CN116390797A - 用于从低品级氢气生产超高纯氢气的工艺和设备 - Google Patents
用于从低品级氢气生产超高纯氢气的工艺和设备 Download PDFInfo
- Publication number
- CN116390797A CN116390797A CN202180074382.0A CN202180074382A CN116390797A CN 116390797 A CN116390797 A CN 116390797A CN 202180074382 A CN202180074382 A CN 202180074382A CN 116390797 A CN116390797 A CN 116390797A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- adsorption
- pressure
- gas
- purge
- 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
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
- B01J20/16—Alumino-silicates
- B01J20/18—Synthetic zeolitic molecular sieves
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- 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
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0423—Beds in columns
-
- 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
- B01D53/047—Pressure swing adsorption
- B01D53/0476—Vacuum pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
- B01J20/28014—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their form
- B01J20/28052—Several layers of identical or different sorbents stacked in a housing, e.g. in a column
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3408—Regenerating or reactivating of aluminosilicate molecular sieves
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3416—Regenerating or reactivating of sorbents or filter aids comprising free carbon, e.g. activated carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3491—Regenerating or reactivating by pressure treatment
-
- 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
- B01D2253/102—Carbon
-
- 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
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/16—Hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
- B01D2257/7022—Aliphatic hydrocarbons
- B01D2257/7025—Methane
-
- 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
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40013—Pressurization
- B01D2259/40016—Pressurization with three sub-steps
-
- 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
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40028—Depressurization
- B01D2259/40032—Depressurization with three sub-steps
-
- 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
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40035—Equalization
