WO2014007089A1 - バイオガスの生物学的脱硫装置及び脱硫方法 - Google Patents

バイオガスの生物学的脱硫装置及び脱硫方法 Download PDF

Info

Publication number
WO2014007089A1
WO2014007089A1 PCT/JP2013/067187 JP2013067187W WO2014007089A1 WO 2014007089 A1 WO2014007089 A1 WO 2014007089A1 JP 2013067187 W JP2013067187 W JP 2013067187W WO 2014007089 A1 WO2014007089 A1 WO 2014007089A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
hydrogen sulfide
biogas
oxygen
biological desulfurization
Prior art date
Application number
PCT/JP2013/067187
Other languages
English (en)
French (fr)
Japanese (ja)
Inventor
田中　俊博
大介 南
正司 小田切
Original Assignee
荏原実業株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 荏原実業株式会社 filed Critical 荏原実業株式会社
Priority to SG11201408776VA priority Critical patent/SG11201408776VA/en
Publication of WO2014007089A1 publication Critical patent/WO2014007089A1/ja

Links

Images

Classifications

    • 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
    • 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
    • B01D53/30—Controlling by gas-analysis apparatus
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • 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
    • C10L3/103—Sulfur containing contaminants
    • 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
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/10—Recycling of a stream within the process or apparatus to reuse elsewhere therein
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/24—Mixing, stirring of fuel components
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/26—Composting, fermenting or anaerobic digestion fuel components or materials from which fuels are prepared
    • 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

