WO2017154519A1 - 燃焼システム - Google Patents
燃焼システム Download PDFInfo
- Publication number
- WO2017154519A1 WO2017154519A1 PCT/JP2017/005881 JP2017005881W WO2017154519A1 WO 2017154519 A1 WO2017154519 A1 WO 2017154519A1 JP 2017005881 W JP2017005881 W JP 2017005881W WO 2017154519 A1 WO2017154519 A1 WO 2017154519A1
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- WO
- WIPO (PCT)
- Prior art keywords
- gas
- water vapor
- combustion
- processing chamber
- carbon dioxide
- Prior art date
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- 238000002485 combustion reaction Methods 0.000 title claims abstract description 151
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 212
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 176
- 239000012528 membrane Substances 0.000 claims abstract description 131
- 238000000926 separation method Methods 0.000 claims abstract description 115
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 106
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 106
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 157
- 238000006477 desulfuration reaction Methods 0.000 claims description 10
- 230000023556 desulfurization Effects 0.000 claims description 10
- 238000000855 fermentation Methods 0.000 claims description 9
- 230000004151 fermentation Effects 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 4
- 239000008236 heating water Substances 0.000 claims description 4
- 229910052717 sulfur Inorganic materials 0.000 claims description 4
- 239000011593 sulfur Substances 0.000 claims description 4
- 239000012466 permeate Substances 0.000 abstract description 9
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 320
- 238000000034 method Methods 0.000 description 24
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 19
- 238000011156 evaluation Methods 0.000 description 19
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- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 5
- 229920001577 copolymer Polymers 0.000 description 5
- 230000029087 digestion Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
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- 238000009792 diffusion process Methods 0.000 description 4
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- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 4
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- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000010248 power generation Methods 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000002028 Biomass Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
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- FJDQFPXHSGXQBY-UHFFFAOYSA-L caesium carbonate Chemical compound [Cs+].[Cs+].[O-]C([O-])=O FJDQFPXHSGXQBY-UHFFFAOYSA-L 0.000 description 3
- 229910000024 caesium carbonate Inorganic materials 0.000 description 3
- 238000004090 dissolution Methods 0.000 description 3
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- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
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- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 2
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- 229920001477 hydrophilic polymer Polymers 0.000 description 2
- 230000002209 hydrophobic effect Effects 0.000 description 2
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 2
- 229920000058 polyacrylate Polymers 0.000 description 2
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- 229920001343 polytetrafluoroethylene Polymers 0.000 description 2
- CPRMKOQKXYSDML-UHFFFAOYSA-M rubidium hydroxide Chemical compound [OH-].[Rb+] CPRMKOQKXYSDML-UHFFFAOYSA-M 0.000 description 2
- 239000010801 sewage sludge Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- 239000008400 supply water Substances 0.000 description 2
- MFGOFGRYDNHJTA-UHFFFAOYSA-N 2-amino-1-(2-fluorophenyl)ethanol Chemical compound NCC(O)C1=CC=CC=C1F MFGOFGRYDNHJTA-UHFFFAOYSA-N 0.000 description 1
- PECYZEOJVXMISF-UHFFFAOYSA-N 3-aminoalanine Chemical compound [NH3+]CC(N)C([O-])=O PECYZEOJVXMISF-UHFFFAOYSA-N 0.000 description 1
- RZVAJINKPMORJF-UHFFFAOYSA-N Acetaminophen Chemical compound CC(=O)NC1=CC=C(O)C=C1 RZVAJINKPMORJF-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical class OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- 102000003846 Carbonic anhydrases Human genes 0.000 description 1
- 108090000209 Carbonic anhydrases Proteins 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000004471 Glycine Substances 0.000 description 1
- 101100008681 Glycine max DHPS1 gene Proteins 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 229910000288 alkali metal carbonate Inorganic materials 0.000 description 1
- 150000008041 alkali metal carbonates Chemical class 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- ZMCUDHNSHCRDBT-UHFFFAOYSA-M caesium bicarbonate Chemical compound [Cs+].OC([O-])=O ZMCUDHNSHCRDBT-UHFFFAOYSA-M 0.000 description 1
- HUCVOHYBFXVBRW-UHFFFAOYSA-M caesium hydroxide Inorganic materials [OH-].[Cs+] HUCVOHYBFXVBRW-UHFFFAOYSA-M 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 229910052800 carbon group element Inorganic materials 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
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- 229910052798 chalcogen Inorganic materials 0.000 description 1
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- 229910052801 chlorine Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- TVZPLCNGKSPOJA-UHFFFAOYSA-N copper zinc Chemical compound [Cu].[Zn] TVZPLCNGKSPOJA-UHFFFAOYSA-N 0.000 description 1
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- 150000001993 dienes Chemical class 0.000 description 1
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- UQSQSQZYBQSBJZ-UHFFFAOYSA-N fluorosulfonic acid Chemical compound OS(F)(=O)=O UQSQSQZYBQSBJZ-UHFFFAOYSA-N 0.000 description 1
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- KEDRKJFXBSLXSI-UHFFFAOYSA-M hydron;rubidium(1+);carbonate Chemical compound [Rb+].OC([O-])=O KEDRKJFXBSLXSI-UHFFFAOYSA-M 0.000 description 1
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- 244000144972 livestock Species 0.000 description 1
- 239000002075 main ingredient Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
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- 229910052696 pnictogen Inorganic materials 0.000 description 1
- BFPJYWDBBLZXOM-UHFFFAOYSA-L potassium tellurite Chemical compound [K+].[K+].[O-][Te]([O-])=O BFPJYWDBBLZXOM-UHFFFAOYSA-L 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 230000001141 propulsive effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- WPFGFHJALYCVMO-UHFFFAOYSA-L rubidium carbonate Chemical compound [Rb+].[Rb+].[O-]C([O-])=O WPFGFHJALYCVMO-UHFFFAOYSA-L 0.000 description 1
- 229910000026 rubidium carbonate Inorganic materials 0.000 description 1
- 229940082569 selenite Drugs 0.000 description 1
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- 229910052720 vanadium Inorganic materials 0.000 description 1
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Images
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—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 diffusion
- B01D53/228—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 diffusion characterised by specific membranes
-
- 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
- B01D53/22—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 diffusion
-
- 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
- B01D53/22—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 diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
-
- 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
- B01D53/26—Drying gases or vapours
- B01D53/268—Drying gases or vapours by diffusion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
- B01D69/06—Flat membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
- B01D69/08—Hollow fibre membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
- B01D69/10—Supported membranes; Membrane supports
- B01D69/107—Organic support material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23K—FEEDING FUEL TO COMBUSTION APPARATUS
- F23K5/00—Feeding or distributing other fuel to combustion apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23K—FEEDING FUEL TO COMBUSTION APPARATUS
- F23K5/00—Feeding or distributing other fuel to combustion apparatus
- F23K5/002—Gaseous fuel
- F23K5/007—Details
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/55—Compounds of silicon, phosphorus, germanium or arsenic
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/05—Biogas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2325/00—Details relating to properties of membranes
- B01D2325/20—Specific permeability or cut-off range
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- 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 combustion system for obtaining energy by burning a gas containing carbon dioxide containing methane as a main component such as biogas obtained by methane fermentation of organic matter such as biomass and organic waste.
