CN112358899A - System and method for preparing liquefied natural gas from biogas - Google Patents
System and method for preparing liquefied natural gas from biogas Download PDFInfo
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- CN112358899A CN112358899A CN202011349959.8A CN202011349959A CN112358899A CN 112358899 A CN112358899 A CN 112358899A CN 202011349959 A CN202011349959 A CN 202011349959A CN 112358899 A CN112358899 A CN 112358899A
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- adsorption
- biogas
- adsorbent
- adsorption unit
- tail gas
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- 238000000034 method Methods 0.000 title claims abstract description 70
- 239000003949 liquefied natural gas Substances 0.000 title claims abstract description 56
- 238000001179 sorption measurement Methods 0.000 claims abstract description 241
- 239000007789 gas Substances 0.000 claims abstract description 168
- 239000003463 adsorbent Substances 0.000 claims abstract description 137
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 60
- 238000003795 desorption Methods 0.000 claims abstract description 50
- 230000008929 regeneration Effects 0.000 claims abstract description 24
- 238000011069 regeneration method Methods 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims description 71
- 238000010521 absorption reaction Methods 0.000 claims description 48
- 239000007921 spray Substances 0.000 claims description 44
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 42
- 238000005262 decarbonization Methods 0.000 claims description 25
- 238000010438 heat treatment Methods 0.000 claims description 22
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 21
- 239000001569 carbon dioxide Substances 0.000 claims description 21
- 238000006477 desulfuration reaction Methods 0.000 claims description 17
- 230000023556 desulfurization Effects 0.000 claims description 17
- 238000003860 storage Methods 0.000 claims description 17
- 238000001816 cooling Methods 0.000 claims description 14
- 238000011049 filling Methods 0.000 claims description 14
- 238000002360 preparation method Methods 0.000 claims description 14
- 238000004332 deodorization Methods 0.000 claims description 9
- 238000010248 power generation Methods 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 239000000446 fuel Substances 0.000 claims description 7
- 238000004891 communication Methods 0.000 claims description 6
- 230000006837 decompression Effects 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 6
- 239000003507 refrigerant Substances 0.000 claims description 4
- 238000007781 pre-processing Methods 0.000 claims description 3
- 230000002045 lasting effect Effects 0.000 claims 1
- 239000002028 Biomass Substances 0.000 abstract description 2
- 238000000746 purification Methods 0.000 abstract description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 18
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 238000005261 decarburization Methods 0.000 description 12
- 239000002250 absorbent Substances 0.000 description 10
- 230000002745 absorbent Effects 0.000 description 10
- 238000010586 diagram Methods 0.000 description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 9
- 238000002485 combustion reaction Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 5
- 238000006392 deoxygenation reaction Methods 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 125000004122 cyclic group Chemical group 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 4
- 238000006297 dehydration reaction Methods 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- 238000003912 environmental pollution Methods 0.000 description 4
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 4
- 229910052753 mercury Inorganic materials 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 230000001877 deodorizing effect Effects 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 229910001447 ferric ion Inorganic materials 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 210000003608 fece Anatomy 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 229910001448 ferrous ion Inorganic materials 0.000 description 1
- 238000005429 filling process Methods 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- -1 iron ion Chemical class 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000011085 pressure filtration Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/103—Sulfur containing contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/105—Removal of contaminants of nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
- F25J1/023—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock for the combustion as fuels, i.e. integration with the fuel gas system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/66—Landfill or fermentation off-gas, e.g. "Bio-gas"
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/62—Separating low boiling components, e.g. He, H2, N2, Air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/64—Separating heavy hydrocarbons, e.g. NGL, LPG, C4+ hydrocarbons or heavy condensates in general
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Physics & Mathematics (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Separation Of Gases By Adsorption (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention relates to the technical field of biomass gas purification, in particular to a system and a method for preparing liquefied natural gas from methane. The tail gas generated in the liquefaction process is used as regeneration gas to regenerate the adsorbent. The embodiment of the invention provides a system for preparing liquefied natural gas from biogas, which is characterized by comprising the following components: the pretreatment device comprises an adsorption unit, the adsorption unit comprises an adsorption channel and a desorption channel, wherein the inlet of the desorption channel is communicated with the first inlet of the adsorption channel, an adsorbent is arranged in the adsorption channel, and the adsorbent is used for adsorbing odor in the biogas; the liquefying device is used for liquefying the methane treated by the pretreatment device to obtain liquefied natural gas and tail gas, and comprises a tail gas outlet which is communicated with the inlet of the desorption channel.
Description
Technical Field
The invention relates to the technical field of biomass gas purification, in particular to a system and a method for preparing liquefied natural gas from methane.
Background
The biogas is a combustible and odorous gas generated by the fermentation of organic substances (such as human and animal excreta, straws, sewage and other organic substances) under anaerobic conditions through microorganisms. Landfill gas is one of the biogas.
The main component of the biogas is methane, and besides methane, the biogas also contains gases such as carbon dioxide, nitrogen, oxygen, hydrogen sulfide and the like and some solid particles.
Disclosure of Invention
The invention mainly aims to provide a system and a method for preparing liquefied natural gas from biogas. The tail gas generated in the liquefaction process is used as regeneration gas to regenerate the adsorbent.
In order to achieve the purpose, the invention adopts the following technical scheme:
in one aspect, an embodiment of the present invention provides a system for preparing liquefied natural gas from biogas, including: the biogas digester comprises a pretreatment device and a liquefaction device, wherein the pretreatment device comprises an adsorption unit, the adsorption unit comprises an adsorption channel and a desorption channel, an inlet of the desorption channel is communicated with a first inlet of the adsorption channel, an adsorbent is arranged in the adsorption channel, and the adsorbent is used for adsorbing odor in biogas; the liquefaction device is used for liquefying the methane treated by the pretreatment device to obtain liquefied natural gas and tail gas, and comprises a tail gas outlet which is communicated with the inlet of the desorption channel.
In some embodiments, the system further comprises: a power generation device comprising a fuel inlet; the outlet of the desorption passage communicates with the fuel inlet.
In some embodiments, the pretreatment device further comprises a decarbonization unit connected in series with an outlet of the adsorption channel of the adsorption unit, the decarbonization unit comprises a carbon dioxide exhaust port connected with a deodorization tank, and a bypass pipeline connected in parallel with the deodorization tank, and a first valve is arranged on the bypass pipeline.
