CN117241874A - 用于再生预纯化容器的方法 - Google Patents
用于再生预纯化容器的方法 Download PDFInfo
- Publication number
- CN117241874A CN117241874A CN202180097229.XA CN202180097229A CN117241874A CN 117241874 A CN117241874 A CN 117241874A CN 202180097229 A CN202180097229 A CN 202180097229A CN 117241874 A CN117241874 A CN 117241874A
- Authority
- CN
- China
- Prior art keywords
- prepurification
- vessel
- purge gas
- oxygen
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 64
- 230000001172 regenerating effect Effects 0.000 title claims abstract description 13
- 239000007789 gas Substances 0.000 claims abstract description 111
- 238000010926 purge Methods 0.000 claims abstract description 86
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 73
- 239000001301 oxygen Substances 0.000 claims abstract description 73
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 73
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000000926 separation method Methods 0.000 claims abstract description 39
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 21
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 229910001868 water Inorganic materials 0.000 claims abstract description 14
- 239000012535 impurity Substances 0.000 claims abstract description 13
- 239000001257 hydrogen Substances 0.000 claims abstract description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 40
- 239000003054 catalyst Substances 0.000 claims description 38
- 230000008929 regeneration Effects 0.000 claims description 32
- 238000011069 regeneration method Methods 0.000 claims description 32
- 239000003463 adsorbent Substances 0.000 claims description 23
- 229910052757 nitrogen Inorganic materials 0.000 claims description 20
- 238000000746 purification Methods 0.000 claims description 19
- 239000000463 material Substances 0.000 claims description 14
- 238000004821 distillation Methods 0.000 claims description 11
- 229910021536 Zeolite Inorganic materials 0.000 claims description 9
- 239000000356 contaminant Substances 0.000 claims description 9
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 9
- 239000010457 zeolite Substances 0.000 claims description 9
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 239000002808 molecular sieve Substances 0.000 claims description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 6
- 238000011144 upstream manufacturing Methods 0.000 claims description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- 229910052786 argon Inorganic materials 0.000 claims description 4
- 229910000510 noble metal Inorganic materials 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- 239000000741 silica gel Substances 0.000 claims description 2
- 229910002027 silica gel Inorganic materials 0.000 claims description 2
- 238000003860 storage Methods 0.000 claims description 2
- 230000000717 retained effect Effects 0.000 claims 1