- biogas obtained by methane fermentation of organic waste such as biomass and sewage sludge as a new energy source.
- the biogas is used in applications such as power generation or boilers as a substitute for fossil fuels.
- Biogas generally contains about 40% carbon dioxide in addition to methane, although it varies depending on the methane gas production conditions (fermentation conditions). Further, it contains a very small amount of a sulfur compound such as siloxane and hydrogen sulfide, and must be removed at the time of use.
- a sulfur compound such as siloxane and hydrogen sulfide
- digestion gas from sewage sludge processed in a relatively large facility contains many impurities such as sulfur compounds such as hydrogen sulfide (H 2 S) and siloxane.
- impurities such as sulfur compounds such as hydrogen sulfide (H 2 S) and siloxane.
- various trace components may vary depending on individual equipment and gas production conditions. Elements: V, Pb, Cl, etc., ethane, propane, dienes, benzene, toluene, etc.) are present, and their amounts and concentrations are considered to be different.
- the output and thermal efficiency of a biogas engine that uses a mixed gas of methane and carbon dioxide as fuel greatly decreases as the concentration of carbon dioxide increases.
- a gas engine uses a mixed gas containing 40% CO 2
- the engine output is reduced by 40% and the thermal efficiency is also reduced by 14% compared to methane fuel having a purity of 100%.
- methane fuel having a purity of 100%.
- a 100 kW natural gas engine is used, only a 60 kW output can be obtained.
- a 100 kW output is required, a natural gas engine of about 170 kW is required.
- the equipment cost of the engine is almost proportional to the output, so that the equipment cost increases by 70%.
- the thermal efficiency is reduced by 14%, the fuel cost is increased by about 16% compared to the natural gas engine.
- Patent Document 1 describes a biogas power generation device that controls the total number of gas engines to be driven and the drive of a surplus gas combustion device in accordance with the pressure at which biogas is supplied to the engine.
- Patent Document 2 discloses a power generation method in which carbon dioxide in digestion gas obtained by methane fermentation of organic matter such as biomass and organic waste is absorbed and separated using an alkaline absorbent, and high-purity methane gas is supplied to the engine. Is described.
- Patent Document 3 in a gas engine using a gas whose property changes during operation such as biogas as fuel, when the temperature of the exhaust gas is not within a preset range, the air-fuel ratio is corrected and controlled, A control method for a premixed gas engine that prevents engine misfire or combustion anomalies is described.
- Patent Document 4 and Patent Document 5 relate to combustion control of an engine using a mixed gas of biogas and city gas (natural gas) as a fuel.
- Patent Document 4 discloses oxygen concentration in exhaust gas
- Patent Document 5 describes exhaust gas.
- biogas is unstable in the amount and components generated depending on the conditions (fermentation conditions) when methane gas is generated. Therefore, when biogas is used as fuel, combustion becomes unstable and stable output is obtained. It may not be possible.
- the gas from which the carbon dioxide component is removed from the biogas is supplied to the engine for the above solution, the gas quality will be close to that of normal natural gas. It is done.
- the existing chemical absorption method, high-pressure water absorption method, PSA and the like are all expensive and require large-scale facilities and energy, resulting in a loss of environmental merit by using biogas.
- the cost of a purification facility for processing digestion gas of 660 Nm 3 / h is about 15 It is reported to be 300 million yen.
- the digestion gas of 660 Nm 3 / h corresponds to the rated fuel of a 2000 kW biogas engine, and the price of the 2000 kW biogas engine itself is currently about 400 million yen, so in the CO 2 removal by the existing high pressure water absorption method This increases the cost of the gas engine by about 5 times.
- the energy consumption is equivalent to approximately 15% of the energy obtained by methane combustion of biogas Yes.
- the energy required for CO 2 removal by the existing water absorption method cancels the efficiency improvement effect of the gas engine by CO 2 removal.
- the present invention can obtain a stable output without the need for complicated engine adjustment work even when using an engine that uses methane such as biogas as a main component and gas containing carbon dioxide as fuel gas.
- a combustion system comprises: A separation unit that removes carbon dioxide from the gas to be treated, which contains a mixed gas containing methane as the main component and carbon dioxide, and obtains high-purity methane gas with a reduced carbon dioxide content, and combustion that burns methane gas
- a combustion system comprising: The separation part has a first treatment chamber and a second treatment chamber separated by a separation membrane; The separation membrane selectively transmits carbon dioxide in the gas to be processed supplied to the first processing chamber to the second processing chamber, and has a higher methane purity than the gas to be processed.
- the first feature is that the first separation gas and the second separation gas in the second processing chamber containing carbon dioxide in the gas to be processed are obtained.
- the combustion system according to the first aspect of the present invention is further preferably characterized in that the separation membrane is a facilitated transport membrane to which a carrier that selectively reacts with carbon dioxide is added. .
- the combustion system according to the second aspect of the present invention preferably further includes: A water vapor supply unit for supplying water vapor to the first processing chamber; A third feature is that the mixed gas containing water vapor supplied by the water vapor supply unit is supplied to the first processing chamber as the gas to be processed.
- the combustion system according to the third aspect of the present invention preferably further includes:
- the steam supply unit supplies the steam generated by heating water by heat exchange with the high-temperature exhaust gas generated by methane combustion in the combustion unit to the first processing chamber.
- the combustion system according to the third or fourth aspect of the present invention preferably further includes:
- the fifth feature is that the water vapor supply unit supplies water vapor contained in the exhaust gas generated by the methane combustion in the combustion unit to the first processing chamber.
