物分析仪10用于实时监控水解酸化池1中的脱硫效果。沼气成分分析仪11用于实时监测产甲烷池2生产的沼气的成分。通过使用硫酸盐和硫化物分析仪10和沼气成分分析仪11能够实时了解系统的运行状况，并通过控制器12对防腐气泵9及空气泵8的流量进行调节，以保证系统的高效、正常运行。
可选地，控制器12还能够通过分析收集的数据了解系统的运行状况。
本实施方式通过设置自动控制机构，能够根据硫酸盐和硫化物分析仪10以及沼气成分分析仪11实时获取的数据，调节经空气泵8进入沼液吹脱池3的空气的流量以及经防腐气泵9进入水解酸化池1的脱硫酸化气的流量，有利于保证系统的高效、正常运行。
实施例一
下面以处理量为50立方米/天为例，具体说明本发明的实施过程。
硫酸盐有机废水以35升/分钟的流速通过硫酸盐有机废水进口101进入水解酸化池1，废水在水解酸化池1内进行水解酸化和硫酸盐还原反应，产生含有CO 2、H 2、H 2S、挥发性有机酸和其它硫化物等的酸化气和脱硫后的水解酸化液。含有H 2S的酸化气通过水解酸化池1的酸化气出气口103、气体输送管道以及H 2S吸收池4的酸化气进气口403进入H 2S吸收池4以进行脱H 2S净化。
水解酸化池1产生的脱硫后的水解酸化液经水解酸化池1的水解酸化液出口102、连接管路及产甲烷池2的水解酸化液进口201进入产甲烷池2。在产甲烷池2内借助产甲烷菌的作用，产生沼液和主要成分为甲烷的沼气。沼气经产甲烷池2的沼气出气口203、管路进入沼气利用装置7以直接利用，即燃烧或发电。
产甲烷池2产生的沼液经产甲烷池2的沼液出口202、连接管路及沼液吹脱池3的沼液进口301进入沼液吹脱池3以进行空气曝气。沼液吹脱池3的底部安装有微孔曝气头303，微孔曝气头303的供气管路上安装有空气泵8，通过控制空气泵8的气量使气液比为800。微孔曝气头303用于吹脱沼液中的CO 2和NH 3等溶解性气体，使吹脱后的沼液的pH值上升至9.9。1/2的吹脱后的沼液经沼液吹脱池3的吹脱沼液出口302、管路进入出水池6以进行后续的深度处理并在最终达标排放。另外1/2的吹脱后的沼液经沼液吹脱池3的吹脱沼液回流出液口304、连接管路及H 2S吸收池4的吹脱沼液进口401进入H 2S吸收池4，用于吸收水解酸化池1产生的H 2S。
一部分H 2S吸收池4产生的含硫吸收液经含硫吸收液出口402排放至外界以备后续的化肥生产，另一部分则经含硫吸收液出口402、管路以及沼液吹脱池3的回流进液口306回流至沼液吹脱池3。
一部分H 2S吸收池4产生的脱硫酸化气经出气口404、防腐气泵9以及水解酸化池1的进气口104进入水解酸化池1，其中进气口104的深度为1.5米。脱硫酸化气借助导流板105对水解酸化池1中的混合液进行搅拌，促进产酸相中H 2S的释放以及硫离子至H 2S的转化。导流板105可以对流态进行控制，提高搅拌效果并节约能源。
另一部分H 2S吸收池4产生的脱硫酸化气经出气口404、管路以及产甲烷池2的回流进气口204回流至产甲烷池2，用于为产甲烷池2提供氢原料，其中回 流进气口204的深度为0.2米。
沼液吹脱池3吹脱产生的气体被排放至废气处理装置5以进行净化处理，去除其中的NH 3、CO 2和H 2S等气体，净化后的气体达标排放。
虽然本发明所公开的实施方式如上，但所述的内容只是为了便于理解本发明而采用的实施方式，并非用以限定本发明。任何本发明所属技术领域内的技术人员，在不脱离本发明所公开的精神和范围的前提下，可以在实施的形式上及细节上作任何的修改与变化，但本发明的专利保护范围，仍须以所附的权利要求书所界定的范围为准。

Claims (10)

  1. 一种处理硫酸盐有机废水的方法，其特征在于，包括以下步骤：
    使水解酸化池产生的含有H 2S的酸化气进入H 2S吸收池；
    使水解酸化池产生的水解酸化液进入产甲烷池产生沼气和沼液；
    使沼液进入沼液吹脱池进行氨氮和二氧化碳脱除，获得吹脱后的沼液；