In some embodiments, the liquefaction plant comprises a plurality of stages of condensing devices and a liquid storage tank in communication with the liquid outlet of each stage of condensing devices in the plurality of stages of condensing devices;
the multistage condensing device further comprises a heat exchange channel, a gas outlet of the last stage of liquid storage tank is communicated with an inlet of the heat exchange channel, and an outlet of the heat exchange channel is used as the tail gas outlet.
In some embodiments, the liquefaction plant further comprises a filling channel having a filling boil-off gas outlet in communication with the inlet of the heat exchange channel.
In some embodiments, the adsorption unit is a plurality of adsorption units, the adsorption channels of the adsorption units are connected in parallel, the desorption channels of the adsorption units are connected in parallel, and a second valve is connected in series to each adsorption channel and each desorption channel.
In some embodiments, the desorption passage comprises a heating passage and a cooling passage connected in parallel, and the heating passage and the cooling passage are both connected in series with a third valve.
In some embodiments, the adsorption unit further comprises a pressurization line, wherein an inlet of the pressurization line is communicated with an outlet of the adsorption channel, and an outlet of the pressurization line is communicated with the second inlet of the adsorption channel and/or the inlet of the cooling channel.
In some embodiments, a pressure relief valve is connected to the heating channel.
In some embodiments, a desulfurization unit is also included; the desulfurization unit comprises a spray absorption tower and a spray absorption liquid regeneration device, the spray absorption tower comprises a spray absorption liquid inlet, a methane inlet and a spray absorption liquid outlet, and the spray absorption liquid regeneration device comprises an absorption liquid inlet communicated with the spray absorption liquid outlet and an absorption liquid outlet communicated with the spray absorption liquid inlet; the biogas inlet is used for introducing biogas.
In another aspect, an embodiment of the present invention provides a method for preparing liquefied natural gas from biogas, including:
pretreating the biogas, wherein the pretreatment comprises adsorbing odor in the biogas by using an adsorbent in an adsorption unit; liquefying the pretreated methane to obtain liquefied natural gas and tail gas; and desorbing the odor adsorbed by the adsorbent by using tail gas generated in the liquefaction process.
In some embodiments, the pre-processing further comprises: decarbonization is handled, accomplishes the back at decarbonization, detects the foul smell content in the tail gas after the decarbonization handle the foul smell content in the tail gas after the decarbonization is handled is greater than under the condition of predetermineeing the threshold value, right tail gas after the decarbonization is handled carries out the deodorization the foul smell content in the tail gas after the decarbonization is handled is less than or equal to and predetermines under the condition of threshold value, directly discharges tail gas after the decarbonization is handled.
In some embodiments, the adsorption unit comprises a first adsorption unit and a second adsorption unit; the method for adsorbing odor in the biogas by using the adsorbent in the adsorption unit comprises the following steps: adsorbing odor in the biogas by using the adsorbent in the first adsorption unit, and desorbing odor in the adsorbent in the second adsorption unit by using tail gas generated in the liquefaction process; and after the preset time lasts, adsorbing odor in the biogas by using the adsorbents in the second adsorption units, and desorbing the odor in the adsorbents in the first adsorption unit by using tail gas generated in the liquefaction process.
In some embodiments, the adsorption unit further comprises a third adsorption unit; the method for adsorbing odor in the biogas by using the adsorbent in the adsorption unit comprises the following steps: adsorbing odor in the biogas by using the adsorbent in the first adsorption unit, desorbing odor in the adsorbent in the third adsorption unit by using the heated tail gas, and desorbing odor in the adsorbent in the second adsorption unit by using the unheated tail gas; after the first preset time lasts, adsorbing odor in the biogas by using the adsorbent in the second adsorption unit, desorbing odor in the adsorbent in the first adsorption unit by using heated tail gas, and desorbing odor in the adsorbent in the third adsorption unit by using unheated tail gas; after the second preset time lasts, adsorbing odor in the biogas by using an adsorbent in a third adsorption unit, desorbing odor in the adsorbent in the second adsorption unit by using heated tail gas, and desorbing odor in the adsorbent in the first adsorption unit by using unheated tail gas;
in some embodiments, the preparation method further comprises, while adsorbing odor from biogas with the adsorbent in the first adsorption unit, desorbing odor from the adsorbent in the third adsorption unit with heated tail gas, and desorbing odor from the adsorbent in the second adsorption unit with unheated tail gas: carrying out decompression treatment on the adsorption channel of the third adsorption unit;
performing pressure boosting treatment on the adsorption channel of the second adsorption unit; the preparation method comprises the following steps of adsorbing odor in the methane by using the adsorbent in the second adsorption unit, desorbing odor in the adsorbent in the first adsorption unit by using heated tail gas, and desorbing odor in the adsorbent in the third adsorption unit by using unheated tail gas, wherein the preparation method further comprises the following steps: carrying out decompression treatment on the adsorption channel of the first adsorption unit; performing pressure boosting treatment on the adsorption channel of the third adsorption unit;
the preparation method comprises the following steps of adsorbing odor in the biogas by using an adsorbent in a third adsorption unit, desorbing odor in the adsorbent in the second adsorption unit by using heated tail gas, and desorbing odor in the adsorbent in the first adsorption unit by using unheated tail gas, wherein the preparation method further comprises the following steps: carrying out decompression treatment on the adsorption channel of the second adsorption unit; and performing pressure boosting treatment on the adsorption channel of the first adsorption unit.
In some embodiments, before desorbing odor adsorbed by the adsorbent by using tail gas generated in the liquefaction process, the method further comprises:
and heating the tail gas in the liquefaction process by using the refrigerant subjected to heat exchange in the liquefaction process so as to increase the temperature of the tail gas.
The embodiment of the invention provides a system and a method for preparing liquefied natural gas from biogas. In the process, the cyclic utilization of the tail gas generated in the liquefaction process can be realized, the problems that the tail gas exhaust combustion generated in the liquefaction process in the prior art is not beneficial to the full utilization of the heat value in the methane and the environmental pollution caused by the tail gas exhaust combustion are solved, in addition, when the odor adsorbed by the adsorbent is desorbed, the adsorbent can be regenerated without additionally arranging a regenerated gas supply device, and the resource can be saved.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings needed to be used in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings based on these drawings without creative efforts.