- the combustion system according to the present invention having any one of the third to fifth features is further preferably, An exhaust gas supply unit configured to mix at least a part of an exhaust gas containing carbon dioxide and water vapor generated by methane combustion in the combustion unit with the mixed gas and supply the mixed gas as the processing target gas to the first processing chamber; It is a sixth feature to further provide.
- a seventh feature is that the apparatus further comprises a water vapor removing unit that removes water vapor from the first separated gas and supplies the first separated gas from which the water vapor has been removed to the combustion unit.
- the combustion system according to the seventh aspect of the present invention preferably further includes:
- the eighth feature is that the steam supply section supplies the steam removed by the steam removal section to the first processing chamber.
- a ninth feature is that a sweep gas supply unit is provided for supplying a sweep gas to the second processing chamber.
- the sweep gas includes water vapor
- a tenth characteristic is that the water vapor supply unit supplies water vapor contained in the sweep gas to the sweep gas supply unit.
- the combustion system according to the eighth aspect of the present invention preferably further includes: A sweep gas supply unit for supplying a sweep gas containing water vapor to the second processing chamber;
- a sweep gas supply unit for supplying a sweep gas containing water vapor to the second processing chamber;
- the eleventh feature is that the sweep gas supply unit supplies the sweep gas containing the water vapor removed by the water vapor removal unit to the second processing chamber.
- the combustion system according to the present invention having any one of the ninth to eleventh features preferably further comprises:
- the sweep gas supply unit supplies the water vapor generated by heating water by heat exchange with the high-temperature exhaust gas generated by methane combustion in the combustion unit to the second processing chamber. It is characterized by.
- the combustion system according to the present invention having any one of the ninth to twelfth characteristics preferably further comprises
- the thirteenth feature is that the sweep gas supply unit supplies water vapor contained in the exhaust gas generated by methane combustion in the combustion unit to the second processing chamber.
- the mixed gas may be a gas derived from a biogas produced by organic methane fermentation.
- the separation membrane is a facilitated transport membrane to which a carrier that selectively reacts with carbon dioxide is added
- the separation membrane is provided with a desulfurization apparatus using an ultrahigh-order desulfurization catalyst and is derived from the biogas.
- the sulfur component (hydrogen sulfide) contained in the gas is removed.
- carbon dioxide contained in biogas or the like is removed using a separation membrane, and high purity methane gas is supplied to the combustion chamber.
- a separation membrane for removing carbon dioxide a facilitated transport membrane to which a carrier that selectively reacts with carbon dioxide is added can be suitably used.
- the removed carbon dioxide can be recovered and reused for various industrial applications.
- Carbon dioxide removal by permeation through the separation membrane requires a large membrane area to obtain a high-purity separation gas, but carbon dioxide removal as in the high-pressure water absorption method. Therefore, it is energy-saving compared to the process that consumes a large amount of energy, and the environmental merit by using biogas can be enjoyed to the maximum.
- the combustion state in the combustion chamber is detected by a method such as measuring the temperature of exhaust gas as in Patent Documents 3 to 5, for example.
- Control that controls the air-fuel ratio or mixing ratio of the fuel gas based on the combustion state, and control that detects the combustibility (methane purity) of the fuel gas and boosts the fuel gas according to the combustibility and supplies it to the combustion chamber There is something to do.
- the combustion system of the present invention by removing carbon dioxide using a separation membrane, such complicated control is not required, and the combustion state or the combustibility of the fuel gas is detected. Therefore, a low-cost engine with a simple configuration can be used. It is possible to use a general-purpose inexpensive natural gas engine.
- the water vapor to be mixed with the biogas can be separated from the mixed gas of water vapor and carbon dioxide discharged by the combustion of methane gas and reused. Furthermore, the carbon dioxide contained in the exhaust gas can be recovered and reused via the separation membrane, and it is possible to reduce the environmental load by not discharging the carbon dioxide to the external environment. .
- the schematic diagram which shows the principal part structure of the combustion system which concerns on one Embodiment of this invention The schematic diagram which shows the principal part structure of the combustion system which concerns on one Embodiment of this invention.
- the schematic diagram which shows the principal part structure of the combustion system which concerns on one Embodiment of this invention The schematic diagram which shows the principal part structure of the combustion system which concerns on one Embodiment of this invention.
- FIG. 1 schematically shows a main configuration of a combustion system 1 according to an embodiment of the present invention.
- the arrow in FIG. 1 shows the flow path and direction through which the gas flows in a simplified manner, and the chemical formula shown in FIG. 1 is conceptually included in the gas flowing in the direction of the arrow in the drawing. Represents the main ingredient.
- description of a three-way valve, a mixing valve, and the like required in the gas flow path is omitted.
- symbol shall be attached
- the combustion system 1 includes a separation unit 14 and a combustion unit 15.
- the separation unit 14 removes carbon dioxide from the gas to be treated which includes a mixed gas containing methane as a main component and carbon dioxide, and separates it into a high-purity methane gas having a reduced content of at least carbon dioxide. Then, the combustion unit 15 burns the high purity methane gas obtained by the separation unit 14.
- the combustion unit 15 is, for example, a combustion chamber of a gas engine or a gas turbine, and is provided to convert thermal energy generated by a methane gas combustion reaction into energy such as kinetic energy or electric power.
- the separation unit 14 has two processing chambers 11 and 12 separated by a separation membrane 13.
- a gas mixture containing components derived from biogas is supplied to the processing chamber 11 (first processing chamber) as a gas to be processed via the gas flow path 21.
- the mixed gas is a gas mainly composed of methane gas and containing carbon dioxide.
- impurities such as hydrogen sulfide and siloxane can be removed by using existing desulfurization equipment, activated carbon adsorption system siloxane removal equipment, etc. Used and removed in advance.
- a wet desulfurization method using an absorbing solution or an adsorptive desulfurization method using a sulfur adsorbent such as zinc oxide or iron oxide can be used.
- sulfur adsorbent such as zinc oxide or iron oxide
- sulfur adsorbent such as zinc oxide or iron oxide
- sulfur can be completely removed to a level of ppb or lower.
- an ultrahigh-order desulfurization catalyst because the facilitated transport membrane may be affected by hydrogen sulfide depending on the type of carrier used and its concentration.