Definitions

  • the present invention relates to a biogas biological desulfurization apparatus and a desulfurization method, and more particularly to a technology for efficiently treating hydrogen sulfide contained in biogas generated in a methane fermentation process by converting it to sulfuric acid.
  • Biogas mainly composed of methane gas
  • concentration of biogas varies depending on the method of methane fermentation, it contains 65 to 85% methane, 15 to 35% carbon dioxide, and 1000 to 6000 ppm hydrogen sulfide as main components.
  • Methane in the generated biogas can be used as fuel for the boiler, and steam generated from the boiler can be used effectively in the heating facility.
  • Biogas also serves as a fuel for gas engines and can generate electricity.
  • Hydrogen sulfide contained in biogas is oxidized to sulfurous acid gas (SO 2 ) during combustion, and the generated sulfurous acid gas becomes sulfuric acid when dissolved in moisture and causes acid rain when released into the atmosphere.
  • SO 2 sulfurous acid gas
  • the condensed moisture turns into sulfuric acid, which causes problems such as corrosion. Therefore, in order to use biogas, removal of hydrogen sulfide has become an important issue.
  • a dry desulfurization method as a method for removing hydrogen sulfide in biogas, and hydrogen sulfide is removed using a pellet-type desulfurization agent mainly composed of iron oxide.
  • the amount of hydrogen sulfide removed by the desulfurizing agent is approximately proportional to the amount of iron oxide present.
  • the iron oxide involved in the hydrogen sulfide removal reaction of the desulfurizing agent disappears, the removal performance deteriorates and it is necessary to replace it with a new agent.
  • Other desulfurization methods include biological desulfurization methods using microorganisms as in the present invention.
  • a trace amount of air or oxygen is supplied to a biogas, and hydrogen sulfide is converted by microorganisms into sulfur (S) or sulfuric acid (H 2 ) in the reaction pathway shown in the following (formula 1) and (formula 2).
  • This is a method of generating and removing SO 4 ).
  • the microorganisms involved in (Formula 1) and (Formula 2) can adhere to or float on the surface of the filler, and there are many aerobic bacteria that are sulfur-oxidizing bacteria in nature. Since microorganisms are involved, temperature and moisture are essential for the living environment of microorganisms.
  • (Formula 1) is a reaction in which hydrogen sulfide generates elemental sulfur (S) by sulfur-oxidizing bacteria. This is the main reaction when oxygen is 1/2 mol or less of hydrogen sulfide. When oxygen exceeds 1/2 mol of hydrogen sulfide, the reaction of (Formula 2) is further performed by sulfur-oxidizing bacteria, and sulfuric acid (H 2 SO 4 ) is generated. In order to convert all the hydrogen sulfide into sulfuric acid (H 2 SO 4 ), 2 mol or more of hydrogen sulfide is theoretically required in the presence of sulfur-oxidizing bacteria.
  • patent document 1 as an example of biological desulfurization technique.
  • this method when the treatment becomes worse, a part of the removed hydrogen sulfide is precipitated as sulfur and adheres to the filler, and a part is converted to sulfuric acid.
  • a technique is described in which the precipitated sulfur is filled with water in a biological desulfurization tower and peeled off by aeration to recover the treatment performance.
  • sulfur-oxidizing bacterium has a disadvantage that the initial hydrogen sulfide removing ability is reduced at an accelerated rate because the biological reaction is inhibited by the formation of sulfur.
  • Patent Document 2 which is another technology, the processing gas in the desulfurization tower is circulated, and the control of the circulation amount is controlled by the pressure value of the pressure adjustment tank installed in the latter stage of the desulfurization tower.
  • the gas is stored in the pressure adjustment tank, and the gas in the pressure adjustment tank is used as the circulating gas to the desulfurization tower.
  • biogas containing high-concentration hydrogen sulfide flows in this method, biogas is not circulated and the load of hydrogen sulfide is reduced if the biogas processed in the gas utilization facility at the latter stage of the pressure adjustment tank is used. Since it is processed in a high state, there is a drawback that it is impossible to avoid the cause of the sulfur being precipitated and the desulfurization performance being lowered.
  • the supply of the oxygen-containing gas is adjusted according to the flow rate of the processing gas from the desulfurization tower, and is managed by an oxygen concentration meter installed in the processing gas outflow line at the latter stage of the desulfurization tower.
  • oxygen concentration in the processing gas is increased, and the supply amount of the oxygen-containing gas is controlled to be reduced. For this reason, there is a defect that oxygen necessary for conversion to sulfuric acid is insufficient, sulfur deposition is promoted, and processing performance is further deteriorated.
  • the problem to be solved by the present invention is that, in view of the above-mentioned problems, the hydrogen sulfide under high load is efficiently treated, and the hydrogen sulfide to be treated is converted into sulfuric acid, thereby eliminating the blockage in the apparatus and cleaning. It is an object of the present invention to provide a biogas biological desulfurization apparatus and a desulfurization method that can be processed at low cost by eliminating such processes.
  • the biological desulfurization apparatus and the biological desulfurization method of the present invention have the following technical features.
  • a biogas inflow line for introducing biogas from the end of the biological desulfurization tower is provided; Providing a packed bed made of a filler to which microorganisms adhere in the biological desulfurization tower; A processing gas outlet line for discharging the processing gas at the other end of the biological desulfurization tower and after the packed bed; Providing a circulation gas line for circulating a part of the processing gas to an end of the biological desulfurization tower into which the biogas flows;
  • the biogas inflow line and the circulating gas line are connected to an end of the biological desulfurization tower after joining, and the biogas and a part of the processing gas are mixed to end the biological des
  • a mixed gas line to supply A gas flow meter is provided in the biogas inflow line