Fig. 1 is a schematic structural diagram of a system for producing liquefied natural gas from biogas according to an embodiment of the present invention;
fig. 2 is a schematic structural diagram of another system for producing liquefied natural gas from biogas according to an embodiment of the present invention;
fig. 3 is a schematic structural diagram of another system for producing liquefied natural gas from biogas according to an embodiment of the present invention;
fig. 4 is a schematic structural diagram of another system for producing liquefied natural gas from biogas according to an embodiment of the present invention;
FIG. 5 is a schematic structural diagram of a liquefaction device according to an embodiment of the present invention;
FIG. 6 is a schematic structural diagram of another system for producing liquefied natural gas from biogas according to an embodiment of the present invention;
fig. 7 is a schematic structural diagram of another system for producing liquefied natural gas from biogas according to an embodiment of the present invention;
fig. 8 is a schematic structural diagram of another system for producing liquefied natural gas from biogas according to an embodiment of the present invention;
fig. 9 is a schematic structural diagram of another system for producing liquefied natural gas from biogas according to an embodiment of the present invention;
fig. 10 is a schematic flow chart of a method for producing liquefied natural gas from biogas according to an embodiment of the present invention;
fig. 11 is a schematic structural diagram of another system for preparing liquefied natural gas from biogas according to an embodiment of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it is to be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and thus, are not to be construed as limiting the present invention. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
Some embodiments of the present invention provide a system for preparing liquefied natural gas from biogas, as shown in fig. 1, including: a pretreatment apparatus 1 and a liquefaction apparatus 2. The pretreatment device 1 comprises an adsorption unit 11, wherein the adsorption unit 11 comprises an adsorption channel 111 and a desorption channel 112, an inlet 112a of the desorption channel 112 is communicated with a first inlet 111a of the adsorption channel 111, and an adsorbent is arranged in the adsorption channel 111 and is used for adsorbing odor in biogas. The liquefying device 2 is used for liquefying the biogas treated by the pretreatment device 1 to obtain liquefied natural gas and tail gas, the liquefying device 2 comprises a tail gas outlet 21, and the tail gas outlet 21 is communicated with an inlet 112a of the desorption passage 112.
In order to adsorb odor in the biogas, the adsorption channel 111 may include a biogas inlet 111b and a biogas outlet 111c, when the odor in the biogas is adsorbed by the adsorbent, the biogas enters the adsorption channel 111 through the biogas inlet and contacts the adsorbent in the adsorption channel 111, the odor in the biogas is adsorbed by the adsorbent, and the adsorbed biogas is discharged through the biogas outlet 111c, so as to complete adsorption of the odor in the biogas.
The desorption passage 112 and the adsorption passage 111 may be the same passage, the adsorption passage 111 is provided with a first inlet 111a, the first inlet 111a is an inlet different from the biogas inlet 111b, the inlet 112a of the desorption passage 112 is communicated with the first inlet 111a, when the odor adsorbed by the adsorbent is desorbed, the regeneration gas is introduced into the adsorption passage 111 through the inlet 112a of the desorption passage 112, the regeneration gas is brought into contact with the adsorbent adsorbed with the odor in the adsorption passage 111, and the adsorbent adsorbed with the odor is purged by using the regeneration gas, so that the odor adsorbed by the adsorbent can be desorbed, and the regeneration of the adsorbent is realized.
In the system for preparing liquefied natural gas from biogas according to the embodiment of the present invention, since the tail gas outlet 21 of the liquefaction device 2 is communicated with the inlet 112a of the desorption passage 112, the tail gas generated during liquefaction can be directly used to desorb the odor adsorbed by the adsorbent, thereby realizing regeneration of the adsorbent. In the process, the cyclic utilization of the tail gas generated in the liquefaction process can be realized, the problems that the tail gas exhaust combustion generated in the liquefaction process in the prior art is not beneficial to the full utilization of the heat value in the methane and the environmental pollution caused by the tail gas exhaust combustion are solved, in addition, when the odor adsorbed by the adsorbent is desorbed, the adsorbent can be regenerated without additionally arranging a regenerated gas supply device, and the resource can be saved.
In some embodiments, as shown in fig. 2, the system further comprises a power generation device 3, the power generation device 3 comprising a fuel inlet 31, the outlet 112b of the desorption passage 112 communicating with the fuel inlet 31.
In the embodiments, by providing the power generation device 3 and communicating the fuel inlet of the power generation device 3 with the outlet 112b of the desorption passage 112, after the odor adsorbed by the adsorbent is desorbed by the tail gas generated in the liquefaction process, the tail gas carrying odor can be used as fuel gas for power generation, thereby realizing self-generated power generation, which can be used for solving the power consumption requirement of the electrical equipment in the system, and meanwhile, in the desorption process, the tail gas generated in the liquefaction process can be used for diluting the odor, and the combustion heat of the odor is used for power generation, thereby solving the problems that in the prior art, the odor is treated by a combustion mode, the combustion heat in the odor cannot be utilized, and the economic benefit is not improved.
The structure of the pretreatment device 1 is not particularly limited.
In some embodiments, as shown in fig. 3, the pretreatment device 1 may further include, in addition to the above adsorption unit 11: a desulfurization unit 12. The desulfurization unit 12 includes a spray absorption tower 121 and a spray absorption liquid regeneration device 122, and the spray absorption tower 121 includes a spray absorption liquid inlet 121a, a biogas inlet 121b, and a spray absorption liquid outlet 121 c. The spray absorbent regeneration device 122 includes an absorbent inlet 122a communicating with the spray absorbent outlet 121c, and an absorbent outlet 122b communicating with the spray absorbent inlet 121 a. The biogas inlet 121b is used for introducing biogas.
In these examples, the spray absorption tower 121 and the spray absorption liquid regeneration device 122 are provided, so that the spray absorption liquid and the biogas are brought into contact with each other in a counter-current manner, and the hydrogen sulfide in the biogas can be absorbed by the spray absorption liquid. On the other hand, the recycle of the spray absorption liquid can be realized by regenerating the spray absorption liquid absorbed with hydrogen sulfide.
The structure of the spray absorption tower 121 is not particularly limited, and the spray absorption liquid may be contacted with the biogas in a counter-current manner.
In some embodiments, the spray absorption tower 121 may have a multi-stage spray structure, such as a four-stage spray structure, which may implement a large-scale desulfurization process.
After the countercurrent contact, the desulfurized biogas contains water and elemental sulfur.