- the separation membrane 13 has a function of selectively transmitting the carbon dioxide gas contained in the gas to be processed to the processing chamber 12 (second processing chamber) side with a transmittance higher than that of methane gas. . Thereby, the purity of the carbon dioxide of the gas in the process chamber 11 falls, and the purity of methane gas rises. On the other hand, the purity of the carbon dioxide gas in the processing chamber 12 increases.
- the purity of the gas refers to the molar concentration ratio of the gas component to the total gas (that is, equal to the ratio of the gas partial pressures). This is the same in the following description.
- the separation membrane 13 is preferably composed of a facilitated transport membrane.
- the facilitated transport film is a film formed by adding a carrier that selectively reacts with a specific gas molecule (here, carbon dioxide) into, for example, a gel film. A specific configuration of the facilitated transport film will be described later.
- the “carrier” is a substance having the effect of increasing the permeation rate of a specific gas by containing the substance in the film.
- CO 2 recovery and recovery process can be achieved compared to the current chemical absorption method and the more expensive PSA (Pressure Swing Adsorption) method.
- PSA Pressure Swing Adsorption
- CO 2 recovery from power generation exhaust gas, steel manufacturing exhaust gas, cement exhaust gas, etc., and next-generation energy processes such as CTL (Coal to Liquids: liquid fuel production from coal) It can also be applied to small-scale chemical plants and facilities that could not be applied to the existing decarbonation field, and CO 2 can be easily separated and recovered, which is expected to contribute greatly to a low-carbon society.
- the gas to be processed containing methane gas and carbon dioxide gas has a first separation gas in the processing chamber 11 in which the purity of the methane gas is higher than that of the gas to be processed and the purity of the carbon dioxide gas is lower. Separated into a second separation gas.
- the first separation gas is sent to the combustion section 15 via the gas flow path 23, the water vapor separation section 16, and the gas flow path 24, and methane gas is used for combustion.
- the second separation gas contains a large amount of carbon dioxide, and can be recovered and reused for various industrial uses.
- the separation membrane 13 is a facilitated transport membrane, if there is no moisture in the separation membrane 13, the carbon dioxide permeation rate is generally very small. Therefore, moisture in the membrane is indispensable to obtain a high permeation rate. It is.
- One method for maintaining moisture in the separation membrane 13 is to configure the gel layer with a hydrogel having high water retention. This makes it possible to retain moisture in the membrane as much as possible even at high temperatures where the moisture content in the separation functional layer is reduced. For example, high selective permeation performance can be realized at high temperatures of 100 ° C. or higher.
- moisture water vapor
- water vapor gas steam
- a mixed gas containing methane gas and carbon dioxide gas a mixed gas containing methane gas and carbon dioxide gas
- the mixed gas containing water vapor passes through the gas flow path 21. It is supplied to the processing chamber 11 of the separation unit 14.
- the relative humidity of the gas to be treated containing water vapor is preferably 30% to 100%, more preferably 40% to 100%.
- the gas to be treated containing water vapor may be pressurized or heated.
- the pressure for boosting is preferably 200 kPa (A) to 1000 kPa (A), more preferably 400 kPa (A) to 1000 kPa (A), taking into account the energy required for boosting.
- the temperature may be about room temperature, but the carbon dioxide permeation performance tends to increase with temperature, and is preferably 60 ° C. to 130 ° C., more preferably 80 ° C. to 120 ° C.
- the first separation gas is a gas containing methane gas and water vapor although the purity of carbon dioxide is low.
- the first separation gas is a gas containing methane gas and water vapor although the purity of carbon dioxide is low.
- the water vapor removing unit 16 is provided between the treatment chamber 11 and the combustion chamber of the combustion unit 15, and the water vapor removing unit 16 removes the water vapor mixed by the water vapor supply unit 17 from the first separation gas.
- the high-purity methane gas after removing the water vapor is supplied to the combustion unit 15.
- a known configuration using a water vapor permeable membrane such as a condenser or a perfluoro-based membrane (or a perfluorosulfonic acid-based membrane) can be used.
- the facilitated transport membrane may be composed of a material different from that of the separation membrane 13 or the same material.
- the water vapor removed by the water vapor removing unit 16 is added to the gas to be treated, it can be supplied to the water vapor supplying unit 17 through the gas flow path 25.
- the method for supplying water vapor by the water vapor supply unit 17 is not limited to the method using the water vapor removed by the water vapor removal unit 16. Although energy is consumed separately, water may be heated to generate water vapor. In this case, energy can be saved by using the high-temperature exhaust gas generated by methane combustion in the combustion unit 15 and heating the water by heat exchange with the high-temperature exhaust gas to generate water vapor. Further, as will be described later, it is possible to reuse the water vapor contained in the exhaust gas after the methane combustion reaction.
- the sweep gas is supplied from the gas flow path 22 (sweep gas supply unit).
- the sweep gas preferably contains water vapor gas.
- the water vapor supply unit 17 can supply water vapor to the processing chamber 12 so that water vapor is included in the sweep gas, in addition to supplying the gas to be processed to which water vapor has been added to the processing chamber 11.
- the water vapor contained in the sweep gas like the water vapor supplied to the processing chamber 11, can be expected to save energy by heating and producing water by heat exchange with the high-temperature exhaust gas produced by methane combustion. In addition, as described later, it is possible to reuse the water vapor contained in the exhaust gas after the methane combustion reaction.
- the partial pressure difference of the water vapor gas between the supply side (processing chamber 11) and the permeation side (processing chamber 12) is reduced, and the water vapor in the gas to be processed
- the gas permeation amount it is possible to suppress a decrease in the relative humidity of the gas to be processed.
- the higher the CO 2 recovery rate the lower the relative humidity of the gas in the processing chamber 12 (second separation gas) because the ratio of the water vapor gas on the permeate side becomes lower.
- the water vapor gas contained in the sweep gas is reduced. A decrease in relative humidity can be suppressed by increasing the flow rate.
- the gas to be processed containing methane and carbon dioxide is supplied to the processing chamber 11, and the carbon dioxide in the gas to be processed is transmitted through the separation membrane 13 with a higher transmittance than methane.
- High-purity methane gas containing almost no carbon can be supplied to the combustion section 15.
- the gas engine can obtain a stable output without the need for complicated engine adjustment work even when biogas is used as fuel. Therefore, it can be expected to reduce size and output.
- Second Embodiment 2 to 6 schematically show other configuration examples of the combustion system of the present invention.