  • a hydrogen sulfide concentration meter is provided in the mixed gas line
  • An arithmetic unit for calculating a hydrogen sulfide load amount from the hydrogen sulfide concentration value of the biogas by the hydrogen sulfide concentration meter and the gas flow value by the gas flow meter is provided
  • a biological desulfurization apparatus comprising a circulating gas signal transmission mechanism for operating the circulating gas amount adjusting mechanism based on a calculation result of the hydrogen sulfide load amount of the computing unit.
  • An oxygen-containing gas inflow line for introducing an oxygen-containing gas into the biogas inflow line is provided, A supply adjustment mechanism for the oxygen-containing gas amount is provided in the oxygen-containing gas inflow line,
  • An oxygen-containing gas inflow line for introducing an oxygen-containing gas into the mixed gas line is provided, A supply adjustment mechanism for the oxygen-containing gas amount is provided in the oxygen-containing gas inflow line,
  • the biogas inflow step includes an oxygen-containing gas inflow step of introducing an oxygen-containing gas into the biogas,
  • the mixed gas step includes an oxygen-containing gas inflow step of introducing an oxygen-containing gas into the biogas,
  • the removed hydrogen sulfide is converted to sulfuric acid to eliminate the problem of clogging due to the precipitation of sulfur, and a highly efficient biological
  • the chemical desulfurization process is maintained.
  • a gas flow meter is provided in the biogas inflow line
  • a hydrogen sulfide concentration meter is provided in the mixed gas line
  • the concentration and gas of the hydrogen sulfide concentration meter are used to obtain a mixed gas hydrogen sulfide concentration suitable for biological desulfurization methods.
  • desulfurization treatment can be performed with a sulfuric acid conversion rate of 100%. % Can be desulfurized.
  • Precipitated sulfur is hydrophobic, so when it adheres to the filler, it covers the surface of the microorganisms adhering to the filler surface and reduces the activity. Sulfur continues to precipitate toward the depth of the filler, eventually closing the filler in the biological desulfurization tower. Sulfur is difficult to remove from the filler once deposited, and it does not return to the original treatment performance even if the stripping treatment is performed by some means. Therefore, sulfur should be used to maintain the biological desulfurization treatment performance. It is important to devise treatment without depositing.
  • the inventors of the present application have examined the conditions for maintaining the treatment performance of biological desulfurization without precipitating sulfur by installing an apparatus in a biogas plant.
  • Biogas A gas generated by methane fermentation and does not contain oxygen.
  • -Oxygen-containing gas A gas containing oxygen.
  • Circulating gas A gas in which a part of the processing gas flows again into the biological desulfurization tower by the circulating gas amount adjusting mechanism.
  • -Gas mixture A gas mixture of biogas and process gas. The hydrogen sulfide concentration of this gas is measured.
  • Processing gas Gas discharged from a biological desulfurization tower.
  • K in (Expression 3) is a correction coefficient using temperature as a parameter, and is expressed by (Expression 4).
  • Correction coefficient K [kg / m 3 ] (273 + 35) /273/22.4 ⁇ 34 (Formula 4)
  • the calculation of the sulfuric acid conversion rate is obtained from the sulfuric acid conversion amount per day and the removed hydrogen sulfide amount per day.
  • the calculation method of the sulfuric acid conversion amount per day is shown in (Formula 5)
  • the amount of hydrogen sulfide removed per day is shown in (Formula 6)
  • the sulfuric acid conversion rate is shown in (Formula 7).
  • Sulfuric acid conversion amount [kg-H 2 SO 4 / day] (sulfuric acid concentration on that day ⁇ sulfuric acid concentration on the previous day) [kg-H 2 SO 4 / L] ⁇ circulating fluid volume [L / day] (Formula 5)
  • Oxygen consumed in the biological desulfurization system includes an oxygen amount necessary for sulfation by microorganisms (O 2 O 3 ) and an oxygen amount necessary for respiration of microorganisms (O R ).
  • Oxygen-containing gas supply amount supplied to the biological desulfurization tower of the present invention [kg-O 2 / day] is a O O + O R.
  • O O [kg-O 2 / day] removal of hydrogen sulfide amount [kg-H 2 S / day ] ⁇ 32/34 [kg-O 2 / kg / H 2 S] ⁇ 2 ( Equation 8)
  • the oxygen required for biological desulfurization is supplied in gaseous form.
  • pure oxygen gas supplied as an oxygen-containing gas at 25 ° C.
  • the pure oxygen gas amount is expressed by (Equation 9).
  • Pure oxygen gas amount [m 3 -O 2 / day] O 2 O [kg-O 2 /day]/32 ⁇ 22.4 ⁇ (273+25)/273/1000 (formula 9)
  • Air amount [m 3 -air / day] pure oxygen gas amount [m 3 -O 2 / day] ⁇ (100/21) (Formula 10)
  • the adhesion amount per 1 m 3 of filler was 1 kg-SS / m 3 and the respiration rate was 5 to 10 mg-O 2 / (g-SS ⁇ hr).
  • Microorganisms adhering per filler 1 m 3 is 1kg-SS, O R is 0.12 ⁇ 0.24kg-O 2 / day .
  • O R is sufficiently smaller than O 2 O , in order not to inhibit the activity of microorganisms, the inventors have experimented to contain 1.5 to 3 times as much oxygen as O 2 O. It has been found that a gas supply rate is preferred.
  • the amount of oxygen to be supplied is less than 1.5 times that of O 2 O , the sulfation of microorganisms is delayed, and when it becomes 3 or more times that of O 2 O, a large amount of unreacted oxygen-containing gas is contained in the processing gas.
  • the concentration of methane gas inside decreases, and the value of fuel decreases.
  • Embodiments of the present invention will be described below.
  • the inventor conducted long-term continuous experiments using the biological desulfurization apparatus of the present invention, and efficiently and stably even under conditions where the concentration of hydrogen sulfide in biogas and the flow rate of biogas fluctuate. We examined the method of processing.
  • FIG. Implementation is not limited to this embodiment.
  • the filler to which microorganisms adhere was packed in the packed bed 1a of the biological desulfurization tower 1.
  • a gas flow meter 3 is provided in the biogas inflow line 2.
  • the biogas inflow line 2 and the circulation gas line 9 merge to mix the biogas and the circulation gas.