Based on this, in some embodiments, as shown in fig. 3, a baffle plate 123 is further disposed at the top of the spray absorption tower 121, and by disposing the baffle plate 123, water and elemental sulfur in the valence band in the biogas can be removed, so that the content of water and elemental sulfur in the biogas after desulfurization treatment is reduced, and the desulfurization effect is improved.
Here, taking the spraying absorption liquid as a ferric ion solution as an example, after the ferric ion solution contacts with the biogas in a countercurrent manner, hydrogen sulfide in the biogas is firstly dissolved in the spraying absorption liquid and reacts with the spraying absorption liquid to generate elemental sulfur and a ferrous ion solution, so that the hydrogen sulfide in the biogas can be removed.
The structure of the spray absorbent regeneration device 122 is not particularly limited, and the spray absorbent can be regenerated.
In some embodiments, as shown in fig. 3, the spray absorption liquid regeneration device 122 includes a settling tower 122A and a solid-liquid separation device 122B. The absorbent inlet 122A is provided in the settling tower 122A, and the settling tower 122A is further provided with an oxidant inlet 122c and a solid-liquid discharge port 122 d. The solid-liquid separator 122B includes a solid-liquid inlet 122e and a liquid outlet 122f, and the liquid outlet 122f is in communication with the sprayed absorbent inlet 121a as an absorbent outlet 122B.
In these embodiments, when the spray absorption liquid absorbing hydrogen sulfide needs to be regenerated, the spray absorption liquid absorbing hydrogen sulfide may be discharged into the settling tower 122A through the spray absorption liquid outlet 121a, elemental sulfur settles to the bottom of the settling tower 122, the upper layer is a divalent iron ion solution, and an oxidizing agent is added into the settling tower 122A through the oxidizing agent inlet 122c, so that the regeneration of the spray absorption liquid can be realized. The lower-layer elemental sulfur is discharged into the solid-liquid separation device 122B through the solid-liquid discharge port, so that solid-liquid separation can be realized, and the cyclic utilization of the spray absorption liquid can be realized. In this process, by providing the settling tower 122A and the solid-liquid separation device 122B, large-scale treatment can be realized.
Wherein, the bottom of the settling tower 122A may be an inverted cone structure. In order to avoid sulphur sticking to the cone bottom, the cone bottom may be provided with a purge gas nozzle.
The structure of the solid-liquid separator 122B is not particularly limited.
In some embodiments, the solid-liquid separation device 122B is a pressure filtration device. The elemental sulfur can be filter-pressed into a filter cake by a filter pressing device.
Wherein, the biogas outlet of the desulfurization unit 12 may be communicated with the biogas inlet 111b of the adsorption channel 111. Namely, after a large amount of hydrogen sulfide in the biogas is removed, other sulfur-containing substances in the biogas are removed.
In some embodiments, as shown in fig. 4, the pretreatment device 1 further includes a decarbonization unit 13 connected in series between the adsorption unit 11 and the liquefaction device 2, the decarbonization unit 13 includes a carbon dioxide exhaust port 131, the carbon dioxide exhaust port 131 is connected with a deodorization tank 132, and a bypass pipe 133 connected in parallel with the deodorization tank 132, and a first valve a is disposed on the bypass pipe 133.
In these embodiments, the carbon dioxide exhaust port 131 of the decarbonizing unit 13 is connected to the deodorizing tank 132, so that the exhaust gas from the decarbonizing unit 13 can be further deodorized to prevent environmental pollution. On the other hand, by providing the bypass duct 133 connected in parallel with the deodorization tank 132, and providing the first valve a on the bypass duct 133, the odor content in the exhaust gas discharged from the decarburization unit 13 can be detected before the exhaust gas discharged from the decarburization unit 13 is discharged, and if the odor content in the exhaust gas discharged from the decarburization unit 13 is greater than or equal to the preset threshold, the first valve a is controlled to be closed, the exhaust gas discharged from the decarburization unit 13 is deodorized and then discharged, and if the odor content in the exhaust gas discharged from the decarburization unit 13 is less than the preset threshold, the first valve a is controlled to be opened, so that the exhaust gas discharged from the decarburization unit 13 can be directly released.
The decarbonizing unit 13 can include a decarbonizing adsorption tower 132, a carbon dioxide adsorbent is disposed in the decarbonizing adsorption tower 132, a carbon dioxide exhaust port 131 is disposed on the decarbonizing adsorption tower, and a pressure reducing valve 132a is disposed on the decarbonizing adsorption tower 132.
The carbon dioxide in the biogas is adsorbed by the carbon dioxide adsorbent to realize decarburization, and after decarburization is completed, the decarburization adsorption tower 132 can be vacuumized by controlling the reducing valve 132a to realize desorption of the carbon dioxide from the carbon dioxide adsorbent, so that exhaust of the tail gas is realized.
In some embodiments, as shown in FIG. 5, the liquefaction plant 2 includes a multi-stage condensing unit 22, and a liquid storage tank 23 in communication with the liquid outlet of each stage of condensing unit 22 in the multi-stage condensing unit 22. The multistage condensing device 22 further comprises a heat exchange channel 221, the gas outlet 23a of the last stage liquid storage tank 23 is communicated with the inlet 221a of the heat exchange channel 221, and the outlet 221b of the heat exchange channel 221 is used as the tail gas outlet 21.
In the embodiments, the heat exchange channel 221 is arranged in the multistage condensing device 22, the gas outlet 23a of the last stage liquid storage tank 23 is communicated with the inlet 221a of the heat exchange channel 221, and the outlet 221b of the heat exchange channel 221 is used as the tail gas outlet 21, so that on one hand, nitrogen in the liquefaction process can be used as tail gas for circulation, and on the other hand, before tail gas generated in the liquefaction process is used for desorbing odor adsorbed by an adsorbent, heat exchange can be performed between the tail gas generated in the liquefaction process and refrigerant in the multistage condensing device 22, the temperature of the tail gas generated in the liquefaction process is increased, energy can be fully utilized, and energy consumption is saved.
Wherein, the multi-stage condensing device 22 can be a two-stage condensing device 22, and correspondingly, the liquid storage tank 23 is also provided with two stages. The first-stage condensing device 22 condenses heavy hydrocarbon in the methane and stores the heavy hydrocarbon in the first-stage liquid storage tank 23A, the second-stage condensing device 22 condenses methane in the methane and stores the methane in the second-stage liquid storage tank 23B, and nitrogen in the methane is discharged through the gas outlet 23A of the second-stage liquid storage tank 23B.