- the combustion systems 2 to 6 shown in FIGS. 2 to 6 enable the exhaust gas generated by the combustion reaction of methane to be reused in the combustion unit 15.
- the water vapor gas is a sweep gas supplied to the second processing chamber 12 of the separation unit or mixed with the gas to be processed, so that the moisture in the separation membrane is maintained even at high temperature conditions as described above, and a high transmittance is obtained. Can be obtained.
- the load of exhaust gas on the environment can be reduced.
- various industrial uses are also possible by increasing the purity.
- the exhaust gas generated in the combustion unit 15 is mixed with the water vapor from the water vapor supply unit 17 and supplied as a sweep gas.
- the structure which utilizes effectively the water vapor
- carbon dioxide is contained in the exhaust gas, it is necessary to adjust the mixing ratio and flow rate of water vapor so that the partial pressure of carbon dioxide in the sweep gas does not exceed the partial pressure of carbon dioxide in the gas to be treated There is.
- the composition of the exhaust gas after methane combustion, the ratio of nitrogen and oxygen in the air 4: 1, and, when all the oxygen in taken into the combustion chamber air is used without excess or deficiency of methane combustion, CO 2 : H 2 O: N 2 1: 2: 8.
- the exhaust gas is used as the sweep gas for the facilitated transport film, it is necessary to supply the pressurized exhaust gas to the processing chamber 12 in order to obtain the above-mentioned preferable relative humidity.
- the partial pressure of contained carbon dioxide also increases, and the propulsive force necessary for the selective permeation of carbon dioxide may be reduced. For this reason, in general, in order to obtain high selection performance by using the exhaust gas as the sweep gas for the facilitated transport membrane, water vapor is separately added to the sweep gas.
- the facilitated transport membrane non-permselective membrane e.g. the solution-diffusion mechanism according to the CO 2 separation membrane
- the facilitated transport membrane non-permselective membrane requires no moisture membrane permeation, only directly, put the exhaust gas to the permeate side, the effect of the sweep gas Can be expected.
- the water vapor separation unit 18 is provided on the flow path 26 through which the exhaust gas from the combustion unit flows.
- the water vapor separation unit 18 separates the water vapor contained in the exhaust gas.
- the separated water vapor can be mixed with the sweep gas or the gas to be processed via the water vapor supply unit 17.
- a known configuration using a water vapor permeable membrane can be used as in the water vapor remover 16.
- a facilitated transport membrane can also be used in the water vapor separation part.
- the gas containing carbon dioxide and nitrogen remaining after the water vapor separation can be used as a sweep gas supplied to the processing chamber 12 (not shown) as in the combustion system of FIG.
- the exhaust gas from the combustion unit 15 is processed in the treatment chamber (supply side) 31 of the separation unit 34 provided with a separation membrane 33 (CO 2 facilitated transport membrane) separate from the separation unit 14. Supplied in.
- the exhaust gas component contains nitrogen gas resulting from the intake of oxygen necessary for combustion from the air.
- the permeate side treatment is performed in the chamber 32.
- a gas containing carbon dioxide and water vapor from which nitrogen is removed is obtained. This gas can be used in various industries as high-purity carbon dioxide gas by removing the water vapor component.
- a sweep gas can be flowed into the processing chamber 32. As the sweep gas, water vapor is preferable.
- the water vapor supply unit 17 can supply water vapor mixed with the exhaust gas in the processing chamber 31 to obtain a high carbon dioxide permeation rate and water vapor supplied into the processing chamber 32 as a sweep gas.
- the combustion system 5 shown in FIG. 5 is the same as the combustion system 4 in FIG. 4 in that a separation unit 34 for removing nitrogen in the exhaust gas is provided, but carbon dioxide and water vapor obtained by nitrogen separation are used.
- the contained gas is mixed with the biogas by the exhaust gas supply unit 19, and the mixed gas is supplied to the supply side (processing chamber 11) of the separation unit 14 as the gas to be processed.
- carbon dioxide in the exhaust gas selectively permeates through the separation membrane 33 of the separation unit 34 and further selectively permeates through the separation membrane 13 of the separation unit 14 and is recovered as the second separation gas in the processing chamber 12.
- the recovered carbon dioxide gas can be used in various industries as high-purity carbon dioxide gas after the water vapor is removed.
- the combustion system shown in FIG. 6 has a configuration in which the processing chamber 12 of the separation unit 14 to which the sweep gas is supplied and the processing chamber 32 of the separation unit 34 are shared in the configuration of FIG. Instead of the separation parts 14 and 34, a separation part 35 is provided.
- the separation unit 35 is divided into three processing chambers by the separation membranes 13 and 33.
- a mixed gas of biogas and water vapor supplied from the water vapor supply unit 17 is supplied as a gas to be processed.
- the processing chamber 38 separated by the separation membrane 33 is supplied with a mixed gas obtained by mixing the exhaust gas after methane combustion with the water vapor supplied from the water vapor supply unit 17.
- the processing chamber 37 separated by both the separation membrane 13 and the separation membrane 33 is supplied with water vapor gas as a sweep gas, and carbon dioxide gas contained in the biogas is transferred from the processing chamber 36 through the separation membrane 13 to the processing chamber.
- the carbon dioxide gas in the exhaust gas is selectively permeated into the processing chamber 37 from the processing chamber 38 through the separation membrane 33.
- the combustion section 15 can reuse the water vapor gas or carbon dioxide gas in the exhaust gas generated by the combustion reaction of methane.
- the carbon dioxide gas generated by the combustion is recovered through the separation membrane 13 or 33, so that the carbon dioxide is not released to the external environment. It becomes possible to reduce.
- the separation membranes 13 and 33 are CO 2 facilitated transport membranes and have a structure in which a carrier that selectively reacts with CO 2 is contained in the gel membrane as described above.
- the CO 2 carrier include cesium carbonate or cesium bicarbonate, or alkali metal carbonates or bicarbonates such as rubidium carbonate or rubidium bicarbonate.
- an alkali metal hydroxide such as cesium hydroxide or rubidium hydroxide can be said to be equivalent because it reacts with carbon dioxide to produce a carbonate or heavy carbonate.
- amino acids such as 2,3-diaminopropionate (DAPA) and glycine are known to exhibit high CO 2 permeation performance.
- CO 2 facilitated transport membrane the above carrier gel layer that is configured to include in the gel film, it can be made by supporting the hydrophilic or hydrophobic porous membrane.