- B01D2259/40039—Equalization with three sub-steps
-
- 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
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40035—Equalization
- B01D2259/40041—Equalization with more than three sub-steps
-
- 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
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40043—Purging
-
- 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
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40043—Purging
- B01D2259/40045—Purging with two sub-steps
-
- 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
- B01D2259/406—Further details for adsorption processes and devices using more than four beds
- B01D2259/4062—Further details for adsorption processes and devices using more than four beds using six beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
- B01J20/16—Alumino-silicates
- B01J20/165—Natural alumino-silicates, e.g. zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/32—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating
- B01J20/3231—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating characterised by the coating or impregnating layer
- B01J20/3234—Inorganic material layers
- B01J20/324—Inorganic material layers containing free carbon, e.g. activated carbon
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2220/00—Aspects relating to sorbent materials
- B01J2220/40—Aspects relating to the composition of sorbent or filter aid materials
- B01J2220/48—Sorbents characterised by the starting material used for their preparation
- B01J2220/4875—Sorbents characterised by the starting material used for their preparation the starting material being a waste, residue or of undefined composition
- B01J2220/4881—Residues from shells, e.g. eggshells, mollusk shells
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2220/00—Aspects relating to sorbent materials
- B01J2220/50—Aspects relating to the use of sorbent or filter aid materials
- B01J2220/60—Use in several different columns
- B01J2220/606—Use in several different columns parallel disposed columns
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0001—Separation or purification processing
- C01B2210/0009—Physical processing
- C01B2210/0014—Physical processing by adsorption in solids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0042—Making ultrapure specific gas