In order to overflow nitrogen dissolved in methane, the second-stage liquid storage tank 23B may be a rectification tank, and a heat transfer medium channel 24 may be disposed in the second-stage liquid storage tank 23B, so that liquid in the second-stage liquid storage tank 23B is heated by a heat transfer medium, so as to overflow nitrogen dissolved in the liquid.
In some embodiments, the liquefaction apparatus 2 further comprises a filling channel 25, the filling channel 25 having a filling volatile gas outlet 25a, the filling volatile gas outlet 25a being in communication with the inlet 221a of the heat exchange channel 221.
In this embodiment, through making filling volatile gas export 25a and heat transfer channel 221's entry 221a intercommunication, can make filling volatile gas also carry out desorption to the adsorbed foul smell of adsorbent as the tail gas that the liquefaction in-process produced, avoid the exhaust combustion processing, cause the problem of wasting of resources.
Wherein, the above filling channel 25 further comprises an liquefied natural gas inlet 25b, and the liquefied natural gas inlet 25b can be communicated with the liquid outlet 23b of the last stage storage tank 23.
As in the case where the above liquefaction apparatus 2 includes the two-stage tank 23, the liquefied natural gas inlet 25B communicates with the liquid outlet 23B of the second-stage tank 23B.
In order to avoid too rapid volatilization of the liquefied natural gas during the filling process, optionally, the multistage condensation device 22 may further include an liquefied natural gas condensation passage 222, an inlet 222a of the liquefied natural gas condensation passage 222 is communicated with the liquid outlet 23b of the last stage storage tank 23, and an outlet 222b of the liquefied natural gas condensation passage 222 is communicated with the liquefied natural gas inlet 25 b. That is, before filling liquefied natural gas, the liquefied natural gas is condensed again to prevent volatilization.
The number of the adsorption units 11 is not particularly limited, and one or more adsorption units 11 may be provided.
In some embodiments, as shown in fig. 6, the adsorption unit 11 is multiple, the adsorption channels 111 of the multiple adsorption units 11 are connected in parallel, the desorption channels 112 of the multiple adsorption units 11 are connected in parallel, and the second valve b is connected in series to each adsorption channel 111 and each desorption channel 112.
"plurality" herein means greater than or equal to two.
In these embodiments, by providing a plurality of adsorption units 11, connecting the adsorption channels 111 of the adsorption units 11 in parallel, connecting the desorption channels 112 of the adsorption units 11 in parallel, and connecting the second valve b in series on each adsorption channel 111 and each desorption channel 112, the odor in the biogas can be adsorbed by using part of the adsorbents in the adsorption units 11 by controlling the opening and closing of the second valve b, and meanwhile, the odor adsorbed by the adsorbents in the remaining adsorption units 11 is desorbed by using the tail gas generated in the liquefaction process, so that the cyclic adsorption of the adsorbents in the adsorption units 11 can be realized, and the occurrence of stoppage can be avoided.
Illustratively, taking two adsorption units 11 including a first adsorption unit 11A and a second adsorption unit 11B as an example, during driving, odor in biogas can be adsorbed by the adsorbent in the first adsorption unit 11A by opening the second valve B on the adsorption passage 111 of the first adsorption unit 11A, after a first preset time, closing the second valve B on the adsorption passage 111 of the first adsorption unit 11A, opening the second valve B on the adsorption passage 111 of the second adsorption unit 11B, adsorbing odor in biogas by the adsorbent in the second adsorption unit 11B, and simultaneously, opening the second valve B on the desorption passage 112 of the first adsorption unit 11A, desorbing odor adsorbed by the adsorbent in the first adsorption unit 11A by using tail gas generated during liquefaction. After the second preset time, closing the second valve B on the adsorption channel 111 of the second adsorption unit 11B, opening the second valve B on the desorption channel 112 of the second adsorption unit 11B, desorbing the odor adsorbed by the adsorbent in the second adsorption unit 11B by using the tail gas generated in the liquefaction process, simultaneously opening the second valve B on the adsorption channel 111 of the first adsorption unit 11A, adsorbing the odor in the biogas by using the adsorbent in the first adsorption unit 11A, and repeating the cycle, so that the odor in the biogas can be adsorbed continuously in the whole process.
In some embodiments, as shown in fig. 6, desorption passage 112 includes heating passage 112A and cooling passage 112B in parallel, with third valve c connected in series to both heating passage 112A and cooling passage 112B.
In these embodiments, by providing the heating channel 112A and the cooling channel 112B, the tail gas generated in the liquefaction process can be heated and cooled, and the odor adsorbed by the adsorbent in the adsorption unit 11 can be desorbed by using the heated tail gas and the cooled tail gas, respectively, so that heating desorption can be realized, the desorption effect can be improved, and after heating desorption, the temperature of the adsorption channel 111 can be reduced to the temperature required for adsorption by the cooled tail gas, and the adsorption effect can be improved.
Wherein the heating channel 112A may be obtained by providing a heating device 20 on the desorption channel 112.
In some embodiments, as shown in fig. 6, the system further comprises a pressurization line 14, an inlet 14a of the pressurization line 14 is communicated with the biogas outlet 111c and/or the off-gas outlet 21 of the adsorption channel 111, and an outlet 14B of the pressurization line 14 is communicated with the second inlet 111d of the adsorption channel 111 and/or the inlet of the cooling channel 112B.
In these embodiments, by providing the pressurization pipeline 14, and communicating the inlet 14a of the pressurization pipeline 14 with the biogas outlet 111c of the adsorption channel 111, and communicating the outlet 14B of the pressurization pipeline 14 with the second inlet 111d of the adsorption channel 111 and/or the inlet of the cooling channel 112B, the adsorption channel 111 and/or the cooling channel 112B can be pressurized by the deodorized biogas, thereby realizing pressure-increasing adsorption and facilitating adsorption of odor in the biogas.
The second inlet 111d may be a biogas inlet 111b, or may be the first inlet 111 a. And is not particularly limited herein.
In some embodiments, as shown in FIG. 6, a pressure relief valve d is connected to the heating channel 112A. By connecting the pressure reducing valve d to the heating passage 112A, it is also possible to perform pressure-reduced desorption, which facilitates desorption of the odor from the adsorbent.