- the film material constituting the gel film include a polyvinyl alcohol (PVA) film, a polyacrylic acid (PAA) film, and a polyvinyl alcohol-polyacrylic acid (PVA / PAA) salt copolymer film.
- PVA polyvinyl alcohol
- PAA polyacrylic acid
- PAA polyvinyl alcohol-polyacrylic acid
- the gel film is preferably a hydrogel film.
- the polyvinyl alcohol-polyacrylic acid (PVA / PAA) salt copolymer film and the polyacrylic acid film are hydrogel films.
- the hydrogel is a three-dimensional network structure formed by crosslinking a hydrophilic polymer by chemical crosslinking or physical crosslinking, and has a property of swelling by absorbing water.
- a catalyst that accelerates the reaction between the CO 2 carrier and CO 2 may be contained in the membrane.
- a catalyst preferably contains a carbonic anhydrase or an oxo acid compound, and in particular, an oxo acid of at least one element selected from the group 14 element, group 15 element, and group 16 element It is preferable that the composition includes a compound.
- the catalyst preferably includes at least one of a tellurite compound, a selenite compound, an arsenite compound, and an orthosilicate compound.
- the CO 2 facilitated transport film 13 (33) is composed of a gel film composed of a hydrogel containing a carbon dioxide carrier and a porous film carrying the gel film.
- the film structure of CO 2 -facilitated transport membrane the present invention is not limited to the specific examples, which was to form a gel film containing carrier, for example, in the outer peripheral side or the inner circumference side of the porous support of cylindrical shape It does not matter.
- a cast solution made of an aqueous solution containing a PVA / PAA salt copolymer, a CO 2 carrier (here, Cs 2 CO 3 ), and a CO 2 hydration reaction catalyst is prepared (step 1). More specifically, 2 g of a polyvinyl alcohol-polyacrylic acid (PVA / PAA) salt copolymer (for example, SS gel manufactured by Sumitomo Seika), 4.67 g of cesium carbonate, and 0.80 with respect to cesium carbonate. 025 times the number of moles of potassium tellurite is added to 80 g of water and stirred until dissolved to obtain a cast solution.
- the cast solution obtained in Step 1 is cast on the PTFE porous membrane with an applicator (Step 2). Thereafter, the cast solution is gelled by drying to form a gel layer (step 3).
- the CO 2 carrier constituting the CO 2 facilitated transport membrane As the CO 2 carrier constituting the CO 2 facilitated transport membrane, the above-mentioned Cs 2 CO 3 is used, and a membrane in which a CO 2 carrier is added to a hydrogel mainly composed of a PVA / PAA salt copolymer as a hydrogel membrane, It was carried on a hydrophobic PTFE porous membrane to form a separation membrane 13.
- the gas to be treated was a mixed gas containing nitrogen, carbon dioxide, and water vapor (in place of methane) as described above.
- the processing temperature was 110 ° C.
- the total pressure of the gas to be processed was kept constant at 900 kPa
- the partial pressure of the water vapor gas supplied to the processing chamber 11 was changed.
- the sweep gas is water vapor gas or a mixed gas of water vapor and Ar.
- the partial pressure of the water vapor gas is the same as that of the gas to be treated. Under conditions 1 and 2, the sweep gas is set so that the total pressure is 100 kPa (atmospheric pressure). Ar gas was added.
- FIG. 7 shows the evaluation results of the temperature, the pressure of the gas to be treated and the sweep gas, the composition ratio (partial pressure ratio), the relative humidity, the CO 2 permeance and the N 2 permeance under each evaluation condition.
- the N 2 permeance is “below the GC detection limit” because the N 2 concentration in the second separation gas that has passed through the separation membrane 13 is too low, and N 2 is detected by gas chromatography. This means that the permeance could not be calculated.
- the N 2 permeance in this case is estimated to be 1.37 ⁇ 10 ⁇ 8 [mol / m 2 s ⁇ kPa] at most.
- CO 2 selectivity to N 2 (CH 4) can be expressed as the ratio of the CO 2 permeance for N 2 (CH 4) permeance.
- FIG. 7 shows that the CO 2 facilitated transport membrane has a CO 2 / N 2 selectivity exceeding 500. Therefore, the CO 2 / CH 4 selectivity has the same selection performance.
- the evaluation condition 1 ⁇ 3, CO 2 permeance as the relative humidity increases is high.
- Such humidity dependence is considered to be a feature of the facilitated transport film.
- the facilitated transport membrane has a very high CO 2 permeance and selectivity as compared with other separation membranes (separation membranes having a dissolution / diffusion mechanism, etc.) particularly in a high humidity region.
- the flow rate of the gas to be processed (excluding water vapor) supplied to the processing chamber 11 was set to 330 Nm 3 / h.
- the CO 2 permeance was set to a constant value (the value shown in FIG. 7) regardless of the membrane area.
- the facilitated transport membrane is characterized in that the CO 2 permeance increases as the CO 2 partial pressure difference between the supply side (processing chamber 11 side) and the permeation side (processing chamber 12 side) decreases (for example, Japanese Patent Application No. 2015-223893). reference). Therefore, in actuality, the CO 2 permeance becomes closer to the outlet side of the membrane (near the channel 23) from the inlet side of the membrane (near the channel 21) due to the distribution of the partial pressure of CO 2 in the processing chamber 11 on the membrane. Get higher. Therefore, when the facilitated transport film is used, it is considered that the actually required film area is smaller than the calculated value.
- the required film area was 575 m 2 in the case of the evaluation condition 1, and 250 m 2 in the case of the evaluation condition 3. Although it has a relatively large area, it can be sufficiently realized as a combustion system for biogas combustion by combining a plurality of membrane modules.
- the carbon dioxide contained in the biogas is removed through the CO 2 separation membrane, and the high-purity methane gas after the removal is supplied to the combustion chamber. It is possible to realize a combustion system capable of obtaining a stable output while saving energy and enjoying the maximum environmental merit.
- the separation membranes (CO 2 facilitated transport membranes) 13 and 33 are flat membranes.
- the present invention is not limited to this, and the inner surface of a cylindrical porous membrane is used. Alternatively, it may be a curved surface having a gel layer containing a carrier on the outer surface or a hollow fiber membrane.