  • a hydrogen sulfide concentration meter 4 is provided in the mixed gas line 5.
  • the oxygen-containing gas inflow line 6 is directly connected to the biogas inflow line 2.
  • the supply amount of the oxygen-containing gas 0b is adjusted by the oxygen-containing gas amount supply adjusting mechanism 7.
  • the mixed gas line 5 is directly connected to the biological desulfurization tower 1.
  • the packing material to which microorganisms adhere is made of polyethylene, has a cylindrical shape of ⁇ 15 mm ⁇ h15 mm, has a specific surface area of 1000 m 2 / m 3 , and the treatment gas outflow line 8 is directly connected to the biological desulfurization tower 1.
  • the processing gas 0c is discharged out of the system through the processing gas outflow line 8.
  • the circulating gas line 9 branches from the processing gas outflow line 8 and is connected to the biogas inflow line 2. A part of the processing gas 0c is mixed with the biogas through the circulation gas line 9 by the circulation blower. The circulating gas amount is adjusted by the circulating gas amount adjusting mechanism 10.
  • the circulating fluid 0d from the circulating fluid reservoir 1b was sprinkled from the upper part of the biological desulfurization tower 1.
  • a part of the circulating fluid is intermittently discharged as blow water 0e, and makeup water 0f is replenished and the amount of water in the circulating fluid reservoir 1b. was kept constant.
  • the biogas flow rate value and the mixed gas hydrogen sulfide concentration value are input to the computing unit 12, and the hydrogen sulfide load is calculated based on (Equation 3).
  • the calculator 12 receives the biogas flow rate value and the mixed gas hydrogen sulfide concentration value, calculates the circulating gas amount based on the preset mixed gas hydrogen sulfide concentration value, and adjusts the circulating gas amount adjusting mechanism. .
  • the circulating gas line 9 may be branched from the processing gas outflow line 8 or directly connected to the biological desulfurization tower 1.
  • the circulating gas supply means may use a blower or a pump.
  • the control of the circulating gas amount adjusting mechanism 10 is performed by the circulating gas control mechanism 13.
  • the circulating gas control mechanism 13 may be physical control or control by an electrical signal.
  • the physical control method may be to manually adjust the opening of the blower inverter, valve or damper
  • the electrical control method is to electrically control the inverter or the opening of the valve or damper. May be electrically controlled.
  • the oxygen-containing gas inflow line 6 may be directly connected to the biogas inflow line 2 or may be directly connected to the mixed gas line 5.
  • FIG. 1 An apparatus diagram in which the oxygen-containing gas inflow line 6 is directly connected to the mixed gas line 5 is shown in FIG.
  • the oxygen-containing gas supply means may use a blower or a pump.
  • the oxygen-containing gas supply adjusting mechanism 7 is controlled by the oxygen-containing gas control mechanism 14.
  • the oxygen-containing gas signal transmission mechanism 14 may be physically controlled or controlled by an electrical signal.
  • the physical control method may be to manually adjust the opening of the blower inverter, valve or damper
  • the electrical control method is to electrically control the inverter or the opening of the valve or damper. May be electrically controlled.
  • the gas flow meter an orifice flow meter, a volumetric flow meter, a vortex flow meter, a flow rate type flow meter, etc. can be used, and the positive displacement flow meter can use a measured dry gas meter or a measured wet type, Further, the actual dry gas meter may be a membrane type or a rotor type.
  • the hydrogen sulfide concentration meter As the hydrogen sulfide concentration meter, a measurement method by a potentiostatic electrolytic method, a silver nitrate potentiometric titration method, an ion electrode method, a methylene blue absorptiometry, a gas chromatograph method, or the like may be used. Moreover, you may measure the hydrogen sulfide by a detection tube.
  • the oxygen-containing gas is a gas containing oxygen, and air, pure oxygen, or a gas whose oxygen concentration is adjusted by an oxygen generator may be used.
  • the filler to which microorganisms adhere is only required to be a material having chemical resistance that can be used under strong acidity of pH 1 or lower.
  • the material is preferably an organic substance such as polyethylene, polypropylene, vinyl chloride, and polyurethane.
  • the shape of the filler is preferably a cylinder, a reticulated skeleton pipe, a ball or a sea urchin.
  • the specific surface area is preferably in the range of 50 to 1000 m 2 / m 3 .
  • the porosity is preferably in the range of 80 to 96%.
  • the computing unit only needs to have a function of calculating the hydrogen sulfide load based on the hydrogen sulfide concentration and the gas flow rate. Further, it is only necessary to have a function for recording the hydrogen sulfide concentration, the gas flow rate, and the hydrogen sulfide load.
  • the recording method of the measured value and the calculation result by the calculator may be a digital data logger or a recorder using chart paper.
  • the mixed gas hydrogen sulfide concentration is preferably adjusted to be in the range of 100 to 1000 ppm by circulating the processing gas.
  • the mixed gas hydrogen sulfide concentration is adjusted to be in a range of 150 to 500 ppm by circulating the processing gas.
  • FIG. 1 is an apparatus diagram in which piping is installed so as to process biogas in a downward flow, and biogas may be processed in an upward flow.
  • FIG. 3 shows an apparatus diagram in which piping is installed so as to process biogas in an upward flow using the present invention.
  • FIG. 1 A flowchart for controlling the circulating gas amount adjusting mechanism of the present invention is shown in FIG.
  • the present invention measures the biogas flow Q B, to measure the mixed gas hydrogen sulfide concentrations C.
  • the circulating gas amount Q R calculated in calculator adjusts the circulation amount of gas Q R by operating the circulating gas amount adjusting mechanism.
  • the oxygen-containing gas supply adjustment mechanism is operated to adjust the oxygen-containing gas supply.
  • the biological desulfurization apparatus of FIG. 1 was filled with a cylindrical filler of ⁇ 15 mm ⁇ h15 mm made of polyethylene and having a specific surface area of 1000 m 2 / m 3 and ⁇ 15 mm ⁇ h15 mm.