In some embodiments, as shown in fig. 7, the pretreatment device 1 may further include a deoxidation unit 15, and the deoxidation unit 15 is used for removing oxygen from the biogas.
In some embodiments, the deoxygenation unit 15 may be connected in series between the decarbonization unit 13 and the liquefaction plant 2, with a catalyst disposed in the deoxygenation unit 15.
In these embodiments, carbon dioxide and water can be generated by using methane and oxygen under the catalytic action of the catalyst, and the deoxygenation can be realized by arranging the catalyst in the deoxygenation unit 15.
It should be noted that, after the desulfurization treatment of the biogas, hydrogen sulfide in the biogas cannot be removed, but remains at about 10ppm, and the presence of the hydrogen sulfide causes catalyst poisoning.
Based on this, in some embodiments, as shown in fig. 7, the system further includes a fine desulfurization unit 16 connected in series between the decarbonization unit 13 and the deoxidation unit 15, where the fine desulfurization unit 16 is configured to remove hydrogen sulfide in the biogas again so that the content of hydrogen sulfide in the biogas is less than a first preset threshold, and in case that the content of hydrogen sulfide in the biogas is less than the first preset threshold, the catalyst is not poisoned.
Wherein the first preset threshold may be 0.1 ppm.
In some embodiments, fine desulfurization unit 16 may include multiple zinc oxide absorption tanks in series or parallel.
In some embodiments, as shown in fig. 8, the system may further include a fine decarbonization unit 17 and a dehydration unit 18 connected in series between the deoxygenation unit 15 and the liquefaction plant 2.
In the embodiments, by providing the fine decarbonization unit 17, carbon dioxide in the biogas can be further removed, so that the heat value of the natural gas is prevented from being reduced due to the high content of carbon dioxide, and the pipeline can be prevented from being blocked due to the carbon dioxide being condensed into solid at low temperature. By providing the dehydration unit 18, it is possible to prevent the calorific value of the natural gas from being affected by an excessively high water content.
In some embodiments, the fine decarbonization unit 17 may include an alkaline absorption liquid storage tank 171 and an alkaline absorption liquid regeneration device 172. The alkaline absorption liquid is used for absorbing carbon dioxide, a small amount of residual hydrogen sulfide in the fine desulfurization process can be absorbed, and the problems that acid gas exists in natural gas, metal is corroded, and environment pollution is caused are solved.
In still other embodiments, as shown in fig. 9, the system may further include a demercuration unit 19 connected in series between the dehydration unit 18 and the liquefaction plant 2, wherein the demercuration unit 19 is used for removing mercury in the biogas. It is also possible to avoid that the mercury becomes solid during condensation and blocks the pipes.
In practical applications, the mercury content in the biogas can be detected after dehydration to determine whether mercury removal is required.
In some embodiments, as shown in fig. 9, the system may further include a dust removal unit 10, the dust removal unit 10 includes a biogas inlet 10a and a biogas outlet 10b, the biogas inlet 10a is used for introducing biogas, and the biogas outlet 10b may be communicated with the biogas inlet 12a of the desulfurization unit 12.
That is, mechanical impurities such as dust in the biogas are removed before the desulfurization treatment.
In some embodiments, the dust removal unit 10 may include a water washing device, and the biogas is dedusted by the water washing device, and part of the acid gas such as carbon dioxide, hydrogen sulfide, etc. in the biogas may be removed.
Some embodiments of the present invention provide a method for producing liquefied natural gas from biogas, referring to fig. 10, including:
step 1) pretreating the biogas, wherein the pretreatment comprises adsorbing odor in the biogas by using an adsorbent in an adsorption unit.
And 2) liquefying the pretreated methane to obtain liquefied natural gas and tail gas.
And 3) desorbing the odor adsorbed by the adsorbent by using the tail gas generated in the liquefaction process.
It can be known that, as biogas is a combustible gas with odor, odor in biogas needs to be removed before the biogas is liquefied.
The type of the adsorbent is not particularly limited, and the adsorbent can be any adsorbent which can adsorb odor in the biogas and can desorb the adsorbed odor by purging the regeneration gas. For example, the adsorbent may be activated carbon.
The regeneration gas may be an inert gas or the like in desorbing the odor absorbed by the adsorbent, and is not particularly limited.
According to the principle that the main components of the biogas include methane, nitrogen, carbon dioxide, oxygen, hydrogen sulfide and other gases, before liquefaction is needed, the carbon dioxide, hydrogen sulfide, oxygen and other gases in the biogas need to be removed so as to reach the pipe conveying standard, and it can be known that the biogas only contains methane, nitrogen, a small amount of carbon dioxide, hydrogen sulfide and other gases in the liquefaction process.
And according to the mode of adopting condensation step by step in the liquefaction process, can learn, the tail gas that produces in the liquefaction process includes nitrogen gas, so, desorbs the foul smell that the adsorbent adsorbs through regard to nitrogen gas as regeneration gas, can realize the regeneration of adsorbent. In the process, the additional arrangement of a regeneration gas supply device can be avoided, and the recycling of tail gas generated in the liquefaction process can be realized. Solves the problem of environmental pollution caused by the exhaust combustion of tail gas generated in the liquefaction process in the prior art, and can improve economic benefit.
In some embodiments, the pre-processing further comprises: and (3) decarbonizing, namely detecting the odor content in the tail gas subjected to decarbonizing after the decarbonizing is finished, deodorizing the tail gas subjected to decarbonizing under the condition that the odor content in the tail gas subjected to decarbonizing is greater than a preset threshold value, and directly discharging the tail gas subjected to decarbonizing under the condition that the odor content in the tail gas subjected to decarbonizing is less than or equal to the preset threshold value.
In these embodiments, the tail gas after the decarburization treatment may be deodorized and then discharged or directly discharged according to the odor content in the tail gas after the decarburization treatment, so that the tail gas after the decarburization treatment can be prevented from polluting the environment.
In some embodiments, as shown in fig. 9, the adsorption unit 11 includes a first adsorption unit 11A and a second adsorption unit 11B. The method for adsorbing the odor in the biogas by using the adsorbent in the adsorption unit comprises the following steps:
the odor in the biogas is adsorbed by the adsorbent in the first adsorption unit 11A, and the odor in the adsorbent in the second adsorption unit 11B is desorbed by the tail gas generated in the liquefaction process.
After the preset time is continued, adsorbing odor in the biogas by using the adsorbent in the second adsorption unit 11B, and desorbing odor in the adsorbent in the first adsorption unit 11A by using tail gas generated in the liquefaction process.