- the present invention does not depend on the arrangement of the processing chambers in each processing section, and a configuration in which a plurality of cylindrical processing chambers having a common axis are separated by a CO 2 facilitated transport membrane or a permeable membrane, A configuration in which the processing chambers are arranged in series in the extending direction of the axial center can be considered.
- a gel membrane composed of a polyvinyl alcohol-polyacrylate copolymer is used as a material for the CO 2 facilitated transport membrane.
- CO 2 selective separation ability It is possible to adopt the same hydrophilic polymer that exhibits the above.
- the CO 2 carrier is not limited to the materials mentioned in the embodiment, and other material films may be adopted as long as the desired CO 2 selective permeation performance is obtained.
- water vapor is used as the sweep gas.
- the sweep gas flowing into the processing chamber 12 of the separation unit 14 the processing chamber 32 of the separation unit 34, or the processing chamber 37 of the separation unit 35.
- the sweep gas may contain a gas component such as nitrogen gas or argon gas.
- the gas component is contained in the second separation gas, a step of separating the gas component is separately required when assuming the reuse of the carbon dioxide gas in the second separation gas.
- the sweep gas supplied to the processing chamber 32 can be a mixed gas containing a gas component other than water vapor, but the gas component is mixed with biogas, Since it is circulated and supplied into the processing chamber 11, a step of removing the gas component before the combustion unit 15 is required.
- the sweep gas flowing into the processing chambers 12, 32 (FIG. 4) and 37 can be easily separated from the carbon dioxide gas if the reuse of the carbon dioxide gas in the second separation gas is taken into consideration. It is preferable that water vapor gas is suitable.
- the sweep gas that flows into the processing chamber 32 of FIG. 5 is preferably one that can be easily separated from methane gas and carbon dioxide gas, and is preferably water vapor gas.
- Steam gas is mixed with a part of the second separation gas in the processing chambers 12 and 37, a part of the permeated gas in the processing chamber 32, or a part of the exhaust gas after methane combustion, and the mixed gas is reused as a sweep gas. It can also be used.
- the mixed gas contains carbon dioxide, it is necessary to adjust the mixing ratio of the water vapor gas so that the partial pressure of carbon dioxide in the sweep gas is lower than the partial pressure of carbon dioxide in the gas to be treated. .
- combustion systems 1 to 6 shown in FIGS. 1 to 6 are given as examples of the configuration of the combustion system.
- the present invention is not limited to these specific configurations.
- a person skilled in the art can easily configure another combustion system by appropriately combining a part or all of the configurations of the combustion systems 1 to 6 as long as there is no contradiction as a whole.
- the configurations suggested by such combustion systems 1 to 6 can also be said to be disclosed in the present specification.
- the present invention can be used for a combustion system that uses a mixed gas in which carbon dioxide gas is contained in a combustible gas, such as a biogas obtained by methane fermentation of organic matter, as a fuel.
- a mixed gas in which carbon dioxide gas is contained in a combustible gas, such as a biogas obtained by methane fermentation of organic matter, as a fuel.
- Combustion system 14 Separation unit 11: First treatment chamber 12: Second treatment chamber 13: Separation membrane 15: Combustion unit 16: Water vapor removal unit 17: Water vapor supply unit 18: Water vapor separation unit 19: Exhaust gas supply Part 21 to 26: Gas flow path 34, 35: Separation part 31, 32, 36 to 38: Processing chamber 33: Separation membrane