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0043—Impurity removed
- C01B2210/0045—Oxygen
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0043—Impurity removed
- C01B2210/0046—Nitrogen
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2210/00—Purification or separation of specific gases
- C01B2210/0043—Impurity removed
- C01B2210/0068—Organic compounds
- C01B2210/007—Hydrocarbons
-
- 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
- Y02C20/20—Capture or disposal of greenhouse gases of methane
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Separation Of Gases By Adsorption (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
本发明公开了一种工艺和多塔真空变压吸附装置,所述工艺和装置用于在1.2MPa‑3.0MPa从含有95.0vol%‑99.9vol%氢气和一种或多种杂质的原料气中生产超高纯氢气(≥99.997vol%)。在本发明中,所述装置包括六个并联的吸附塔、对应每个塔的五个控制阀、原料气缓冲罐、产品气缓冲罐和真空泵。在本发明的装置中实现真空变压吸附(VPSA)循环的工艺包括3步或3步以上的顺流减压步骤、3步或3步以上的逆流加压步骤和1步真空吹扫。所述工艺可以通过自动或程序控制、优化输出和低成本操作,在专门设计的撬块或集装箱上完成,用于根据工业气体、医药用途和氢能应用生产和供应超高纯氢气。
Description
高纯度氢气(H2)是一种用于各种工业加工过程、航空航天领域以及医疗医用领域的传统工业气体。同时,它还极大地推动新兴氢能源应用。动态发展的氢能燃料电池提供了广泛的优势,包括最大限度地减少二氧化碳排放、为燃料电池汽车提供动力、以及将电能转化为氢气作为能量转换和储存。为了保证氢燃料电池以高能量效率和可靠性使用,氢气需要至少99.97vol%的纯度。最重要的是,氢气中的杂质被严格限制在一定水平内,例如甲烷低于100ppm,总烃类(除甲烷外)低于2ppm,氧气低于5ppm,氮气低于300ppm,二氧化碳低于2ppm,一氧化碳低于0.2ppm。氢燃料电池可预测的激增和应用需要有效和高效地生产超高纯氢气。
技术领域
本发明涉及一种真空变压吸附(VPSA)工艺和与所述VPSA工艺对应的多塔装置,所述工艺和装置用于从低品级纯氢气流(≥95vol%)生产超高纯氢气(≥99.997vol%)。
背景技术
目前,通过变压吸附(PSA)工艺生产纯氢是一种工业成熟的工艺。典型的PSA系统包含多个吸附塔(也称为“吸附床”),每个独立的吸附塔都按程序化的和计划的顺序运行,称之为PSA循环。PSA循环包括许多众所周知的步骤,一个特定的PSA应用需要技术人员以合适的方式组合已知的步骤以实现所需的分离目标。这些已知的步骤包括但不限于:进料和吸附步骤、顺流均压步骤、顺流提供吹扫步骤、逆流吹扫和脱附步骤、逆流均压步骤和再加压步骤。美国专利(9,381,460 B2)包括了对各种氢气PSA步骤的综合性描述,同时也描述了几个在工业中用于从气体混合物中分离氢气的、组合这些步骤的实际循环。但是,在每个列出的循环中,都没有定义氢气产品的规格,大概,它们在典型的工业纯氢气的范围内。
通常,工业用纯氢气由甲烷蒸汽重整(SMR)或类似的工艺体系生产。来自工业氢气PSA工艺的氢气纯度通常在95.0vol%-99.9vol%的范围内,而来自这些工艺的杂质含量水平并未按照燃料电池氢气的要求进行严格控制。因此,需要比传统氢气PSA工艺更先进的纯化技术来获得高/超高纯氢气。
目前用于将从传统PSA工艺获得的低品级氢气产品(典型的氢气在95.0vol%-99.9vol%的范围内)升级为超高纯氢气的纯化方法包括多级氢气PSA、低温变温吸附工艺(Cryo-TSA)、钯基合金膜氢分离技术和通过金属氢化物提纯氢的方法。多级氢气PSA不可避免地需要更多投资成本和额外的能源消耗。
Cryo-TSA工艺需要将氢气原料气和吸附塔冷却至液氮温度(-196℃)。吸附剂在该温度下吸附杂质,同时获得高于99.999vol%的高纯氢气作为产品气。为了使吸附剂再生,需要将吸附塔中的温度重新加热到正常环境温度。由于较大的温度波动范围和制冷剂的使用,与传统的PSA工艺相比,Cryo-TSA需要格外高的能耗、对建造材料的特殊考虑和液体系统的额外控制机制。
钯基合金膜在较高的温度(400-500℃)下对氢气具有单一选择性。可以通过精心设计的设备利用这一特性来生产含有超过99.999vol%氢气的超高纯氢气产品。然而,钯膜的高成本和低产量阻碍了该工艺在超高纯氢气的大规模生产中的普及。