  • the mixed gas flowed downward in the biological desulfurization tower.
  • the oxygen-containing gas was mixed in the biogas inlet line.
  • the circulating fluid was activated sludge and stored in a circulating fluid storage tank at the bottom of the biological desulfurization tower.
  • the circulating liquid was sent to the upper part of the biological desulfurization tower by a pump and sprinkled with 200 L / day in parallel with the gas direction.
  • the processing temperature was set to 35 ° C.
  • Air oxygen concentration; volume ratio 21%) was used as the oxygen-containing gas.
  • the methane concentration in the biogas was 80% by volume and the carbon dioxide concentration was 20% by volume, and was almost constant throughout the implementation period.
  • the circulation ratio refers to the ratio (Q R / Q B ) of the circulation gas amount (Q R ) to the biogas flow rate (Q B ).
  • the biogas hydrogen sulfide concentration and the biogas amount were changed with the passage of measurement time.
  • the processing conditions for each measurement time are as follows. Measurement time: 0 to 4 hr, biogas hydrogen sulfide concentration: 1500 ppm, biogas amount: 4 m 3 / day Measurement time: 4-8 hrs.
  • Biogas hydrogen sulfide concentration 1500 ppm, biogas amount: 2 m 3 / day Measurement time: 8 to 12 hr, biogas hydrogen sulfide concentration: 3000 ppm, biogas amount: 2 m 3 / day Measurement time: 12 to 16 hr, biogas hydrogen sulfide concentration: 6000 ppm, biogas amount: 1.5 m 3 / day Measurement time: 16 to 20 hr...
  • the experimental conditions were changed every 4 hours, and the processing performance was investigated.
  • the amount of circulating gas was controlled so that the mixed gas hydrogen sulfide concentration was 300 ppm. Even if fluctuations in the biogas stream water concentration or fluctuations in the amount of biogas occurred, the treatment could be followed, and hydrogen sulfide was not detected from the treatment gas, and 100% could be removed. When the hydrogen sulfide concentration in the biogas was 300 ppm, 100% of the hydrogen sulfide was removed even when the circulating gas was stopped.
  • the experimental results according to the present invention are shown in FIG.
  • the circulating gas amount was supplied at 16 m 3 / day with respect to the biogas amount 4 m 3 / day in order to set the hydrogen sulfide concentration of the mixed gas to 300 ppm.
  • the load at this time was 2.0 kg / (m 3 ⁇ day).
  • the mixed gas hydrogen sulfide concentration was 300 ppm, and hydrogen sulfide was not detected from the process gas.
  • the circulating gas amount was supplied at 8 m 3 / day with respect to the biogas amount 2 m 3 / day in order to set the mixed gas hydrogen sulfide concentration to 300 ppm.
  • the load at this time was 1.0 kg / (m 3 ⁇ day).
  • the mixed gas hydrogen sulfide concentration was 300 ppm, and hydrogen sulfide was not detected from the process gas.
  • the circulating gas amount was supplied at 18 m 3 / day with respect to the biogas amount 2 m 3 / day.
  • the load at this time was 2.0 kg / (m 3 ⁇ day).
  • the mixed gas hydrogen sulfide concentration was 300 ppm, and hydrogen sulfide was not detected from the process gas.
  • the circulating gas amount was supplied at 1.3 m 3 / day with respect to the biogas amount 2 m 3 / day in order to set the mixed gas hydrogen sulfide concentration to 300 ppm.
  • the load at this time was 0.3 kg / (m 3 ⁇ day).
  • the mixed gas hydrogen sulfide concentration was 300 ppm, and hydrogen sulfide was not detected from the process gas.
  • biogas hydrogen sulfide concentration was 300 ppm during the measurement period of 20 to 24 hours, the circulating gas was stopped. The load at this time was 0.2 kg / (m 3 ⁇ day). The mixed gas hydrogen sulfide concentration was 300 ppm, and hydrogen sulfide was not detected from the process gas.
  • the circulation ratio is 4 times; that is, when the amount of circulating gas is 4 times based on the amount of biogas, the treatment performance deteriorates when the biogas hydrogen sulfide concentration is 3000 ppm or more.
  • the biogas hydrogen sulfide concentration is low, such as 500 ppm or less, the process gas does not contain hydrogen sulfide, but is excessively diluted, so that the purity as biogas is low.
  • FIG. 7 shows the experimental result of the comparison, and details will be described below.
  • the biogas amount was 4 m 3 / day during the measurement time of 0 to 4 hours, the circulating gas amount was 16 m 3 / day.
  • the load at this time was 2.0 kg / (m 3 ⁇ day). At this time, hydrogen sulfide was not detected from the processing gas.
  • the circulating gas amount was set to 8 m 3 / day.
  • the load at this time was 1.0 kg / (m 3 ⁇ day). At this time, hydrogen sulfide was not detected from the processing gas.
  • the circulating gas amount was set to 8 m 3 / day.
  • the load at this time was 2.0 kg / (m 3 ⁇ day).
  • the treatment gas hydrogen sulfide concentration was 300 ppm, and the hydrogen sulfide removal rate was 90%.
  • the circulating gas amount was set to 6 m 3 / day.
  • the load at this time was 3.0 kg / (m 3 ⁇ day).
  • the treatment gas hydrogen sulfide concentration was 2000 ppm, and the hydrogen sulfide removal rate was 67%.
  • the biogas amount was 2 m 3 / day in the measurement time period of 16 to 20 hours, the circulating gas amount was 8 m 3 / day.
  • the load at this time was 0.3 kg / (m 3 ⁇ day). At this time, hydrogen sulfide was not detected from the processing gas.
  • the biogas amount was 2 m 3 / day in the measurement time period of 20 to 24 hours, the circulating gas amount was 8 m 3 / day.
  • the load at this time was 0.2 kg / (m 3 ⁇ day). At this time, hydrogen sulfide was not detected from the processing gas.
  • the biological desulfurization apparatus of FIG. 1 was filled with a cylindrical filler of ⁇ 15 mm ⁇ h15 mm made of polyethylene and having a specific surface area of 1000 m 2 / m 3 and ⁇ 15 mm ⁇ h15 mm.
  • the mixed gas flowed downward in the biological desulfurization tower.
  • the oxygen-containing gas was mixed in the biogas inlet line.
  • the circulating fluid was activated sludge and stored in a circulating fluid storage tank at the bottom of the biological desulfurization tower.
  • the circulating liquid was sent to the upper part of the biological desulfurization tower by a pump and sprinkled with 200 L / day in parallel with the gas direction.
  • the processing temperature was set to 35 ° C.
  • Air oxygen concentration; volume ratio 21%) was used as the oxygen-containing gas, and was supplied in the range of 15 L / day to 120 L / day.