- 238000001179 sorption measurement Methods 0.000 description 17
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 8
- 238000002156 mixing Methods 0.000 description 7
- 229930195733 hydrocarbon Natural products 0.000 description 5
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 4
- 230000009977 dual effect Effects 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000001272 nitrous oxide Substances 0.000 description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 229910000792 Monel Inorganic materials 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 229910052763 palladium Inorganic materials 0.000 description 2
- 239000002594 sorbent Substances 0.000 description 2
- 238000011282 treatment Methods 0.000 description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- -1 carbon dioxide hydrocarbons Chemical class 0.000 description 1
- 238000010960 commercial process Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000010408 sweeping Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0295—Start-up or control of the process; Details of the apparatus used, e.g. sieve plates, packings
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/864—Removing carbon monoxide or hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8671—Removing components of defined structure not provided for in B01D53/8603 - B01D53/8668
- B01D53/8675—Ozone
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04181—Regenerating the adsorbents
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04775—Air purification and pre-cooling
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04854—Safety aspects of operation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/112—Metals or metal compounds not provided for in B01D2253/104 or B01D2253/106
- B01D2253/1124—Metal oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/10—Noble metals or compounds thereof
- B01D2255/102—Platinum group metals
- B01D2255/1023—Palladium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/207—Transition metals
- B01D2255/2073—Manganese
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/207—Transition metals
- B01D2255/20761—Copper
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/108—Hydrogen
-
- 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
- B01D2257/502—Carbon monoxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40086—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by using a purge gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/414—Further details for adsorption processes and devices using different types of adsorbents
- B01D2259/4141—Further details for adsorption processes and devices using different types of adsorbents within a single bed
- B01D2259/4145—Further details for adsorption processes and devices using different types of adsorbents within a single bed arranged in series
- B01D2259/4146—Contiguous multilayered adsorbents