通过金属氢化物提纯氢气是一种化学吸附过程,使用金属合金与氢气发生化学反应以形成金属氢化物,大部分氢气被固定在固相中、而杂质留在气相中,从而使氢气与杂质分离。此后,可以通过氢化物形成反应的逆反应,分解金属氢化物来收集超高纯氢气(≥99.999vol%)。这种工艺的主要问题是金属合金的稳定性,金属合金的性能在几个吸附/释放循环后会迅速衰减,因此需要经常性的维护和更换吸附剂。
为避免上述工艺存在的缺点,北京环宇京辉京城气体科技有限公司提出了一种新的方法。他们的中国专利(CN105,268,282A)描述了一种低温PSA工艺,包括四个并联的吸附塔和11个连续步骤(一个吸附步骤、三组提供和接收均压步骤、顺流和逆流吹气步骤,以及再加压步骤),在-30到-35℃将含99.999vol%氢气的原料气纯化为含99.99999vol%氢气的超高纯氢气。这个发明提出了一种将成熟的PSA步骤创新为新的PSA循环以获得超高纯氢气的技术途径,尽管这个发明所生产的氢气产品规格远高于获得超高纯氢气的目的,此外该发明中使用的零下温度也需要大量额外的能量消耗。
发明内容
本发明是在上述情形下提出的。本发明提供一种工艺和多塔真空变压吸附(VPSA)装置,所述工艺和装置用于从含有95.0vol%-99.9vol%氢气和一种或多种杂质的原料气中生产纯度超过99.997vol%的氢气。在本发明中,所述装置包括六个或更多个并联的吸附塔、对应每个塔的五个控制阀、原料气缓冲罐、产品气缓冲罐和真空泵。在本发明的装置中实现真空变压吸附循环的工艺包括3步或3步以上的顺流减压步骤、3步或3步以上的逆流加压步骤和1步真空吹扫。
附图说明
在附图中:
图1
[图1]是实施本发明VPSA工艺来提纯高纯氢的六床VPSA系统的示意图;
图2
[图2]是本发明的六床VPSA装置所运行的12步VPSA循环的工艺&流程图。
具体实施方式
根据本发明的第一方面,提供了一种通过真空变压吸附将低品级氢气纯化为超高纯氢气的工艺,该工艺使用六个或更多个各自填充有吸附剂的吸附塔。每个吸附塔被编程为重复执行相同的含12个步骤的依序循环。但在某一时刻,六个吸附塔分别运行不同步骤,以便六个吸附塔能够协同运行以满足氢气原料气的连续利用和提供超高纯氢气的连续生产。下面描述的过程是关注于六个吸附塔中的一个吸附塔来进行的。
重复执行的多步骤循环包括:
(a)吸附步骤:使原料气通过吸附塔以将杂质吸附在吸附剂上,并得到排出气作为超高纯氢气产品。
(b)吸附和提供再加压步骤:在吸附步骤的基础上,将所述吸附塔的部分排出气引入正在进行再加压步骤的另一吸附塔中。
(c)第一顺流均压减压步骤:在吸附步骤后,所述吸附塔中的气体顺流流至正在进行逆流均压加压步骤的另一吸附塔,直至两个相连的吸附塔内的压力达到相同水平。
(d)第二顺流均压减压步骤:在第一均压减压步骤后,所述吸附塔中的气体顺流流至另一正在进行第二逆流均压加压步骤的吸附塔,直至两个相连的吸附塔内的压力达到相同水平。
(e)第三顺流均压减压步骤:在第二均压减压步骤后,所述吸附塔中的气体顺流流至正在进行第三逆流均压加压步骤的另一吸附塔,直至两个相连的吸附塔内的压力达到相同水平。
(f)顺流提供吹扫步骤:在第三顺流均压减压步骤之后,所述吸附塔中的剩余气体顺流流至正在进行接收吹扫步骤的另一吸附塔。
(g)脱附步骤:所述吸附塔中的气体被强制性地逆流流出所述吸附塔底部,排空力由与所述吸附塔连接的真空泵提供,所有抽出的气体被认为是脱附气产品。
(h)逆流真空吹扫步骤:在脱附步骤之后,所述吸附塔从顶部接收来自正在进行顺流提供吹扫步骤的另一吸附塔的气流,同时来自位于底部的真空泵的抽空继续产生脱附气产品。
(i)第三逆流均压加压步骤:气流从所述吸附塔顶部逆流流动以对所述吸附塔加压,所述气流来自正在进行第三顺流均压减压步骤的另一吸附塔,直至两个相连的吸附塔内的压力达到相同水平。
(j)第二逆流均压加压步骤:气流从所述吸附塔顶部逆流流动以对所述吸附塔加压,所述气流来自正在进行第二顺流均压减压步骤的另一吸附塔,直至两个相连的吸附塔内的压力达到相同水平。
(k)第一逆流均压加压步骤:气流从所述吸附塔顶部逆流流动以对所述吸附塔加压,所述气流来自正在进行第一顺流均压减压步骤的另一吸附塔,直至两个相连的吸附塔内的压力达到相同水平。
(l)产品气再加压步骤:来自产品气缓冲罐的气流从所述吸附塔顶部逆流流动以对所述吸附塔加压。在步骤(l)之后,所述吸附塔将再次运行步骤(a)以进行另一个PSA循环。
据此,通过所述真空变压吸附工艺获得了超高纯氢气产品(≥99.997vol%)。
优选的,要通过所述工艺纯化的纯氢气原料气含有95.0vol%-99.9vol%的氢气,余量为包括氮气(N2)、氧气(O2)、甲烷(CH4)、烃类(HCs)、二氧化碳(CO2)和一氧化碳(CO)的副成分,纯氢气原料气的压力在1.2MPa-3.0MPa表压范围内。
优选的,在步骤(g)脱附步骤和步骤(h)逆流吹扫步骤中,真空泵将吸附塔抽真空至10-50kPa的绝对压力水平。
在一个变形例中,每个吸附塔包括以25%-75%的比例装填在纯氢气原料气的流动方向的上游部分的活性炭(第一吸附剂)或类似物层,和以25%-75%的比例装填在纯氢气原料气的流动方向的下游部分的沸石类吸附剂(第二吸附剂)或类似物的计算层。合适的活性炭包括但不限于椰壳活性炭。合适的沸石类吸附剂包括但不限于5A、CaX、LiX、13X、LiA沸石。
氢气回收率,定义为超高纯氢气产品(>99.997vol%)中氢气的总摩尔量除以纯氢气原料气中氢气的摩尔量。本发明所述工艺的氢气回收率非常高,通常大于85%,更优选大于90%。这通常远高于其他已公开的用于超高纯氢气生产的氢气PSA工艺,后者通常可实现60%-80%的氢气回收率。