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Abstract
Description
メタンを主成分として二酸化炭素を含む混合ガスを成分とする被処理ガスから二酸化炭素を除去し、少なくとも二酸化炭素の含有量が低減された高純度のメタンガスを得る分離部と、メタンガスを燃焼させる燃焼部とを備えた燃焼システムであって、
前記分離部が、分離膜によって隔てられた第1処理室と第2処理室を有し、
前記分離膜が、前記第1処理室に供給された前記被処理ガス中の二酸化炭素を選択的に前記第2処理室へと透過させ、前記被処理ガスよりメタン純度の高い前記第1処理室内の第1分離ガスと、前記被処理ガス中の二酸化炭素を含む前記第2処理室内の第2分離ガスを得る構成としたことを第1の特徴とする。
前記第1処理室に水蒸気を供給する水蒸気供給部を備え、
前記水蒸気供給部により供給される水蒸気を含む前記混合ガスが、前記被処理ガスとして、前記第1処理室に供給されることを第3の特徴とする。
前記水蒸気供給部は、前記燃焼部でのメタン燃焼により生成された高温の排出ガスとの熱交換により水を加熱して生成された水蒸気を、前記第1処理室に供給することを第4の特徴とする。
前記水蒸気供給部は、前記燃焼部でのメタン燃焼により生成された排出ガスに含まれる水蒸気を、前記第1処理室に供給することを第5の特徴とする。
前記燃焼部でのメタン燃焼により生成された二酸化炭素及び水蒸気を含んだ排出ガスの少なくとも一部を前記混合ガスと混合し、前記被処理ガスとして前記第1処理室に供給する排出ガス供給部を更に備えることを第6の特徴とする。
前記第1分離ガスから水蒸気を除去し、水蒸気が除去された前記第1分離ガスを前記燃焼部に供給する水蒸気除去部を更に備えることを第7の特徴とする。
前記水蒸気供給部は、前記水蒸気除去部によって除去された水蒸気を、前記第1処理室に供給することを第8の特徴とする。
前記第2処理室にスイープガスを供給するスイープガス供給部を備えることを第9の特徴とする。
前記水蒸気供給部が、前記スイープガスに含まれる水蒸気を前記スイープガス供給部に供給することを第10の特徴とする。
前記第2処理室に水蒸気を含んだスイープガスを供給するスイープガス供給部を備え、
前記スイープガス供給部は、前記水蒸気除去部によって除去された水蒸気を含んだ前記スイープガスを、前記第2処理室に供給することを第11の特徴とする。
前記スイープガス供給部は、前記燃焼部でのメタン燃焼により生成された高温の排出ガスとの熱交換により水を加熱して生成された水蒸気を、前記第2処理室に供給することを第12の特徴とする。
前記スイープガス供給部は、前記燃焼部でのメタン燃焼により生成された排出ガスに含まれる水蒸気を、前記第2処理室に供給することを第13の特徴とする。
図2~図6に、本発明の燃焼システムの他の構成例を模式的に示す。図2~図6に示す燃焼システム2~6は、燃焼部15において、メタンの燃焼反応によって生成された排出ガスの再利用を可能としたものである。
分離膜13及び33は、CO2促進輸送膜であり、前述の通り、ゲル膜中にCO2と選択的に反応するキャリアを含有させた構造になっている。CO2キャリアとしては、例えば、炭酸セシウム若しくは重炭酸セシウム、又は、炭酸ルビジウム若しくは重炭酸ルビジウム等のアルカリ金属の炭酸化物又は重炭酸化物が挙げられる。同様に、水酸化セシウム又は水酸化ルビジウム等のアルカリ金属の水酸化物も、二酸化炭素と反応して炭酸化物や重炭酸化物が生成されるため、等価物といえる。他には、2,3‐ジアミノプロピオン酸塩(DAPA)、グリシンといったアミノ酸が、高いCO2選択透過性能を示すことが知られている。
以下に、CO2促進輸送膜(分離膜13及び33)の製造方法について説明する。
以下に、上記の製造方法で製膜されたCO2促進輸送膜について二酸化炭素の選択透過性の評価結果を示す。
上記評価条件1~3の膜性能評価結果をもとに、第1分離ガスの出口(ガス流路23近傍)側メタン濃度(純度)が90%以上となるために必要な膜面積を計算した結果を示す。必要膜面積の評価に際し、上記評価条件1又は3における被処理ガス組成、スイープガス組成、及び膜透過性能をシミュレータに代入し、膜面積及びスイープガスの流量を変えながら、メタン濃度(純度)が90%以上となる最小の膜面積を求めた。CH4パーミアンスについては、上述の通り、N2パーミアンスを0.74倍した値を採用した。ただし、評価条件1では、N2パーミアンスがGC検出限界以下であるため、評価条件3でのN2パーミアンスを0.74倍した値を評価条件1におけるCH4パーミアンスとして採用した(したがって、実際のCH4パーミアンスはこれよりも低い値と考えられる)。また、処理室11に供給する被処理ガスの流量(水蒸気を除く)は、330Nm3/hに設定した。
以下に、別実施形態について説明する。
14:分離部
11: 第1処理室
12: 第2処理室
13: 分離膜
15: 燃焼部
16: 水蒸気除去部
17: 水蒸気供給部
18: 水蒸気分離部
19: 排出ガス供給部
21~26: ガス流路
34、35: 分離部
31、32、36~38: 処理室
33: 分離膜
Claims (15)
- メタンを主成分として二酸化炭素を含む混合ガスを成分とする被処理ガスから二酸化炭素を除去し、少なくとも二酸化炭素の含有量が低減された高純度のメタンガスを得る分離部と、メタンガスを燃焼させる燃焼部とを備えた燃焼システムであって、
前記分離部が、分離膜によって隔てられた第1処理室と第2処理室を有し、
前記分離膜が、前記第1処理室に供給された前記被処理ガス中の二酸化炭素を選択的に前記第2処理室へと透過させ、前記被処理ガスよりメタン純度の高い前記第1処理室内の第1分離ガスと、前記被処理ガス中の二酸化炭素を含む前記第2処理室内の第2分離ガスを得る構成であることを特徴とする燃焼システム。 - 前記分離膜が、二酸化炭素と選択的に反応するキャリアが添加された促進輸送膜であることを特徴とする請求項1に記載の燃焼システム。
- 前記第1処理室に水蒸気を供給する水蒸気供給部を備え、
前記水蒸気供給部により供給される水蒸気を含む前記混合ガスが、前記被処理ガスとして、前記第1処理室に供給されることを特徴とする請求項2に記載の燃焼システム。 - 前記水蒸気供給部は、前記燃焼部でのメタン燃焼により生成された高温の排出ガスとの熱交換により水を加熱して生成された水蒸気を、前記第1処理室に供給することを特徴とする請求項3に記載の燃焼システム。
- 前記水蒸気供給部は、前記燃焼部でのメタン燃焼により生成された排出ガスに含まれる水蒸気を、前記第1処理室に供給することを特徴とする請求項3又は4に記載の燃焼システム。
- 前記燃焼部でのメタン燃焼により生成された二酸化炭素及び水蒸気を含んだ排出ガスの少なくとも一部を前記混合ガスと混合し、前記被処理ガスとして前記第1処理室に供給する排出ガス供給部を更に備えることを特徴とする請求項3~5の何れか一項に記載の燃焼システム。
- 前記第1分離ガスから水蒸気を除去し、水蒸気が除去された前記第1分離ガスを前記燃焼部に供給する水蒸気除去部を更に備えることを特徴とする請求項3~6の何れか一項に記載の燃焼システム。
- 前記水蒸気供給部は、前記水蒸気除去部によって除去された水蒸気を、前記第1処理室に供給することを特徴とする請求項7に記載の燃焼システム。
- 前記第2処理室にスイープガスを供給するスイープガス供給部を備えることを特徴とする請求項2~8の何れか一項に記載の燃焼システム。
- 前記スイープガスが、水蒸気を含み、
前記水蒸気供給部が、前記スイープガスに含まれる水蒸気を前記スイープガス供給部に供給することを特徴とする請求項9に記載の燃焼システム。 - 前記第2処理室に水蒸気を含んだスイープガスを供給するスイープガス供給部を備え、
前記スイープガス供給部は、前記水蒸気除去部によって除去された水蒸気を含んだ前記スイープガスを、前記第2処理室に供給することを特徴とする請求項7に記載の燃焼システム。 - 前記スイープガス供給部は、前記燃焼部でのメタン燃焼により生成された高温の排出ガスとの熱交換により水を加熱して生成された水蒸気を、前記第2処理室に供給することを特徴とする請求項9~11の何れか一項に記載の燃焼システム。
- 前記スイープガス供給部は、前記燃焼部でのメタン燃焼により生成された排出ガスに含まれる水蒸気を、前記第2処理室に供給することを特徴とする請求項9~12の何れか一項に記載の燃焼システム。
- 前記混合ガスが、有機物のメタン発酵により生成されたバイオガスに由来するガスを含むことを特徴とする請求項1~13の何れか一項に記載の燃焼システム。
- 前記分離膜が、二酸化炭素と選択的に反応するキャリアが添加された促進輸送膜であり、
前記バイオガスに由来するガス中に含まれる硫黄成分を除去する超高次脱硫触媒を用いた脱硫装置を備えることを特徴とする請求項14に記載の燃焼システム。
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