-
- 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
-
- 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
- F25J2205/72—Pressurising or depressurising the adsorption vessel
-
- 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
- F25J2210/42—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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/80—Retrofitting, revamping or debottlenecking of existing plant
-
- 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
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
提供了一种再生预纯化容器的***和方法,其特别适用于对使用富氧吹扫气体流来再生预纯化装置的低温空气分离装置中的进料空气流进行预纯化。所公开的预纯化***和方法被构造成基本上去除进料空气流中的所有水、二氧化碳和其它杂质,任选地包括氢气和一氧化碳杂质。再生预纯化容器的方法优选地包括在对容器进行减压之后利用富氧吹扫气体来再生预纯化容器,然后利用辅助吹扫气体对预纯化容器进行部分再加压,从而稀释包含在预纯化容器中的气体的氧浓度,并任选地对部分再加压后的容器进行减压。
Description
技术领域
本发明涉及用于再生预纯化容器的***和方法,并且更具体地,涉及用于再生空气分离装置的预纯化容器的方法和***,其中再生吹扫气体是富氧吹扫气体。
背景技术
吸附是用于纯化气体和处理流体废物流的公认技术。大气空气的纯化和分离构成广泛使用吸附方法的主要领域之一。为了提高其效率,正在不断开发新的和改进的预纯化***和方法。
具有强烈商业和技术关注的领域之一代表了空气在其低温蒸馏之前的预纯化。通过低温分离空气来制备氮气(N2)和氧气(O2)以及氩气(Ar)的常规空气分离装置基本上分别由两个或至少三个在非常低的温度下运行的集成式蒸馏塔构成。由于这些低温,必须去除进料到空气分离装置的经压缩的空气中的水蒸气(H2O)和二氧化碳(CO2)。如果不去除,则进料空气中存在的水和二氧化碳将会冻结并堵塞用于在低温蒸馏塔中蒸馏之前使进料空气冷却的热交换器。优选地,为了避免冻结,经压缩和预纯化的空气进料流中的水含量必须小于0.1ppm(份每一百万份),同时经压缩和预纯化的空气进料流中的二氧化碳含量必须小于1.0ppm。通常需要去除烃和一氧化二氮以确保此类低温蒸馏***的安全运行,该低温蒸馏***通常涉及处理富氧气流。
目前用于预纯化进料空气的商业方法包括变温吸附装置,该变温吸附装置采用吸附材料层连同任选的催化预纯化技术。通常使用位于低温蒸馏***上游的预纯化装置,其包括前沿吸附剂层以去除水、二氧化碳以及烃和其它污染物,包括氮氧化物。此类预纯化装置还可任选地包括用于去除一种或多种污染物的一种或多种催化剂,随后是任选催化剂下游的用于去除由催化过程产生的污染物的最终吸附剂层。例如,电子工业和所选择的其它工业的一些低温空气分离应用需要在低温蒸馏***中处理进料空气流以产生高纯度或超高纯度氮气产物之前去除进料空气流中的氢气和/或一氧化碳。
应用于与空气分离装置相关联的此类变温吸附预纯化装置的热再生过程用于解吸预纯化器装置中的各个层中的水、二氧化碳和所选择的其它污染物,诸如烃和一氧化二氮。优选地使用涉及至少四个通用步骤的多步骤过程来进行常规的热再生,即:(i)将预纯化容器减压至适用于再生过程的较低压力;(ii)用加热后的吹扫气体对预纯化容器内的层进行加热,以解吸各个吸附层中的水、二氧化碳和其它污染物并对催化剂层进行清洁;(iii)用较冷的吹扫气体(通常称为冷吹扫气体)使预纯化容器内的层冷却至适合于预纯化过程的温度;以及(iv)将预纯化容器再加压回到预纯化过程所需的较高工作压力。在对预纯化容器进行常规热再生时,热吹扫气体和冷吹扫气体通常包括空气流或废弃富氮空气流。然而,先前也已经采用将富氧流用作热吹扫气体和冷吹扫气体,但需要特别考虑安全性。
空气分离装置的安全运行至关重要。因此,当使用富氧吹扫气体来再生与空气分离装置相关联的预纯化器装置时,如果此类部件接触氧浓度高的气体流,则可能需要对一些管道、容器、阀和其它设备进行特殊的清洁处理或采用特殊的材料以确保安全运行。因此,希望通过确保进行再生之后稀释留存在预纯化器容器中的气体的氧含量,从而确保当预纯化容器循环到纯化步骤时没有富氧空气流动堵塞空气分离装置冷箱或流到冷箱上游的涡轮机械设备,最大程度地减少特殊的清洁/处理和特殊的材料要求(以及相关联的成本)。因此,一直需要改进使用富氧吹扫气体的预纯化装置的再生,以确保在再加压后的预纯化容器中的气体的氧浓度小于或等于约30%摩尔体积,并且更优选地小于或等于约26%摩尔体积,以确保空气分离装置的安全运行并且降低与满足接触富氧气体的部件的特殊设计和处理要求相关联的资金和运营成本。
发明内容
本发明的广义特征在于,作为再生预纯化容器的方法,包括以下步骤:(i)将预纯化容器减压至再生压力,该预纯化容器具有置于其中的一层或多层吸附剂和/或催化剂层;(ii)利用热富氧吹扫气体对置于预纯化容器内的一层或多层吸附剂材料和/或一层或多层催化剂材料进行加热,以解吸一层或多层中的水和二氧化碳;(iii)利用冷富氧吹扫气体将预纯化容器内的一层或多层吸附剂和/或催化剂层冷却;(iv)利用辅助吹扫气体将预纯化容器部分再加压至中间压力,以稀释包含在预纯化容器中的气体的氧浓度;以及(v)将预纯化容器完整再加压至对进料气体进行预纯化的工作压力,其中再加压后的预纯化容器中的气体的氧浓度小于或等于约30%摩尔体积,并且更优选地,氧浓度小于约26%摩尔体积。
在一些实施方案中,将预纯化容器部分再加压的步骤还包括利用辅助吹扫气体将预纯化容器部分再加压,然后对预纯化容器进行减压,并且释放辅助吹扫气体以及留存在预纯化容器内的任何富氧吹扫气体。在其它实施方案中,将预纯化容器部分再加压的步骤还包括利用氮气浓度为或高于约85%摩尔体积的富氮气体将预纯化容器部分再加压,以稀释留存在预纯化容器中的气体的氧浓度。预纯化容器内的一层或多层吸附剂优选地包括活性氧化铝、硅胶、沸石基分子筛、X型沸石或它们的组合,而预纯化容器内的一层或多层含层包括霍加拉特催化剂或贵金属催化剂,诸如氧化铝载钯催化剂。再生压力优选地小于约6.0巴,更优选地介于约1.0巴至2.0巴之间,而工作压力通常大于或等于约6.0巴。