在本发明的工艺中应用了两个创造性的设计:(1)不同于传统的氢气PSA工艺中使用氢气产品气作为吹扫载气的方法,本发明中使用了吸附塔中的剩余气体作为吹扫载气;(2)使用真空泵为脱附步骤和吹扫步骤提供额外的抽空驱动力。如果没有这两种创造性设计中的任何一种,氢气产品气的回收率以及纯度将在很大程度上受到影响。
使用剩余气体代替氢气产品气作为吹扫载气可以提高氢气的回收率,因为这避免了任何已纯化的氢气回流到吸附塔内并随后留在吸附塔底部作为废气。本质上,这种替代的吹扫载气在本发明中有效工作的原因是氢气原料气的纯度大于95%。由于原料气中的杂质含量低,在所有均压步骤后吸附塔中的剩余气体仍将是足够纯净的氢气流,类似于传统氢气PSA工艺中的产品气。因此,传统氢气PSA工艺中使用氢气产品气作为吹扫载气的惯性思维不再是最佳选择,反而由于本发明中的特定原料气条件,使用所有均压步骤后吸附塔中的剩余气体作为吹扫载气,在氢气回收方面具有显著优势。
真空泵的使用是本发明的另一个重要特征。作为吸附工艺技术的一般规则,提高吸附剂的再生能力总能提高吸附工艺的性能。特别是在本发明中杂质含量较低的情况下,需要更强大的再生驱动力-在本发明中即为真空-以深度清洁在每个VPSA循环中吸附在吸附剂上的杂质,从而使吸附剂在下一个吸附循环中能够吸附大多数的新的杂质。
根据本发明,一个专门建造的装置,即使用六个填充有精心设计的吸附剂的吸附塔的VPSA装置,可以将低品级纯氢气纯化为99.997%或更高的超高纯氢气。
这种VPSA装置可以实现本发明第一方面的工艺,因此具有与上述关于本发明描述的那些相同的优点。下面的实施例部分给出了本发明的应用实例。
下面结合附图1和2描述本发明的装置的一个优选实施方式。
吸附塔1、2、3、4、5和6并联设置。吸附塔被配置为使用吸附剂从由路径8供应的原料气中吸附除氢气组分以外的吸附目标组分,然后产生通过路经10排出的产品气。
用于供应原料气的原料气供应路径8将原料气缓冲罐8a与六个吸附塔的下部相连。每个吸附塔的原料气供应路径上的原料气供应控制阀1a、2a、3a、4a、5a和6a打开和关闭给相应单个吸附塔的原料气供应。
用于排出脱附气体的脱附路径9与六个吸附塔的下部相连。在脱附路径上安装有真空泵7,以将脱附路径中的压力降低至10-50kPa.A的绝对压力。相应吸附塔的脱附路径上的脱附气控制阀1b、2b、3b、4b、5b、6b打开和关闭通向真空泵7的脱附气体排出路径。侧路控制阀7a与真空泵并联,所述侧路控制阀7a被编程为当脱附排出路径内的绝对压力高于0.11MPa.A时打开排出侧路,反之,当脱附排出路径内的绝对压力低于0.11MPa.A时则关闭侧路。真空泵7的气体出口侧与脱附气缓冲罐9a连接。
用于提供氢气产品气的产品气路径10连接在六个吸附塔的上部和产品气缓冲罐10a之间。每个吸附塔的产品气路径上的产品气控制阀1f、2f、3f、4f、5f、6f打开和关闭通向产品气缓冲罐的相应吸附塔的产品气排出路径。
此外,吸附塔的上部连接有两组均压调节控制阀。在第一均压路径11上,均压调节控制阀1c、2c、3c、4c、5c和6c通过打开/关闭对应的调节控制阀来控制任意两个吸附塔的连通模式。同样地,在第二均压路径12上,均压调节控制阀1d、2d、3d、4d、5d、6d通过打开/关闭对应的调节控制阀来控制任意两个吸附塔之间的连通模式。优选地,在本实施方式中,第一均压路径11用于上述的第三均压步骤和吹扫步骤,而第二均压路径12用于第二和第一均压步骤。
另一组控制阀1e、2e、3e、4e、5e和6e连接产品气缓冲罐10a和在再加压路径13上的吸附塔。再加压控制阀1e、2e、3e、4e、5e和6e打开和关闭相应的再加压路径,所述再加压路径允许产品气罐中的超高纯氢气回流到吸附塔以使吸附塔充压至进料压力。
参照上述实施方式,所述的12步VPSA循环可由此实施以纯化纯氢气原料气来获得超高纯氢气产品。具体地,所有12个VPSA步骤被控制在六个吸附塔中并行运行。以下说明了12步VPSA循环。
在步骤(a)中,吸附塔1进行第一进料和吸附步骤。具体地,通过打开控制阀1a将氢气原料气从吸附塔1的底部引入吸附塔,以吸附大部分的杂质。同时,产品气控制阀1f打开,纯化后的氢气作为高纯氢气产品从吸附塔1顶部排出。
吸附塔4进行脱附步骤,脱附气产品通过打开的脱附控制阀4b由真空泵7从吸附塔4的底部抽出。吸附塔4内的压力降低到脱附压力,所述脱附压力由真空泵的功率决定。
吸附塔3和吸附塔5利用第一均压路径11进行第三均压步骤。具体地,吸附塔5通过打开的均压控制阀5c提供顺流气流,导致吸附塔5内的压力降低。吸附塔3通过打开的均压控制阀3c逆流接收气流,导致吸附塔3内的压力增加。第三均压步骤的总体结果是,在步骤(a)的开始阶段较高的吸附塔5内的压力和在步骤(a)的开始阶段较低的吸附塔3内的压力,在步骤(a)的结束阶段时达到相同水平。
吸附塔2和吸附塔6利用均压路径12进行第一均压步骤。具体地,吸附塔6通过打开的均压阀控制阀6d提供顺流气流,导致吸附塔6内的压力降低。吸附塔2通过打开的均压控制阀2d逆流接收气流,导致吸附塔2内的压力增加。第一均压步骤的总体结果是,在步骤(a)的开始阶段较高的吸附塔6内的压力和在步骤(a)的开始阶段较低的吸附塔2内的压力,在步骤(a)的结束阶段时达到相同水平。