  • the methane concentration in the biogas was 80% by volume and the carbon dioxide concentration was 20% by volume, and was almost constant throughout the implementation period.
  • the removal performance was investigated when the circulating gas flow rate was controlled based on the hydrogen sulfide concentration and biogas flow rate of the mixed gas.
  • biogas having a hydrogen sulfide concentration of 6000 ppm was supplied at 1 m 3 / day, and the set hydrogen sulfide load was 2.0 kg / (m 3 ⁇ day).
  • Circulating gas amount was treated appropriately adjusted to a range of 3 ⁇ 119m 3 / day with respect to biogas flow rate 1 m 3 / day.
  • the results of this experiment are shown in Table 1.
  • the values of the experimental results in the table are the values on the 30th day of evaluation.
  • Circulating gas volume in Run2-1 is to 3m 3 / day supply to the biogas volume 1 m 3 / day, mixed when in the process gas does not contain hydrogen sulfide gas hydrogen sulfide concentrations (hereinafter, the mixed gas of hydrogen sulfide The concentration setting value is set to 1500 ppm. At this time, the removal rate of hydrogen sulfide was 40%, and the conversion rate of sulfuric acid was 70%.
  • Circulating gas volume in Run2-2 is to 5 m 3 / day supply to the biogas volume 1 m 3 / day, a mixed gas of hydrogen sulfide concentration setting was set to be 1000 ppm.
  • the hydrogen sulfide removal rate at this time was 50%, and the sulfuric acid conversion rate was 100%.
  • Circulating gas volume in Run2-3 is to 9m 3 / day supply to the biogas volume 1 m 3 / day, a mixed gas of hydrogen sulfide concentration setting was set to be 600 ppm.
  • the hydrogen sulfide removal rate at this time was 80%, and the sulfuric acid conversion rate was 100%.
  • the circulating gas amount in Run 2-4 was supplied to the biogas amount of 1 m 3 / day at 5 m 3 / day, so that the mixed gas hydrogen sulfide concentration set value was 500 ppm.
  • the hydrogen sulfide removal rate at this time was 95%, and the sulfuric acid conversion rate was 100%.
  • Circulating gas volume in Run2-5 ⁇ Run2-7 is biogas volume 1 m 3 / day in Run2-5 to 14m 3 / day, in Run2-6 19m 3 / day, in Run2-7 39m 3 / day supply did.
  • the mixed gas hydrogen sulfide concentration set value was 400 ppm for Run 2-5, 300 ppm for Run 2-6, and 150 ppm for Run 2-7. During these experiments, the hydrogen sulfide removal rate was 100% and the sulfuric acid conversion rate was 100%.
  • Circulating gas volume in Run2-9 is to 59m 3 / day supply to the biogas volume 1 m 3 / day, a mixed gas of hydrogen sulfide concentration setting was set to be 100 ppm.
  • the hydrogen sulfide removal rate at this time was 50%, and the sulfuric acid conversion rate was 100%.
  • Circulating gas volume in Run2-10 is to 119m 3 / day supply to the biogas volume 1 m 3 / day, a mixed gas of hydrogen sulfide concentration setting was set to be 50 ppm. At this time, the removal rate of hydrogen sulfide was 40%, and the conversion rate of sulfuric acid was 70%.
  • the circulating gas was adjusted so that the mixed gas hydrogen sulfide concentration was 100 to 1000 ppm.
  • the hydrogen sulfide removal rate was 50% or more, and the sulfuric acid conversion rate was 100%.
  • the desulfurization process was carried out.
  • the circulating gas is adjusted so that the mixed gas hydrogen sulfide concentration is 150 ppm to 500 ppm. During these periods, the hydrogen sulfide removal rate is 95% or more and the sulfuric acid conversion rate is 100%. Desulfurization treatment was performed.
  • the amount of circulating gas so that the mixed gas stream hydrogen concentration is in the range of 100 ppm to 1000 ppm, and more preferably, the amount of circulating gas is adjusted to be in the range of 150 ppm to 500 ppm. Is good.
  • the hydrogen sulfide removal rate is 95%, and when the amount of circulating gas is controlled so as to be in the range of 300 ppm to 400 ppm, the hydrogen sulfide removal rate is 100%. Became.
  • the hydrogen sulfide removal rate is 95%, and when the amount of circulating gas is controlled to be 600 ppm or more, the hydrogen sulfide removal rate is 80% or less. It became.
  • the hydrogen sulfide removal rate was 50%, and when the amount of circulating gas was controlled so as to be 1500 ppm, the hydrogen sulfide removal rate was 40%.
  • the biological desulfurization apparatus in FIG. 1 is made of polyethylene, has a specific surface area of 1000 m 2 / m 3 , and is filled with a cylindrical filler of ⁇ 15 mm ⁇ h15 mm to a filling height of 2 m. It was set to 3 .
  • the mixed gas flowed downward in the biological desulfurization tower.
  • the oxygen-containing gas was mixed in the biogas inlet line.
  • the circulating fluid was activated sludge and stored in a circulating fluid storage tank at the bottom of the biological desulfurization tower.
  • the circulating liquid was sent to the upper part of the biological desulfurization tower by a pump and sprinkled 1.6 m 3 / day in parallel with the gas direction.
  • the processing temperature was set to 35 ° C.
  • Air oxygen concentration; volume ratio 21%) was used as the oxygen-containing gas.
  • the methane concentration in the biogas was 80% by volume and the carbon dioxide concentration was 20% by volume, and was almost constant throughout the implementation period.
  • the oxygen-containing gas supply amount is controlled by the hydrogen sulfide load, while the comparison is made by comparing the oxygen-containing gas supply amount with a constant ratio to the gas flow rate.
  • the hydrogen sulfide concentration of the biogas was adjusted to three levels of 1000 ppm, 3000 ppm, and 6000 ppm for both the invention of the present application and the proportionality.
  • the biogas flow rate was constant at 8.3 m 3 / hr.
  • the mixed gas hydrogen sulfide concentration was kept constant at 300 ppm by adjusting the circulating gas flow rate.
  • the evaluation period of the experiment was 5 days for each run.
  • the value of the experimental result in the table is the value on the fifth day of evaluation.
  • Table 2 shows the experimental results (Run 3-1 to Run 3-3) of the present invention.
  • the air supply amount is controlled based on the hydrogen sulfide load amount. Specifically, the amount of oxygen required for sulfation was calculated from the hydrogen sulfide load, and air was supplied so that 1.5 times the amount of oxygen obtained was supplied.
  • Run 3-1 had a hydrogen sulfide load of 0.3 kg / (m 3 / day) and an air supply amount of 0.14 m 3 / hr. As a result of Run3-1, the hydrogen sulfide removal rate was 100%, and the sulfuric acid conversion rate was 100%.