优选地使用加热器将热富氧吹扫气体加热至至少150℃的温度,而冷富氧吹扫气体处于小于或等于约50℃的温度下,这两者优选地来源于蒸馏塔***或空气分离装置的冷凝器的富氧流。辅助吹扫气体优选地为空气,诸如取自预纯化器装置的下游位置的干燥空气流或取自预纯化器装置上游位置的进料空气的分流部分或甚至取自空气分离装置的合成空气流。另选地,辅助吹扫气体可以是取自空气分离装置或位于附近的氮储罐的富氮气体。
附图说明
虽然本说明书的结论是申请人视为其发明内容且明确地指出发明主题的一个或多个权利要求,但据信用于进料气体流的预纯化的本发明***和方法在结合附图考虑时将得到更好的理解,其中:
图1是与空气分离装置相关联的预纯化容器的示意图,所示出的预纯化容器具有一个或多个吸附剂层和/或催化剂层;并且
图2是配置用于与本发明的再生预纯化容器的方法结合使用的双床预纯化装置的示意图,并且示出预纯化装置内的各个流动回路和阀。
具体实施方式
本发明的再生预纯化容器的***和方法针对诸如优选地利用富氧吹扫气体流再生与低温空气分离装置相关联的预纯化装置的应用。
现在转到图1,示出了适合与本发明的***和方法结合使用的预纯化床20的一个实施方案,本发明的***和方法用于预纯化进料气体流,诸如空气。当与空气分离装置相关联时,本发明的用于预纯化进料气体流的***和方法优选地包括至少两个预纯化床,该至少两个预纯化床被构造成纯化在容纳多个吸附层和/或催化剂层的圆柱形容器21的入口22处接纳的进料空气流并且在出口23处输送纯化后的空气流。该至少两个预纯化容器各自还被构造成使用一个或多个富氧吹扫气体流来再生包含在预纯化容器内的吸附层和催化剂层。如本领域众所周知的,在低温空气分离装置中使用两个或更多个预纯化容器使得能够连续生产纯化空气,该纯化空气随后在空气分离装置的冷箱内的蒸馏塔中被分离。当其中的一个或多个预纯化容器正在用于纯化进入的进料空气时,优选地使用被广泛称为热再生的过程来再生一个或多个其它预纯化容器。每个预纯化容器包括多个层,包括一层或多层吸附材料,诸如活性氧化铝和/或沸石基分子筛,以及一层或多层含有催化剂的材料,诸如霍加拉特催化剂和/或贵金属催化剂。
图1中示出的预纯化床20包括置于圆柱形容器21内的第一层氧化铝24和第二层沸石基分子筛25,这两者均构造成通过吸附诸如水蒸气、二氧化碳烃和一氧化二氮之类的杂质来纯化进料气体流。在初始吸附层24、25的下游设置有第三层26,该第三层含有将一氧化碳氧化成二氧化碳并且也吸附氢气和/或将氢气转换为水的霍加拉特,即催化剂材料。含有霍加拉特的层26的下游是任选的沸石基分子筛(未示出),该沸石基分子筛被构造成去除离开含有霍加拉特的层以及任选的含有诸如氧化铝载钯催化剂(例如,0.5wt%的Pd/Al2O3)之类的贵金属催化剂的层(未示出)中的气体流中的水和二氧化碳,该含有贵金属催化剂层被构造成将大部分剩余的氢气氧化成水。还示出了沸石基分子筛的最终封盖层28,该最终封盖层被构造成吸附在含有催化剂材料的层中产生的水蒸气和二氧化碳。也可以将多个诸如蒙乃尔合金(Monel)分离筛网之类的分离筛网27安装在各个催化剂层26与任何相邻的吸附剂层25和28之间。
本发明的***和方法是一种针对在低温空气分离装置中热再生预纯化容器的常规过程进行的修改或改进,并且尤其适用于使用富氧吹扫气体来再生预纯化器装置的预纯化器应用领域。本发明的方法为常规热再生过程中增加一个或多个附加步骤,并且本发明的方法的广义特征在于以下步骤:(i)将预纯化容器减压至适用于预纯化器再生的较低压力;(ii)利用加热后的富氧吹扫气体对预纯化容器内的吸附剂层和催化剂层进行加热,以解吸各个层中的水和二氧化碳并且再生催化剂层;(iii)利用冷富氧吹扫气体将预纯化容器内的吸附剂层和催化剂层冷却至适用于预纯化过程的温度;(iv)在冷却步骤之后,利用辅助吹扫气体对预纯化容器进行部分再加压,从而稀释留存在预纯化容器中的气体的氧浓度,以及任选地对部分再加压后的容器进行减压;(v)将预纯化容器完整再加压回到预纯化过程所需的较高工作压力,其中完整再加压后的预纯化容器中的气体的氧浓度小于或等于约30%摩尔体积,并且更优选地,小于或等于约26%摩尔体积。
具体地,在优选的实施方案中,上述过程的步骤(iv)还包括:(a)利用氧浓度小于约23%的辅助吹扫气体,优选地利用取自预纯化器装置的下游位置的清洁干燥空气流,或可选地利用取自预纯化器装置的上游位置的进料空气流的分流部分,或甚至利用合成空气流(例如,取自空气分离装置的氧流和氮流的混合物),将预纯化容器部分再加压至规定的中间压力;以及(b)通过释放大部分辅助吹扫气体以及任何留存在预纯化容器内的富氧吹扫气体,对预纯化容器进行减压。另选地,步骤(iv)还可包括单一步骤:利用富氮气体,优选地利用氮气浓度高于85%的富氮气体,将预纯化容器部分再加压至规定的中间压力,直至预纯化容器中的氧浓度小于30%摩尔体积,并且更优选地小于或等于约26%摩尔体积。
优选地在与纯化过程期间维持的较高压力相比的诸如1.0巴至2.0巴之类的较低压力下执行预纯化容器的热再生,并且必须在至少150℃的温度下执行,符合适当的安全性要求。通常通过加热吹扫气体以产生热吹扫气体流来执行热再生过程中的加热步骤,该热吹扫气体流经由出口进料到容器并且以与预纯化过程相反的顺序穿过预纯化容器的层。在本发明的方法的许多应用中,吹扫气体可取自低温空气分离装置的蒸馏塔,作为氧产物气体的一部分,或取自富氧沸腾物,或取自从氩冷凝器取出的废气。当富氧热吹扫气体通过预纯化容器的各个层时,再生催化剂层和吸附剂层。通常排出经由入口离开预纯化容器的富氧流出吹扫气体。在加热催化剂层和吸附剂层并使其再生之后,然后使用通常温度为约10℃至50℃的冷富氧吹扫气体冷却预纯化容器中的吸附剂层和催化剂层,该冷富氧吹扫气体沿着与热吹扫气体相同的方向流过预纯化容器。冷却之后,利用辅助吹扫气体稀释预纯化容器中的残余气体的氧浓度,并且将预纯化容器再加压至预纯化过程所需的较高工作压力。
如上述执行再生步骤预定的时间段,该预定的时间段通常被称为循环时间,此后预纯化装置的服务或功能被切换,使得先前再生的容器“在线”并引发纯化过程,而先前纯化进料空气的容器“下线”并引发再生过程。用于生产高纯度或超高纯度氮的空气分离设备的典型预纯化循环时间介于约360分钟至1200分钟之间(即,总循环时间包括共混、纯化服务以及再生服务)。每个预纯化装置在纯化服务和再生服务之间交替,以保持连续产生基本上不含二氧化碳、水、一氧化碳、氢气和其它杂质的纯化空气。