步骤(b)中,吸附塔1进行第二进料和吸附步骤,与步骤(a)类似,通过打开原料气控制阀1a和产品气控制阀1f进行第二进料和吸附步骤。吸附塔2进行再加压步骤。通过打开再加压控制阀2e,将高纯氢气产品气从产品气缓冲罐通过再加压路径13引入到吸附塔2中。在步骤(b)的结束阶段时,吸附塔2内的压力增加到与原料气相同的水平。
吸附塔4进行吹扫步骤,而吸附塔5处于顺流提供吹扫步骤。具体地,在步骤(a)之后脱附气控制阀4b保持开启,以连续抽出吸附塔4内的脱附气体。同时,另一股来自吸附塔5的气流经过均压控制阀4c和第一均压路径11进入吸附塔4。打开均压控制阀5c,使吸附塔5内的气体流出,对吸附塔4进行吹扫。经过吸附塔4和5之间的这种相互作用,在步骤(b)的结束阶段时,吸附塔5内的压力降低到脱附压力以上的一个特定水平,同时吸附塔4内的压力保持在脱附压力。
吸附塔3和吸附塔6利用均压路径12进行第二均压步骤。具体地,吸附塔6通过打开的均压控制阀6d提供顺流气流,导致吸附塔6内的压力降低。吸附塔3通过打开的均压控制阀3d接收逆流气流,造成吸附塔2内的压力增加。第二均压步骤的总体结果是,在步骤(b)的开始阶段较高的吸附塔6内的压力和在步骤(b)的开始阶段较低的吸附塔3内的压力在步骤(b)的结束阶段时达到相同水平。
步骤(a)和步骤(b)包括所述VPSA循环的所有12个步骤:进料和吸附步骤、吸附和提供再加压步骤、第一均压步骤、第二均压步骤、第三均压步骤、脱附步骤、真空吹扫和提供吹扫步骤,尽管每一个步骤由不同的吸附塔进行。此后,步骤(a)和步骤(b)是基本“构造单元”,并可以通过切换吸附塔以执行每个单独的步骤来扩展产生整个VPSA循环。
比如,在步骤(c)和步骤(d)中,吸附塔1进行第一均压步骤和第二均压步骤,与步骤(a)和步骤(b)中的吸附塔6进行的步骤相同。在步骤(e)和步骤(f)中,吸附塔1进行第三均压步骤和顺流提供吹扫步骤,与在步骤(a)和步骤(b)中的吸附塔5进行的步骤相同。在步骤(g)和步骤(h)中,吸附塔1进行脱附步骤和吹扫步骤,与步骤(a)和步骤(b)中的吸附塔4进行的步骤相同。在步骤(i)和步骤(j)中,吸附塔1进行第三和第二均压步骤,与在步骤(a)和步骤(b)中的吸附塔3进行的步骤相同。在步骤(k)和步骤(l)中,吸附塔1进行第一均压步骤和再加压步骤,与在步骤(a)和步骤(b)中的吸附塔2进行的步骤相同。此后,吸附塔1可以再次重复步骤(a)和步骤(b)中的进料和吸附步骤以重新开始VPSA循环。吸附塔2至6与以与吸附塔1一样的方式运行,通过步骤(a)到步骤(l)的切换运行,完成一个完整的VPSA循环。
吸附工艺步骤的依序运行是通过有秩序地打开/关闭程序控制阀来控制的。为实现上述工艺,本实施方式中的程序控制阀可以通过自动控制和通讯系统进行远程或无线控制。作为本发明的一个优选实施方式,本发明的装置包括自动控制系统,例如带有通信模块的可编程逻辑控制器(PLC)或带有通信模块的分布式控制系统(DCS)。技术人员可以根据气体分离的需求,通过自动化的PLC/DCS控制系统,对本发明的装置进行远程/无线控制。
虽然以上对本发明的实施方式进行了说明,但本发明不限于该实施方式。在不脱离本发明的范围的情况下,可以以各种方式进一步改进本发明的用于生产超高纯氢气的特定VPSA工艺和装置。例如,上文描述了六个吸附塔,但是吸附塔的数量不限于六个。任意数量的吸附塔(不少于四个)加上匹配的VPSA循环可以执行与本发明相同的过程,并获得与本发明相同的优点,所述VPSA循环包括吸附步骤、多组均压步骤、吹扫步骤、脱附步骤、真空吹扫步骤和产品再加压步骤。
实施例
实施例1:
本实施例采用本发明的VPSA装置,将炼油厂SMR氢气PSA系统的纯氢气作为原料气,通过上述实施方式描述的方法进一步提纯为超高纯氢气。具体而言,氢气纯化在下述条件下进行。
[表1]
六个吸附塔为圆柱形,直径相同,均为0.8米。吸附剂填料段高度为3.0米,填料段下部填充椰壳活性炭1.5米,填料段上部填充5A沸石1.5米。来自纯化的炼油厂富氢尾气的纯氢气原料气含有99.3170 vol% 的氢气和各种副杂质。原料气体以3500 Nm3/hr的体积流速进入系统。吸附步骤中的吸附压力(最大压力)为3.0 MPa(绝对压力:后述各压力均适用),由真空泵实现的脱附压力为20 KPa.A。上述表1公开了运行条件和VPSA工艺的结果。
实施例2:
在该实施例中,来自乙烷重整过程的富氢尾气的原料气的氢气纯度为95.3601vol%。原料气通过前述实施方式中描述的方法进一步纯化为高纯度氢气。具体而言,氢气纯化在以下条件下进行。
[表2]
本实施例表明,当原料气具有较低的氢气纯度(约95 vol%)和较低的进料压力(1.2 MPa)时,本发明的工艺及装置可以生产超高纯氢气产品气(>99.997 vol%)。
本领域的技术人员将理解,在不脱离本发明的精神和范围的情况下,可以对具体实施方式和实施例进行许多变化和修改。
应当理解,如果本文引用任何现有技术出版物,则此类引用并不构成承认该出版物在澳大利亚或任何其他国家构成本领域公知常识的一部分。
Claims (8)
1.一种由通过多个吸附塔进行的逐步吸附和分离过程生产超高纯氢气的工艺,所述多个吸附塔装填有对至少一种更强可吸附性组分有选择性的吸附剂,在每一过程步骤中的所述多个吸附塔中的每个吸附塔以一种循环和协同的方式运行,所述工艺包括:
(a)真空变压吸附(VPSA)工艺,从一种低品级氢气原料气中生产超高纯氢气;
(b)生产的氢气的纯度大于99.997vol%,用于工业、医疗和氢能应用;
(c)超高纯氢气的产率大于85%,更优选地大于90%。