In these embodiments, by alternately adsorbing odor in the biogas by the adsorbent in the first adsorption unit 11A and the adsorbent in the second adsorption unit 11B, and desorbing odor in the adsorbent in one of the adsorption units by using tail gas generated during liquefaction while adsorbing odor in the biogas, the adsorbents in the first adsorption unit 11A and the second adsorption unit 11B can be recycled to avoid a stop.
In some embodiments, as shown in fig. 11, the adsorption unit 11 further includes a third adsorption unit 11C; the method for adsorbing odor in biogas by using the adsorbent in the adsorption unit 11 comprises the following steps:
the odor in the biogas is adsorbed by the adsorbent in the first adsorption unit 11A, the odor in the adsorbent in the third adsorption unit 11C is desorbed by the heated tail gas, and the odor in the adsorbent in the second adsorption unit 11B is desorbed by the unheated tail gas.
After the first preset time, the odor in the biogas is adsorbed by the adsorbent in the second adsorption unit 11B, the odor in the adsorbent in the first adsorption unit 11A is desorbed by the heated tail gas, and the odor in the adsorbent in the third adsorption unit 11C is desorbed by the unheated tail gas.
After the second preset time, the odor in the biogas is adsorbed by the adsorbent in the third adsorption unit 11C, the odor in the adsorbent in the second adsorption unit 11B is desorbed by the heated tail gas, and the odor in the adsorbent in the first adsorption unit 11A is desorbed by the unheated tail gas.
In these embodiments, by using the adsorbents in at least three adsorption units 11 to adsorb the odor in the biogas, the odor in the biogas can be adsorbed by using the adsorbent in one adsorption unit 11, the odor in the adsorbent in one adsorption unit 11 can be desorbed by using the heated tail gas, and the odor in the adsorbent in one adsorption unit 11 can be desorbed by using the unheated tail gas, so that the efficiency of adsorption, heating and cold blowing can be improved, the adsorption effect can be improved by adsorption under the cooling condition, the desorption effect can be improved by desorption under the heating condition, and the regeneration gas consumption of the adsorbent can be reduced.
In some embodiments, while adsorbing odor from biogas with the adsorbent in the first adsorption unit 11A, desorbing odor from the adsorbent in the third adsorption unit 11C with heated tail gas, and desorbing odor from the adsorbent in the second adsorption unit 11B with unheated tail gas, the preparation method further comprises: depressurizing the desorption passage 112 of the third adsorption unit 11C; the pressure-raising process is performed on the adsorption passage 111 of the second adsorption unit 11B.
The preparation method comprises the following steps of adsorbing odor in the methane by using the adsorbent in the second adsorption unit 11B, desorbing odor in the adsorbent in the first adsorption unit 11A by using the heated tail gas, and desorbing odor in the adsorbent in the third adsorption unit 11C by using the unheated tail gas, wherein the preparation method comprises the following steps: depressurizing the desorption passage 112 of the first adsorption unit 11A; the pressure-raising process is performed on the adsorption passage 111 of the third adsorption unit 11C.
The preparation method comprises the following steps of adsorbing odor in the biogas by using the adsorbent in the third adsorption unit 11C, simultaneously desorbing odor in the adsorbent in the second adsorption unit 11B by using the heated tail gas, and desorbing odor in the adsorbent in the first adsorption unit 11A by using the unheated tail gas, wherein the preparation method comprises the following steps: depressurizing the desorption passage 112 of the second adsorption unit 11B; the adsorption passage 111 of the first adsorption unit 11A is subjected to pressure-raising processing.
In these examples, the desorption effect can be further improved by the pressure-reducing treatment at the time of heating desorption, and the pressure-increasing treatment at the time of desorption by cooling can prepare for the next adsorption to improve the adsorption effect.
In some embodiments, before desorbing odor adsorbed by the adsorbent by using tail gas generated in the liquefaction process, the method further comprises: and heating the tail gas generated in the liquefaction process by using the refrigerant subjected to heat exchange in the liquefaction process so as to increase the temperature of the tail gas.
In the embodiments, the tail gas generated in the liquefaction process is heated, so that the tail gas is convenient to use, and the problem that the odor in the adsorbent in the adsorption unit is desorbed by the heated tail gas in the follow-up process, and more heat sources are needed, so that the energy is not beneficial to effective utilization is solved.
The scope of the present invention is not limited thereto, and any person skilled in the art can easily conceive of changes or substitutions within the technical scope of the present invention, and the present invention is intended to be covered thereby. Therefore, the protection scope of the present invention shall be subject to the protection scope of the appended claims.
Claims (16)
1. A system for preparing liquefied natural gas from biogas is characterized by comprising:
the pretreatment device comprises an adsorption unit, the adsorption unit comprises an adsorption channel and a desorption channel, wherein the inlet of the desorption channel is communicated with the first inlet of the adsorption channel, an adsorbent is arranged in the adsorption channel, and the adsorbent is used for adsorbing odor in the biogas;
the liquefying device is used for liquefying the methane treated by the pretreatment device to obtain liquefied natural gas and tail gas, and comprises a tail gas outlet which is communicated with the inlet of the desorption channel.
2. The system for producing liquefied natural gas from biogas according to claim 1, further comprising: a power generation device comprising a fuel inlet;
the outlet of the desorption passage communicates with the fuel inlet.
3. The system for preparing liquefied natural gas from biogas according to claim 1 or 2, wherein the pretreatment device further comprises a decarbonization unit connected in series with an outlet of the adsorption channel of the adsorption unit, the decarbonization unit comprises a carbon dioxide exhaust port connected with a deodorization tank, and a bypass pipeline connected in parallel with the deodorization tank, and a first valve is arranged on the bypass pipeline.
4. The system for producing liquefied natural gas from biogas according to claim 1 or 2, wherein the liquefaction apparatus comprises a multi-stage condensation apparatus and a liquid storage tank in communication with a liquid outlet of each stage of the multi-stage condensation apparatus;
the multistage condensing device further comprises a heat exchange channel, a gas outlet of the last stage of liquid storage tank is communicated with an inlet of the heat exchange channel, and an outlet of the heat exchange channel is used as the tail gas outlet.
5. The system for producing liquefied natural gas using biogas according to claim 4,
the liquefaction device still includes the filling passageway, the filling passageway has the export of filling volatile gas, filling volatile gas export with the entry intercommunication of heat transfer passageway.