优选地,致密装载附图中示出的预纯化容器。致密负载提供了吸附剂和催化剂的最一致且均匀的填充,其中所需层的找平最小。此外,致密填充使吸附剂沉降最小化。被设计用于一氧化碳和氢气去除的预纯化器的此类致密填充是任选的,并且可用于床中的所有层以确保完整性和均匀的深度。由于用于去除一氧化碳和氢气的第二纯化区段中的相对较薄的层包括多个霍加拉特层和吸附剂层以及可使用的任何基于贵金属的催化剂,重要的是使层的偏移和/或沉降最小化,以便在预纯化器装置的寿命内保持层的均匀深度。
现在转到图2,示意性地示出了双床变温吸附预纯化器装置10。双床变温吸附预纯化器装置10包括两个平行的预纯化器床20和预纯化器床40。预纯化器床20和预纯化器床40各自包括圆柱形容器21、41和填充床,该填充床包括多个吸附剂层和/或催化剂层。
压缩空气流15可通过导管分别经由流31和流51被引导朝向平行的预净化器床20和40中的任一者。阀32和阀52控制进入预纯化器床20和预纯化器床40的进料空气的流动,并且预纯化后的空气通过导管33和导管53从预纯化器床20和预纯化器床40排出,导管33和导管53包含阀34和阀54以控制通过导管33和导管53的预纯化后的空气流的流动。导管33和导管53两者连接,以排出被引导至空气分离装置的冷箱的压缩且预纯化后的空气流60。
如下文更详细论述,富氧吹扫流65可选地由通过热交换器或电加热器66加热,并且通过导管35和导管55进入预纯化器床20和预纯化器床40。富氧吹扫流再生包含在预纯化床20和预纯化床40中的吸附剂。导管35和导管55内的富氧吹扫流分别由阀36和阀56控制。载有先前吸附在预纯化器床20和预纯化器床40内的水蒸气和二氧化碳以及其它杂质的或多或少连续的流出流通过导管37和导管57,并且作为可排出到大气中的废弃流67排放。导管37和导管57内的流出流的流动分别由阀38和阀58控制。
对于在双床变温吸附预纯化器内执行的变温吸附过程,期望使干燥的预纯化后的进料空气连续流动进入相关联的空气分离装置的冷箱。这是通过使用至少两个预纯化器床20和40来完成的,其中至少一个预纯化床处于在线状态并且吸附或催化空气中的杂质,而至少另一个预纯化床处于离线状态并且使其再生。在线预纯化床仅可保持在线,直到其达到吸附杂质的能力并且发生杂质穿透。穿透点通常由污染物(例如,水蒸气和二氧化碳)在出口处达到不可接受的水平(表明污染物使预纯化床饱和)所需的时间定义。一旦达到穿透点,就使在线预纯化器床变为离线并且使先前再生的床恢复为在线以吸附和/或催化杂质。
在本发明的变温吸附过程中,在完整的循环通常有多达8个步骤,每个预纯化器床经历连续重复的步骤。这八个步骤即“共混”;‘纯化’;‘减压’;‘热吹扫’;‘冷吹扫’;‘部分再加压’;‘部分减压’,以及‘完整再加压’。下面的表1结合图2示出使用两个预纯化器床20和40以及空气的辅助吹扫气体的预纯化循环内的多个步骤的性能的相关性,这将在下面的段落中更详细地描述。
表1
在‘共混’步骤期间,两个预纯化床20、40均处于“在线”状态,并且阀32、阀34、阀52和阀54打开,而阀36、阀38、阀56和阀58关闭。在该步骤期间,进料空气流15在两个床之间均匀地分流,而***中没有再生气体65。处于在线状态时,预纯化床20和预纯化床40正在吸附水蒸气、二氧化碳和其它污染物,而存在的任何催化剂将会使诸如一氧化碳和氢气之类的杂质氧化。该“共混’步骤的目的是稀释在再生期间残留在预纯化床中的残余热量,并且进一步稀释所得共混流的氧含量,从而防止加热后的流或富氧流被进料返回到空气分离装置的冷箱中。
在约30分钟的‘共混’步骤之后,其中一个预纯化器床20经受减压或‘减压’步骤并且处于离线状态,而另一个预纯化器床40接纳完整的进料流并且经历‘纯化’步骤,在‘纯化’步骤中,去除水蒸气、二氧化碳和其它杂质,诸如一氧化二氮、烃、一氧化碳、氢气。“离线”的预纯化床20通常被称为经历再生。通过五个或六个不同的步骤完成此类再生,这些步骤依次包括:(i)‘减压’;(ii)‘热吹扫’;(iii)‘冷吹扫’;(iv)利用辅助吹扫气体进行‘部分再加压’;(v)‘部分减压’(任选的);以及(vi)利用空气进行‘完整再加压’。在‘减压’期间,预纯化器床20从工作压力减压至称为再生压力的较低压力,该较低压力小于约6.0巴并且更优选地小于2.0巴并且通常刚好高于大气压。这通过关闭阀32、阀34和阀36的同时打开阀38来完成。‘减压’通常持续约15分钟,尽管‘减压’步骤的持续时间可发生变化,这取决于设备约束或过程限制。一旦减压,‘热吹扫’步骤就开始于使用加热器66将富氧吹扫气体流65加热至高于进料温度并且优选地至少150℃的温度,这取决于预纯化过程和材料约束,并且由于吹扫气体流中的氧浓度较高而通常不高于约190℃。在该‘热吹扫’步骤期间,阀36打开并且允许加热后的富氧吹扫气体流通过导管35和导管37通过预纯化器床20。
在经过一定时间段之后,在本示例中,在163分钟之后,富氧吹扫气体流绕过加热器66或关闭加热器66,从而将富氧吹扫气体流温度降低至接近环境条件并且通常小于或等于约50℃。这就开始‘冷吹扫’步骤,‘冷吹扫’步骤继续利用富氧流65但没有热量进行吹扫。该‘冷吹扫’步骤降低预纯化床20的温度以及使热前锋前进通过预纯化床。在本示例中,‘冷吹扫’步骤持续约272分钟。
然后,通过关闭阀36和阀38并且打开阀72以将辅助吹扫气体70经由导管73引入到预纯化床20中持续指定持续时间(例如,6至15分钟)和/或至预纯化容器20达到介于再生压力与工作压力之间的中间压力来进行‘部分再加压’步骤。优选在靠近吹扫阀和预纯化容器的清洁端部(例如,靠近阀36、阀56和出口23)的位置处将辅助吹扫气体引入到预纯化容器中,并且从靠近预纯化容器的脏污端部(例如,靠近入口23)的位置去除辅助吹扫气体和任何留存的富氧吹扫气体。这种优选的布置确保在完整再加压步骤之后,在吹扫阀或预纯化容器的清洁端部处或附近不堵塞有富氧气体。
在利用清洁干燥空气或合成空气作为辅助吹扫气体70的实施方案中,部分再加压持续约6分钟,然后通过打开阀38并且关闭阀72的同时还保持阀36、阀34和阀32关闭另外9分钟的持续时间来使预纯化床20部分减压。当预纯化器床中的氧浓度降低至小于或等于约30%摩尔体积,并且更优选地小于或等于约26%摩尔体积时,部分减压步骤结束。
在利用氮流作为辅助吹扫气体70的实施方案中,氮流的氮浓度优选地高于85%摩尔体积,部分再加压步骤可持续多达15分钟。当预纯化器床中的氧浓度降低至小于或等于约30%摩尔体积,并且更优选地小于或等于约26%摩尔体积时,部分再加压步骤结束。