2.根据权利要求1的工艺,其特征在于,所述氢气原料气含有95.0vol%-99.9vol%的氢气和一种或多种杂质,一种典型的氢气原料气可以来自于甲烷蒸汽重整(SMR)氢气生产装置或类似的工艺系统,其中,所述氢气原料气含有氧气、氮气、一氧化碳、二氧化碳、甲烷和其他成分的杂质。
3. 根据权利要求1的工艺,其特征在于,所述氢气原料气的压力为1.2-3.0 MPa(或更高),温度为10-50℃。
4.根据权利要求1的工艺,其特征在于,所述工艺包括三个或更多的顺流减压步骤,形式为与其他吸附塔进行压力均衡;三个或更多的逆流加压步骤,形式为与其他吸附塔进行压力均衡;顺流提供吹扫步骤;以及一个真空吹扫脱附步骤。
5.权利要求1所述的工艺,其特征在于,VPSA是一种选择性地从至少一个更强可吸附性组分中分离氢气的真空变压吸附工艺,所述真空变压吸附工艺包括多个吸附塔,所述多个吸附塔中的每个吸附塔装填有吸附至少一种强可吸附性组分的吸附剂,虽然可以使用传统的变压吸附(PSA),但本发明的工艺特别包括:
(a)真空脱附步骤,步骤压降为ΔP1;
(b)提供脱附步骤,步骤压降为ΔP2;
(c)ΔP2/ΔP1 < 3,优选为1.0-2.5,更优选为1.0-1.5。
6.一种从含有氢气、氧气、氮气、一氧化碳、二氧化碳、甲烷和其他非强可吸附性杂质组分的氢气原料气中生产高纯氢气的工艺和装置,所述工艺包括以下VPSA步骤:
(a)进料和吸附步骤,将所述氢气原料气引入所述装置;
(b)进料、吸附和提供再加压步骤;
(c)第一均压减压步骤;
(d)第二均压减压步骤;
(e)第三均压减压步骤;
(f)提供吹扫步骤,以降低提供吹扫的吸附塔的压力;
(g)脱附步骤,以去除杂质;
(h)吹扫/真空吹扫步骤,以在所述脱附步骤后更深层次地清洗所述吸附塔并去除杂质;
(i)第三均压加压步骤;
(j)第二均压加压步骤;
(k)第一均压加压步骤;
(l)再加压步骤,将氢气原料气引入所述装置。
7. 权利要求6所述的工艺,其特征在于,所述吸附步骤的压力在表压1.2 MPa-3.0 MPa(或更高)的范围内。
8. 权利要求6所述的工艺,其特征在于,所述真空吹扫步骤的压力在10-50 kPa.A的范围内,在某些情况下,所述真空吹扫可以被非真空吹扫脱附处理所替代,而不会牺牲产品氢气的纯度和回收率。
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2020904141 | 2020-11-12 | ||
AU2020904141A AU2020904141A0 (en) | 2020-11-12 | A process and plant for producing high purity hydrogen from pure hydrogen gas | |
PCT/AU2021/051278 WO2022099350A1 (en) | 2020-11-12 | 2021-10-30 | A process and plant for producing ultrahigh-purity hydrogen from low-grade hydrogen gas |
Publications (1)
Publication Number | Publication Date |
---|---|
CN116390797A true CN116390797A (zh) | 2023-07-04 |
Family
ID=81600695
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN202180074382.0A Pending CN116390797A (zh) | 2020-11-12 | 2021-10-30 | 用于从低品级氢气生产超高纯氢气的工艺和设备 |
Country Status (3)
Country | Link |
---|---|
CN (1) | CN116390797A (zh) |
AU (1) | AU2021377152B2 (zh) |
WO (1) | WO2022099350A1 (zh) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN115259087B (zh) * | 2022-07-29 | 2023-09-05 | 广西柳州钢铁集团有限公司 | 一种创建预判机制提高氢气纯度的制氢操作方法及系统 |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4963339A (en) * | 1988-05-04 | 1990-10-16 | The Boc Group, Inc. | Hydrogen and carbon dioxide coproduction |
US7452407B2 (en) * | 2006-02-28 | 2008-11-18 | Air Products And Chemicals, Inc. | Production of carbon monoxide-free hydrogen and helium from a high-purity source |
CN108715436B (zh) * | 2018-05-29 | 2019-11-08 | 四川天采科技有限责任公司 | 半导体制程常压废氢气全温程变压吸附提纯再利用的方法 |