6. The system for preparing liquefied natural gas from biogas according to claim 1 or 2, wherein the adsorption unit is provided in plurality, the adsorption channels of the adsorption units are connected in parallel, the desorption channels of the adsorption units are connected in parallel, and a second valve is connected in series to each adsorption channel and each desorption channel.
7. The system for preparing liquefied natural gas from biogas according to claim 1 or 2, wherein the desorption passage comprises a heating passage and a cooling passage connected in parallel, and the heating passage and the cooling passage are both connected in series with a third valve.
8. The system for producing liquefied natural gas from biogas according to claim 7, further comprising a pressurizing pipeline, wherein an inlet of the pressurizing pipeline is communicated with an outlet of the adsorption channel and/or the tail gas outlet, and an outlet of the pressurizing pipeline is communicated with a second inlet of the adsorption channel and/or an inlet of the cooling channel.
9. The system for preparing liquefied natural gas from biogas according to claim 7, wherein the heating channel is connected with a pressure reducing valve.
10. The system for producing liquefied natural gas from biogas according to claim 1 or 2, further comprising a desulfurization unit;
the desulfurization unit comprises a spray absorption tower and a spray absorption liquid regeneration device, the spray absorption tower comprises a spray absorption liquid inlet, a methane inlet and a spray absorption liquid outlet, and the spray absorption liquid regeneration device comprises an absorption liquid inlet communicated with the spray absorption liquid outlet and an absorption liquid outlet communicated with the spray absorption liquid inlet; the biogas inlet is used for introducing biogas.
11. A method for preparing liquefied natural gas from biogas is characterized by comprising the following steps:
pretreating the biogas, wherein the pretreatment comprises adsorbing odor in the biogas by using an adsorbent in an adsorption unit;
liquefying the pretreated methane to obtain liquefied natural gas and tail gas;
and desorbing the odor adsorbed by the adsorbent by using tail gas generated in the liquefaction process.
12. The method for producing liquefied natural gas using biogas according to claim 11,
the pre-processing further comprises: decarbonization is handled, accomplishes the back at decarbonization, detects the foul smell content in the tail gas after the decarbonization handle the foul smell content in the tail gas after the decarbonization is handled is greater than under the condition of predetermineeing the threshold value, right tail gas after the decarbonization is handled carries out the deodorization the foul smell content in the tail gas after the decarbonization is handled is less than or equal to and predetermines under the condition of threshold value, directly discharges tail gas after the decarbonization is handled.
13. The method for producing liquefied natural gas using biogas according to claim 11,
the adsorption unit comprises a first adsorption unit and a second adsorption unit;
the method for adsorbing odor in the biogas by using the adsorbent in the adsorption unit comprises the following steps:
adsorbing odor in the biogas by using the adsorbent in the first adsorption unit, and desorbing odor in the adsorbent in the second adsorption unit by using tail gas generated in the liquefaction process;
and after the preset time lasts, adsorbing odor in the biogas by using the adsorbents in the second adsorption units, and desorbing the odor in the adsorbents in the first adsorption unit by using tail gas generated in the liquefaction process.
14. The method for producing liquefied natural gas using biogas according to claim 13,
the adsorption unit further comprises a third adsorption unit;
the method for adsorbing odor in the biogas by using the adsorbent in the adsorption unit comprises the following steps:
adsorbing odor in the biogas by using the adsorbent in the first adsorption unit, desorbing odor in the adsorbent in the third adsorption unit by using the heated tail gas, and desorbing odor in the adsorbent in the second adsorption unit by using the unheated tail gas;
after the first preset time lasts, adsorbing odor in the biogas by using the adsorbent in the second adsorption unit, desorbing odor in the adsorbent in the first adsorption unit by using heated tail gas, and desorbing odor in the adsorbent in the third adsorption unit by using unheated tail gas;
after lasting second preset time, utilize the adsorbent in the third adsorption unit to adsorb the foul smell in the marsh gas, adopt the tail gas after the heating simultaneously to be right the foul smell in the adsorbent in the second adsorption unit desorbs, adopts unheated tail gas to desorb the foul smell in the adsorbent in the first adsorption unit.
15. The method for preparing liquefied natural gas from biogas according to claim 14, wherein the odor in biogas is adsorbed by the adsorbent in the first adsorption unit, while the odor in adsorbent in the third adsorption unit is desorbed by the heated tail gas, and while the odor in adsorbent in the second adsorption unit is desorbed by the unheated tail gas, the method further comprises:
carrying out decompression treatment on the adsorption channel of the third adsorption unit;
performing pressure boosting treatment on the adsorption channel of the second adsorption unit;
the preparation method comprises the following steps of adsorbing odor in the methane by using the adsorbent in the second adsorption unit, desorbing odor in the adsorbent in the first adsorption unit by using heated tail gas, and desorbing odor in the adsorbent in the third adsorption unit by using unheated tail gas, wherein the preparation method further comprises the following steps:
carrying out decompression treatment on the adsorption channel of the first adsorption unit;
performing pressure boosting treatment on the adsorption channel of the third adsorption unit;
the preparation method comprises the following steps of adsorbing odor in the biogas by using an adsorbent in a third adsorption unit, desorbing odor in the adsorbent in the second adsorption unit by using heated tail gas, and desorbing odor in the adsorbent in the first adsorption unit by using unheated tail gas, wherein the preparation method further comprises the following steps:
carrying out decompression treatment on the adsorption channel of the second adsorption unit;
and performing pressure boosting treatment on the adsorption channel of the first adsorption unit.
16. The method for producing liquefied natural gas using biogas according to any one of claims 11 to 15, wherein the biogas is a liquefied natural gas,
before the tail gas generated in the liquefaction process is used for desorbing the odor adsorbed by the adsorbent, the method further comprises the following steps:
and heating the tail gas generated in the liquefaction process by using the refrigerant subjected to heat exchange in the liquefaction process so as to increase the temperature of the tail gas.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115854654A (en) * | 2022-12-26 | 2023-03-28 | 中国石油大学(华东) | CRS (Central Standard System) technology-based nitrogen expansion, liquefaction and decarburization system and method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115854654A (en) * | 2022-12-26 | 2023-03-28 | 中国石油大学(华东) | CRS (Central Standard System) technology-based nitrogen expansion, liquefaction and decarburization system and method |
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