然后,通过保持阀34和阀38关闭并且打开阀72或阀32,再生过程继续进行‘完整再加压’步骤。如果阀32打开,这允许纯化后的压缩空气流15的一部分将预纯化床20加压至完整工作压力。另选地,如果辅助吹扫气体是空气流或合成空气流,则打开阀72以将预纯化床20加压回到完整工作压力。一旦加压到工作压力,预纯化床20和预纯化床40两者均进入“共混”步骤,因此,阀32、阀34、阀52和阀54完全打开,允许进料空气流15在预净化床20与预净化床40之间均匀分流并且被净化。在‘共混’步骤经历一定时间之后,预纯化床切换并且预纯化床20在‘纯化’步骤中处于在线状态,而预纯化床40经历如以上参照表1所概述的一系列再生步骤。
虽然已参照一个或多个优选的实施方案描述了本发明***和方法,但是应当理解,在不脱离所附权利要求书所示的本发明的实质和范围的情况下,可进行多种添加、改变和省略。例如,当前本发明所公开的***和方法针对使用热再生和变温吸附预纯化技术的应用,预期可以对本发明的***和方法进行调整或进一步修改以与变压吸附预纯化装置和/或使用变压吸附预纯化技术和变温吸附预纯化技术两者的混合型预纯化器装置结合使用。
Claims (17)
1.一种再生预纯化容器的方法,所述方法包括以下步骤:
(i)将预纯化容器减压至再生压力,所述预纯化容器具有置于其中的一层或多层吸附剂和/或催化剂层;
(ii)利用热富氧吹扫气体对置于所述预纯化容器内的所述一层或多层吸附剂材料和/或所述一层或多层催化剂材料进行加热,以解吸所述一层或多层中的水和二氧化碳;
(iii)利用冷富氧吹扫气体将所述预纯化容器内的所述一层或多层吸附剂和/或所述催化剂层冷却至适用于预纯化过程的温度;
(iv)在所述冷却步骤之后,利用辅助吹扫气体对所述预纯化容器进行部分再加压,以稀释包含在所述预纯化容器中的气体的氧浓度;
(v)将所述预纯化容器完整再加压至对进料气体进行预纯化的工作压力,其中所述再加压后的预纯化容器中的所述气体的氧浓度小于或等于约30%摩尔体积。
2.根据权利要求1所述的方法,其中所述再加压后的预纯化容器中的所述气体的氧浓度小于或等于约26%摩尔体积。
3.根据权利要求1所述的方法,其中利用辅助吹扫气体对所述预纯化容器进行部分再加压的所述步骤还包括利用辅助吹扫气体将所述预纯化容器部分再加压至中间压力;然后对所述预纯化容器进行减压,并且释放所述辅助吹扫气体以及留存在所述预纯化容器内的任何富氧吹扫气体。
4.根据权利要求1所述的方法,其中利用辅助吹扫气体对所述预纯化容器进行部分再加压的所述步骤还包括利用氮气浓度高于85%摩尔体积的富氮气体将所述预纯化容器部分再加压至中间压力,从而稀释留存在所述预纯化容器中的气体的氧浓度。
5.根据权利要求1所述的方法,其中所述热富氧吹扫气体的温度为至少150℃。
6.根据权利要求1所述的方法,其中所述冷富氧吹扫气体的温度低于或等于约50℃。
7.根据权利要求1所述的方法,其中所述预纯化容器联接到空气分离装置,并且所述进料气体是空气,其中所述预纯化容器内的所述一层或多层吸附剂包括活性氧化铝、硅胶、沸石基分子筛、X型沸石或它们的组合,并且被构造成去除所述进料气体中的杂质,包括水、二氧化碳和其它污染物。
8.根据权利要求7所述的方法,其中所述预纯化容器内的所述一层或多层催化剂包括霍加拉特催化剂或贵金属催化剂并且被构造成去除杂质,包括氢气和一氧化碳。
9.根据权利要求1所述的方法,其中所述预纯化容器联接到空气分离装置,并且所述热富氧吹扫气体和所述冷富氧吹扫气体取自所述空气分离装置的蒸馏塔***的富氧流。
10.根据权利要求9所述的方法,其中利用所述热富氧吹扫气体对所述一层或多层吸附剂材料和/或所述一层或多层催化剂材料进行加热的所述步骤还包括使用电加热器、燃气加热器或蒸汽加热器对所述富氧流进行加热。
11.根据权利要求1所述的方法,其中所述预纯化容器联接到产生氩气的空气分离装置,并且所述热富氧吹扫气体和所述冷富氧吹扫气体是取自与所述空气分离装置相关联的氩气冷凝器的富氧流。
12.根据权利要求3所述的方法,其中所述再生压力小于约6.0巴;所述工作压力大于或等于约6.0巴;并且所述中间压力介于所述再生压力和所述工作压力之间。
13.根据权利要求3所述的方法,其中所述预纯化容器联接到空气分离装置,并且所述辅助吹扫气体还包括从与所述空气分离装置相关联的预纯化器装置的下游位置取得的干燥空气流,或者从与所述空气分离装置相关联的所述预纯化器装置的上游位置取得的进料空气的分流部分,或者从所述空气分离装置取得的合成空气流。
14.根据权利要求3所述的方法,其中辅助吹扫气体经由辅助纯化控制阀在出口处或者所述出口附近被引入到所述预纯化容器,并且在减压期间,经由部分减压控制阀或所述减压控制阀在所述出口处或所述出口附近释放所述预纯化容器中的所述辅助吹扫气体和任何留存的气体。
15.根据权利要求4所述的方法,其中所述预纯化容器联接到空气分离装置,并且所述富氮流取自所述空气分离装置或氮储罐。
16.根据权利要求4所述的方法,其中富氮气体经由辅助吹扫气体控制阀在所述出口处或所述出口附近被引入到所述预纯化容器中。
17.根据权利要求4所述的方法,其中所述再生压力小于约6.0巴;所述工作压力大于或等于约6.0巴;并且所述中间压力介于所述再生压力和所述工作压力之间。
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US17/234100 | 2021-04-19 | ||
US17/234,100 US11619442B2 (en) | 2021-04-19 | 2021-04-19 | Method for regenerating a pre-purification vessel |
PCT/US2021/054455 WO2022225553A1 (en) | 2021-04-19 | 2021-10-12 | Method for regenerating a pre-purification vessel |
Publications (1)
Publication Number | Publication Date |
---|---|
CN117241874A true CN117241874A (zh) | 2023-12-15 |
Family
ID=78516948
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN202180097229.XA Pending CN117241874A (zh) | 2021-04-19 | 2021-10-12 | 用于再生预纯化容器的方法 |
Country Status (5)
Country | Link |
---|---|
US (1) | US11619442B2 (zh) |
EP (1) | EP4326421A1 (zh) |
KR (1) | KR20230171459A (zh) |
CN (1) | CN117241874A (zh) |
WO (1) | WO2022225553A1 (zh) |