EP3733264A1 (en) * | 2019-05-02 | 2020-11-04 | Casale Sa | A pressure swing adsorption process for producing hydrogen and carbon dioxide |
-
2021
- 2021-10-30 WO PCT/AU2021/051278 patent/WO2022099350A1/en active Application Filing
- 2021-10-30 CN CN202180074382.0A patent/CN116390797A/zh active Pending
- 2021-10-30 AU AU2021377152A patent/AU2021377152B2/en active Active
Also Published As
Publication number | Publication date |
---|---|
AU2021377152B2 (en) | 2024-05-09 |
AU2021377152A1 (en) | 2023-06-08 |
WO2022099350A1 (en) | 2022-05-19 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US8298319B2 (en) | Pressure swing adsorption apparatus and method for hydrogen purification using the same | |
US6245127B1 (en) | Pressure swing adsorption process and apparatus | |
KR100254295B1 (ko) | 단일 흡착 베드를 이용한 압력 스윙 흡착 방법 | |
US8746009B2 (en) | Production of hydrogen from a reforming gas and simultaneous capture of CO2 co-product | |
EP0667178A1 (en) | VSA adsorption process with continuous operation | |
EP2080735A1 (en) | Hydrogen gas separation method and separation apparatus | |
NO144446B (no) | Adiabatisk trykkretsprosess for separasjon av gassblandinger | |
BRPI0618155A2 (pt) | processo e sistema de adsorção por oscilação de pressão no vácuo | |
JPH09239226A (ja) | 改良真空圧力スイング吸着プロセス | |
CN113350968A (zh) | 一种用于合成氢回收尾气成分的提氢装置及工艺 | |
CN110813022A (zh) | 多床快速循环动力学psa | |
CN211799895U (zh) | 一种分离含有氯化氢和氢气混合气体的工艺系统 | |
US20140069275A1 (en) | Low energy cyclic psa process | |
WO2017087167A1 (en) | Staged complementary psa system for low energy fractionation of mixed fluid | |
CN108236829B (zh) | 从含co2原料气中分离高纯度co2的方法及装置 | |
CN116390797A (zh) | 用于从低品级氢气生产超高纯氢气的工艺和设备 | |
WO2023064977A1 (en) | A process and plant of vacuum pressure swing adsorption for producing pure carbon dioxide from industrial off-gas containing co2 | |
AU2016201267B2 (en) | A plant and process for simutaneous recovering multiple gas products from petrochemical offgas | |
CN213101492U (zh) | 从石化排放尾气中同时回收氢气和甲烷气的装置 | |
CN113426245A (zh) | 基于变压吸附的高纯气体制备方法 | |
CN110550606A (zh) | 非稳态下由含氢气体制备高纯氢气的装置及方法 | |
JP4004435B2 (ja) | 圧力変動吸着装置による高純度ガスの製造方法 | |
KR20230106782A (ko) | 주 가스 및 불순물을 포함하는 원료 가스로부터 불순물의 효율적인 분리를 위한 psa 시스템, 및 이의 운전 방법 | |
KR820000517B1 (ko) | 고농축급속 압력순환식 흡착공정 | |
CN116272251A (zh) | 一种二塔串联变压吸附装置及其吸附工艺 |
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 |