    使部分吹脱后的沼液进入H 2S吸收池作为吸收液吸收酸化气中的H 2S。
  2. 根据权利要求1所述的方法，其特征在于，还包括以下步骤：
    使进入H 2S吸收池中的吸收液沿从上至下方向以折流的方式进行流动，吸收酸化气中的H 2S，产生含硫吸收液；
    使进入H 2S吸收池的含有H 2S的酸化气沿从下至上方向进行流动，脱硫后形成脱硫酸化气。
  3. 根据权利要求1或2所述的方法，其特征在于，还包括以下步骤：
    使H 2S吸收池中产生的部分脱硫酸化气进入水解酸化池；
    使水解酸化池中的液体在脱硫酸化气的作用下沿导流装置流动，以使水解酸化池中的混合液得到充分的搅拌并加速H 2S的释放。
  4. 根据权利要求1或2所述的方法，其特征在于，还包括以下步骤：
    使H 2S吸收池中产生的部分含硫吸收液回流至沼液吹脱池；
    使H 2S吸收池中产生的部分脱硫酸化气进入产甲烷池，以作为沼气生产的原料。
  5. 根据权利要求1或2所述的方法，其特征在于，
    采用设置在沼液吹脱池底部的微孔曝气头对进入沼液吹脱池的沼液进行氨氮和二氧化碳脱除，获得吹脱后的沼液。
  6. 一种处理硫酸盐有机废水的系统，其特征在于，包括：
    水解酸化池，其用于产生含有H 2S的酸化气和水解酸化液；
    H 2S吸收池，其与所述水解酸化池相连，以使所述含有H 2S的酸化气进入所述H 2S吸收池中；
    产甲烷池，其与所述水解酸化池相连以使所述水解酸化液进入所述产甲烷池中，所述产甲烷池利用进入其中的所述水解酸化液生产沼气和沼液；以及
    沼液吹脱池，其与所述产甲烷池相连以使所述沼液进入所述沼液吹脱池中， 所述沼液吹脱池对进入其中的沼液进行氨氮和二氧化碳脱除，获得吹脱后的沼液；
    其中，所述沼液吹脱池还与所述H 2S吸收池相连，从而使部分所述吹脱后的沼液进入所述H 2S吸收池作为吸收液吸收酸化气中的H 2S。
  7. 根据权利要求6所述的系统，其特征在于，所述H 2S吸收池的出气口与所述水解酸化池的进气口相连，以向所述水解酸化池中输入部分脱硫酸化气；
    所述水解酸化池中还设置有导流装置，其用于使所述水解酸化池中的液体在脱硫酸化气的作用下沿导流装置流动，以使所述水解酸化池中的混合液得到充分的搅拌并加速H 2S的释放；
    所述H 2S吸收池的出气口还与所述产甲烷池的进气口相连，以向所述产甲烷池输入部分脱硫酸化气。
  8. 根据权利要求6或7所述的系统，其特征在于，所述H 2S吸收池中还设置有折流板组件，所述折流板组件包括多个交替从所述H 2S吸收池的两侧延伸出的折流板，从而使吸收液沿从上至下方向以折流的方式进行流动；
    所述H 2S吸收池的含硫吸收液出口还分别与所述沼液吹脱池的回流进液口以及外界相连，以向所述沼液吹脱池输入含硫吸收液，或向外界排出含硫吸收液。
  9. 根据权利要求6或7所述的系统，其特征在于，所述沼液吹脱池的底部安装有微孔曝气头，所述微孔曝气头的供气管路上安装有空气泵；
    所述沼液吹脱池还分别与出水池及废气处理装置相连。
  10. 根据权利要求9所述的系统，其特征在于，还包括自动控制机构，所述自动控制机构包括：
    硫酸盐和硫化物分析仪、沼气成分分析仪和控制器，所述控制器分别与所述硫酸盐和硫化物分析仪、所述沼气成分分析仪电连接；
    所述硫酸盐和硫化物分析仪设置在连接所述水解酸化池和所述产甲烷池之间的管路上，以对水解酸化池输出的水解酸化液进行分析；
    所述沼气成分分析仪设置在所述产甲烷池上并与所述产甲烷池内部连通，以对产甲烷池中产生的沼气进行分析；
    所述控制器根据所述硫酸盐和硫化物分析仪和所述沼气成分分析仪获得的实时数据自动控制空气泵的流量和进入水解酸化池的脱硫酸化气的流量。
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