Family Cites Families (31)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS59150286A (ja) | 1983-02-15 | 1984-08-28 | 日本酸素株式会社 | アルゴンの製造方法 |
US4822395A (en) | 1988-06-02 | 1989-04-18 | Union Carbide Corporation | Air separation process and apparatus for high argon recovery and moderate pressure nitrogen recovery |
US5069698A (en) | 1990-11-06 | 1991-12-03 | Union Carbide Industrial Gases Technology Corporation | Xenon production system |
US5255522A (en) | 1992-02-13 | 1993-10-26 | Air Products And Chemicals, Inc. | Vaporization of liquid oxygen for increased argon recovery |
US5355681A (en) | 1993-09-23 | 1994-10-18 | Air Products And Chemicals, Inc. | Air separation schemes for oxygen and nitrogen coproduction as gas and/or liquid products |
US5440884A (en) | 1994-07-14 | 1995-08-15 | Praxair Technology, Inc. | Cryogenic air separation system with liquid air stripping |
US5469710A (en) | 1994-10-26 | 1995-11-28 | Praxair Technology, Inc. | Cryogenic rectification system with enhanced argon recovery |
US5722259A (en) | 1996-03-13 | 1998-03-03 | Air Products And Chemicals, Inc. | Combustion turbine and elevated pressure air separation system with argon recovery |
ATE228101T1 (de) | 1996-08-27 | 2002-12-15 | Boc Group Inc | Rückgewinnung von edelgasen |
US5956973A (en) | 1997-02-11 | 1999-09-28 | Air Products And Chemicals, Inc. | Air separation with intermediate pressure vaporization and expansion |
US5802873A (en) | 1997-05-08 | 1998-09-08 | Praxair Technology, Inc. | Cryogenic rectification system with dual feed air turboexpansion |
US5934104A (en) | 1998-06-02 | 1999-08-10 | Air Products And Chemicals, Inc. | Multiple column nitrogen generators with oxygen coproduction |
US6106593A (en) | 1998-10-08 | 2000-08-22 | Air Products And Chemicals, Inc. | Purification of air |
US6173586B1 (en) | 1999-08-31 | 2001-01-16 | Praxair Technology, Inc. | Cryogenic rectification system for producing very high purity oxygen |
US6397632B1 (en) | 2001-07-11 | 2002-06-04 | Praxair Technology, Inc. | Gryogenic rectification method for increased argon production |
US7533540B2 (en) | 2006-03-10 | 2009-05-19 | Praxair Technology, Inc. | Cryogenic air separation system for enhanced liquid production |
US7632337B2 (en) | 2006-06-30 | 2009-12-15 | Praxair Technology, Inc. | Air prepurification for cryogenic air separation |
US20080223077A1 (en) | 2007-03-13 | 2008-09-18 | Neil Mark Prosser | Air separation method |
US8286446B2 (en) | 2008-05-07 | 2012-10-16 | Praxair Technology, Inc. | Method and apparatus for separating air |
US8443625B2 (en) | 2008-08-14 | 2013-05-21 | Praxair Technology, Inc. | Krypton and xenon recovery method |
JP5577044B2 (ja) | 2009-03-11 | 2014-08-20 | 大陽日酸株式会社 | 空気の精製方法 |
US20120036891A1 (en) | 2010-08-12 | 2012-02-16 | Neil Mark Prosser | Air separation method and apparatus |