  • Run 3-2 the hydrogen sulfide load was 1.0 kg / (m 3 ⁇ day), and the air supply amount was 0.42 m 3 / hr. As a result of Run 3-2, the hydrogen sulfide removal rate was 100%, and the sulfuric acid conversion rate was 100%.
  • Table 3 shows comparative experimental results (Run 3-4 to Run 3-6).
  • the air supply amount was controlled so as to be a constant ratio with respect to the biogas flow rate, and an air amount of 5.1% was supplied in volume ratio to the biogas flow rate.
  • biogas flow rate in this experiment is constant and 8.3 m 3 / hr, the air supply amount was 0.42 m 3 / hr.
  • Run 3-4 had a hydrogen sulfide load of 0.3 kg / (m 3 ⁇ day). As a result of Run 3-4, the hydrogen sulfide removal rate was 100%, and the sulfuric acid conversion rate was 100%.
  • Run 3-5 had a hydrogen sulfide load of 1.0 kg / (m 3 ⁇ day). As a result of Run 3-5, the hydrogen sulfide removal rate was 100%, and the sulfuric acid conversion rate was 100%.
  • Run 3-6 had a hydrogen sulfide load of 2.0 kg / (m 3 ⁇ day). In Run 3-6, the hydrogen sulfide removal rate was 60% and the sulfuric acid conversion rate was 60%.
  • Run 3-1 of the present invention sufficient treatment can be performed with an air amount of 0.14 m 3 / hr at a hydrogen sulfide load of 0.3 kg / (m 3 ⁇ day).
  • the value of the biogas as a fuel is reduced.
  • Run 3-6 was deficient in the amount of oxygen necessary for sulfation, resulting in a decrease in the hydrogen sulfide removal rate, and sulfur was deposited, causing the inside of the column to be blocked.
  • the oxygen-containing gas supply amount with the hydrogen sulfide load amount as in the present invention, an appropriate amount of oxygen is supplied with respect to the load, and the hydrogen sulfide removal performance and sulfuric acid conversion rate can also be treated at 100%. Stable processing was possible.
  • Example 3 Using the same experimental apparatus as in Example 3, the processing performance when adjusting oxygen-containing gases having different oxygen concentrations was verified with two Runs.
  • the mixed gas flowed downward in the biological desulfurization tower.
  • the oxygen-containing gas was mixed in the biogas inlet line.
  • the circulating fluid was activated sludge and stored in a circulating fluid storage tank at the bottom of the biological desulfurization tower.
  • the circulating liquid was sent to the upper part of the biological desulfurization tower by a pump and sprinkled 1.6 m 3 / day in parallel with the gas direction.
  • the treatment temperature was set to 35 ° C.
  • the methane concentration in the biogas was 80% by volume
  • the carbon dioxide concentration was 20% by volume, which was almost constant throughout the implementation period.
  • the oxygen-containing gas used was a gas (Run 4-1) in which the oxygen concentration was adjusted to 30% by volume and the nitrogen concentration was adjusted to 70%, and the oxygen concentration was adjusted to 60% by volume and the nitrogen concentration was adjusted to 40% by volume.
  • Gas (Run4-2) in which the oxygen concentration was adjusted to 30% by volume and the nitrogen concentration was adjusted to 70%, and the oxygen concentration was adjusted to 60% by volume and the nitrogen concentration was adjusted to 40% by volume.
  • the biogas was adjusted to a hydrogen sulfide concentration of 6000 ppm.
  • the biogas flow rate was constant at 8.3 m 3 / hr, and the hydrogen sulfide load was 2.0 kg / (m 3 ⁇ day).
  • the mixed gas hydrogen sulfide concentration was kept constant at 300 ppm by adjusting the circulating gas flow rate.
  • Table 4 shows the experimental results (Run 4-1 to Run 4-2) when gases having different oxygen concentrations were supplied.
  • the oxygen concentration in the gas was 30% by volume, and the gas supply rate was 0.59 m 3 / hr.
  • the removal rate of hydrogen sulfide was 100%, and the conversion rate of sulfuric acid was 100%.
  • Run4-2 the oxygen concentration in the gas was 60% by volume, and the gas supply amount was 0.30 m 3 / day. As a result of Run4-2, the hydrogen sulfide removal rate was 100%, and the sulfuric acid conversion rate was 100%.
  • the oxygen concentration in the oxygen-containing gas is different by the treatment according to the present invention, an appropriate amount of oxygen can be supplied and the treatment can be performed satisfactorily.
  • the oxygen concentration is high, the amount of oxygen-containing gas to be supplied is reduced and the value as a biogas is increased.
  • the biological desulfurization apparatus in FIG. 2 is made of polyethylene, has a specific surface area of 1000 m 2 / m 3 , and is filled with a cylindrical filler of ⁇ 15 mm ⁇ h15 mm to a filling height of 2 m. It was set to 3 .
  • the mixed gas flowed downward in the biological desulfurization tower.
  • the oxygen-containing gas was mixed in the mixed gas line.
  • the circulating fluid was activated sludge and stored in a circulating fluid storage tank at the bottom of the biological desulfurization tower.
  • the circulating liquid was sent to the upper part of the biological desulfurization tower by a pump, and sprinkled 1.6 m 3 / day in parallel with the gas direction.
  • the processing temperature was set to 35 ° C.
  • Air oxygen concentration; 21% by volume
  • the methane concentration in the biogas was 80% by volume and the carbon dioxide concentration was 20% by volume, and was almost constant throughout the implementation period.
  • the hydrogen sulfide concentration of the biogas was adjusted to three levels of 1000 ppm, 3000 ppm, and 6000 ppm.
  • the biogas flow rate was constant at 8.3 m 3 / hr.
  • the mixed gas hydrogen sulfide concentration was kept constant at 300 ppm by adjusting the circulating gas flow rate.
  • the evaluation period of the experiment was 5 days for each run.
  • the value of the experimental result in the table is the value on the fifth day of evaluation.
  • Run 5-1 had a hydrogen sulfide load of 0.3 kg / (m 3 / day) and an air supply amount of 0.14 m 3 / hr.
  • the hydrogen sulfide removal rate was 100%, and the sulfuric acid conversion rate was 100%.
  • Run 5-2 the hydrogen sulfide load was 1.0 kg / (m 3 ⁇ day), and the air supply amount was 0.42 m 3 / hr. As a result of Run 5-2, the hydrogen sulfide removal rate was 100%, and the sulfuric acid conversion rate was 100%.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Molecular Biology (AREA)
  • Gas Separation By Absorption (AREA)
PCT/JP2013/067187 2012-07-03 2013-06-24 バイオガスの生物学的脱硫装置及び脱硫方法 WO2014007089A1 (ja)