US8647409B2 (en) | 2012-05-24 | 2014-02-11 | Praxair Technology, Inc. | Air compression system and method |
US9644890B2 (en) | 2013-03-01 | 2017-05-09 | Praxair Technology, Inc. | Argon production method and apparatus |
US8940263B2 (en) | 2013-04-10 | 2015-01-27 | Air Products And Chemicals, Inc. | Removal of hydrogen and carbon monoxide impurities from gas streams |
US20160025408A1 (en) | 2014-07-28 | 2016-01-28 | Zhengrong Xu | Air separation method and apparatus |
US10066871B2 (en) | 2015-07-31 | 2018-09-04 | Praxair Technology, Inc. | Method and apparatus for argon rejection and recovery |
US10024596B2 (en) | 2015-07-31 | 2018-07-17 | Praxair Technology, Inc. | Method and apparatus for argon recovery in a cryogenic air separation unit integrated with a pressure swing adsorption system |
KR102137940B1 (ko) | 2015-12-14 | 2020-07-27 | 엑손모빌 업스트림 리서치 캄파니 | 액화 질소를 사용하여 액화 천연 가스로부터 질소를 분리하기 위한 방법 및 시스템 |
US10663222B2 (en) | 2018-04-25 | 2020-05-26 | Praxair Technology, Inc. | System and method for enhanced recovery of argon and oxygen from a nitrogen producing cryogenic air separation unit |
US10663224B2 (en) | 2018-04-25 | 2020-05-26 | Praxair Technology, Inc. | System and method for enhanced recovery of argon and oxygen from a nitrogen producing cryogenic air separation unit |
-
2021
- 2021-04-19 US US17/234,100 patent/US11619442B2/en active Active
- 2021-10-12 KR KR1020237038998A patent/KR20230171459A/ko unknown
- 2021-10-12 CN CN202180097229.XA patent/CN117241874A/zh active Pending
- 2021-10-12 WO PCT/US2021/054455 patent/WO2022225553A1/en active Application Filing
- 2021-10-12 EP EP21802513.8A patent/EP4326421A1/en active Pending
Also Published As
Publication number | Publication date |
---|---|
WO2022225553A1 (en) | 2022-10-27 |
US20220333860A1 (en) | 2022-10-20 |
KR20230171459A (ko) | 2023-12-20 |
EP4326421A1 (en) | 2024-02-28 |
US11619442B2 (en) | 2023-04-04 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
JP3279585B2 (ja) | 精製された空気の製造法 | |
US6048509A (en) | Gas purifying process and gas purifying apparatus | |
US5202096A (en) | Apparatus for low temperature purification of gases | |
EP1427508B1 (en) | Helium recovery | |
JP3351815B2 (ja) | 不活性ガスの精製方法 | |
KR100328419B1 (ko) | 청정 건조 공기 생성물 스트림 생성 방법, 공기 분리 방법 및 청정 건조 공기 생성물 스트림 생성 장치 | |
KR102570998B1 (ko) | 공급 기체 스트림의 예비정제를 위한 시스템 및 방법 | |
KR102436871B1 (ko) | 공급 기체 스트림의 예비정제를 위한 방법 및 시스템 | |
CN117241874A (zh) | 用于再生预纯化容器的方法 | |
TWI809444B (zh) | 用於預純化進料氣流之方法 | |
KR102570997B1 (ko) | 공급 기체 스트림의 예비정제를 위한 시스템 | |
US20230285898A1 (en) | System and method for pre-purification of a feed gas stream | |
US20050252374A1 (en) | Adsorbent bed and process for removal of propane from feed streams |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PB01 | Publication | ||
PB01 | Publication | ||
SE01 | Entry into force of request for substantive examination | ||
SE01 | Entry into force of request for substantive examination |