Priority Applications (1)

Application Number Priority Date Filing Date Title
SG11201408776VA SG11201408776VA (en) 2012-07-03 2013-06-24 Device and method for biologically desulfurizing biogas

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2012149052A JP5756061B2 (ja) 2012-07-03 2012-07-03 バイオガスの生物学的脱硫装置及び脱硫方法
JP2012-149052 2012-07-03

Publications (1)

Publication Number Publication Date
WO2014007089A1 true WO2014007089A1 (ja) 2014-01-09

Family

ID=49881847

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2013/067187 WO2014007089A1 (ja) 2012-07-03 2013-06-24 バイオガスの生物学的脱硫装置及び脱硫方法

Country Status (4)

Country Link
JP (1) JP5756061B2 (enrdf_load_stackoverflow)
MY (1) MY173249A (enrdf_load_stackoverflow)
SG (1) SG11201408776VA (enrdf_load_stackoverflow)
WO (1) WO2014007089A1 (enrdf_load_stackoverflow)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015108018A1 (ja) * 2014-01-16 2015-07-23 荏原実業株式会社 生物学的脱硫装置及び脱硫方法
WO2015108019A1 (ja) * 2014-01-16 2015-07-23 荏原実業株式会社 生物脱硫装置及び生物脱硫方法
JP2017154044A (ja) * 2016-02-29 2017-09-07 荏原実業株式会社 脱硫システム及び脱硫方法
CN112210409A (zh) * 2020-10-30 2021-01-12 岳阳县枫树湾畜牧有限公司 一种沼气生物脱硫装置及脱硫方法
CN118526968A (zh) * 2024-07-26 2024-08-23 西原环保(上海)股份有限公司 废气处理装置和方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10128042A (ja) * 1996-10-25 1998-05-19 Takuma Co Ltd 悪臭ガスの生物的処理方法
JP2006143780A (ja) * 2004-11-16 2006-06-08 Toshiba Corp バイオガス精製システム
JP2010022965A (ja) * 2008-07-22 2010-02-04 Kobelco Eco-Solutions Co Ltd 消化ガスの脱硫方法及び装置

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH10128042A (ja) * 1996-10-25 1998-05-19 Takuma Co Ltd 悪臭ガスの生物的処理方法
JP2006143780A (ja) * 2004-11-16 2006-06-08 Toshiba Corp バイオガス精製システム
JP2010022965A (ja) * 2008-07-22 2010-02-04 Kobelco Eco-Solutions Co Ltd 消化ガスの脱硫方法及び装置

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015108018A1 (ja) * 2014-01-16 2015-07-23 荏原実業株式会社 生物学的脱硫装置及び脱硫方法
WO2015108019A1 (ja) * 2014-01-16 2015-07-23 荏原実業株式会社 生物脱硫装置及び生物脱硫方法
JP2017154044A (ja) * 2016-02-29 2017-09-07 荏原実業株式会社 脱硫システム及び脱硫方法
CN112210409A (zh) * 2020-10-30 2021-01-12 岳阳县枫树湾畜牧有限公司 一种沼气生物脱硫装置及脱硫方法
CN112210409B (zh) * 2020-10-30 2021-07-20 岳阳县枫树湾畜牧有限公司 一种沼气生物脱硫装置及脱硫方法
CN118526968A (zh) * 2024-07-26 2024-08-23 西原环保(上海)股份有限公司 废气处理装置和方法
CN118526968B (zh) * 2024-07-26 2024-11-12 西原环保(上海)股份有限公司 废气处理装置和方法

Also Published As

Publication number Publication date
SG11201408776VA (en) 2015-03-30
JP2014008493A (ja) 2014-01-20
JP5756061B2 (ja) 2015-07-29
MY173249A (en) 2020-01-08

Similar Documents

Publication Publication Date Title
WO2014007089A1 (ja) バイオガスの生物学的脱硫装置及び脱硫方法
JP6170197B1 (ja) 脱硫システム及び脱硫方法
Ramos et al. Where does the removal of H2S from biogas occur in microaerobic reactors?
CA2497531A1 (en) Controlling wastewater treatment processes
US20230038934A1 (en) Utilization of biogas scrubber in anaerobic membrane bioreactor systems
JP5756060B2 (ja) バイオガスの生物学的脱硫装置及び生物学的脱硫方法
JP2013543729A (ja) 微好気性条件に曝される好冷性嫌気性分解生物反応器における硫化水素の生物酸化
JP6752181B2 (ja) 脱硫システム及び脱硫方法
JP2015214695A (ja) バイオガスの生物学的脱硫装置及び脱硫方法
CA2881911A1 (en) A method and an apparatus for simultaneous removal of thiosalt and nitrogen compounds in waste water
JP5925179B2 (ja) 生物学的脱硫装置及び生物学的脱硫方法
JP6101740B2 (ja) バイオガスの生物学的脱硫方法
WO2015108019A1 (ja) 生物脱硫装置及び生物脱硫方法
JP6215257B2 (ja) バイオガスの生物学的脱硫方法
EP4359112A1 (en) A process to continuously treat a hydrogen sulphide comprising gas and sulphur reclaiming facilities
JP2013226508A (ja) 窒素含有排水処理方法および装置
JP5767722B2 (ja) 生物学的脱硫装置及び脱硫方法
KR100882228B1 (ko) 과염소산염을 포함한 폐수의 처리 장치 및 그 처리 방법
CN106115973A (zh) 一种组合式氨氮去除装置及控制方法
JP5602063B2 (ja) 排水処理装置
JP5140380B2 (ja) バイオマス発電方法およびバイオマス発電設備
JP7030582B2 (ja) 脱硫設備及びバイオガスの脱硫方法
JP2007000871A (ja) 生物学的水処理装置
WO2023153468A1 (ja) メタン生成システム及びメタン生成方法
JP2006143779A (ja) バイオガス精製システム

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 13813373

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: IDP00201500640

Country of ref document: ID

122 Ep: pct application non-entry in european phase

Ref document number: 13813373

Country of ref document: EP

Kind code of ref document: A1