CN108910824B - High-purity hydrogen purification system and purification method - Google Patents
High-purity hydrogen purification system and purification method Download PDFInfo
- Publication number
- CN108910824B CN108910824B CN201811081138.3A CN201811081138A CN108910824B CN 108910824 B CN108910824 B CN 108910824B CN 201811081138 A CN201811081138 A CN 201811081138A CN 108910824 B CN108910824 B CN 108910824B
- Authority
- CN
- China
- Prior art keywords
- adsorption tower
- pressure
- valve
- pipeline
- 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.)
- Active
Links
- 238000000746 purification Methods 0.000 title claims abstract description 71
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 239000001257 hydrogen Substances 0.000 title claims abstract description 60
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000001179 sorption measurement Methods 0.000 claims abstract description 511
- 239000007789 gas Substances 0.000 claims abstract description 273
- 238000007599 discharging Methods 0.000 claims abstract description 62
- 239000002994 raw material Substances 0.000 claims abstract description 55
- 238000000605 extraction Methods 0.000 claims abstract description 24
- 230000007704 transition Effects 0.000 claims description 123
- 238000011010 flushing procedure Methods 0.000 claims description 54
- 230000001105 regulatory effect Effects 0.000 claims description 37
- 239000012535 impurity Substances 0.000 claims description 18
- 238000013022 venting Methods 0.000 claims description 15
- 230000000630 rising effect Effects 0.000 claims description 9
- 238000010926 purge Methods 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 7
- 238000003795 desorption Methods 0.000 claims description 5
- 230000009467 reduction Effects 0.000 claims description 4
- 150000002431 hydrogen Chemical class 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 20
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 abstract description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 2
- 239000001569 carbon dioxide Substances 0.000 abstract description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 description 10
- 239000003463 adsorbent Substances 0.000 description 5
- 239000012530 fluid Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 230000008859 change Effects 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 239000000112 cooling gas Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
Classifications
-
- 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
-
- 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
-
- 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
- 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
- B01D2257/10—Single element gases other than halogens
- B01D2257/102—Nitrogen
-
- 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
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- 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
- B01D2257/00—Components to be removed
- B01D2257/80—Water
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses a high-purity hydrogen purification system and a purification method, wherein the system comprises a main PSA hydrogen extraction device and an auxiliary PSA hydrogen extraction device, the main PSA hydrogen extraction device comprises an adsorption unit A, a raw gas buffer tank A, a product gas buffer tank A, a forward-discharging gas tank, a reverse-discharging gas tank and an analysis gas tank, the auxiliary PSA hydrogen extraction device comprises an adsorption unit B, a raw gas buffer tank B, a product gas buffer tank B and a tail gas tank, the analysis gas tank is connected with the raw gas buffer tank B, and the raw gas buffer tank A is connected with the product gas buffer tank B. The tail gas of the main PSA hydrogen extracting device is compressed and used as the raw material gas of the auxiliary PSA hydrogen extracting device. The product gas of the auxiliary PSA hydrogen extraction device is used as the raw material gas of the main PSA hydrogen extraction device, so that the hydrogen yield is improved, substances such as carbon monoxide, carbon dioxide, methane, nitrogen, water vapor, nitrogen and the like in the crude hydrogen are effectively removed, and the product purity is improved.
Description
Technical Field
The invention relates to the field of hydrogen purification, in particular to a high-purity hydrogen purification system and a purification method.
Background
Hydrogen is a widely used raw material, is industrially used as raw material gas, reducing gas, cooling gas, protecting gas and combustion gas, and has wide application in the scientific research fields of chemical industry, petrochemical industry, metallurgy, mechanical processing, electric power, medicine and the like. The existing hydrogen purification equipment is generally prepared by adopting a PSA process, but the purity is not very high, and the yield is required to be improved.
Disclosure of Invention
The invention aims to provide a high-purity hydrogen purification system.
In order to achieve the above purpose, the invention adopts the following technical scheme: the high-purity hydrogen purification system comprises a main PSA hydrogen extraction device and an auxiliary PSA hydrogen extraction device, wherein the main PSA hydrogen extraction device comprises an adsorption unit A, a raw material gas buffer tank A, a product gas buffer tank A, a forward-air discharge tank, a reverse-air discharge tank and an analysis tank, the auxiliary PSA hydrogen extraction device comprises an adsorption unit B, a raw material gas buffer tank B, a product gas buffer tank B and a tail gas tank,
the adsorption unit A comprises four adsorption towers A, wherein the bottom and the top of each adsorption tower A are respectively connected with a bottom pipeline A and a top pipeline A, different positions of the bottom pipeline A are respectively connected with a raw gas inlet valve A, a reverse discharge valve A and a blow-down valve A, and different positions of the top pipeline A are respectively connected with a product outlet valve A, a final pressure-increasing/primary pressure-equalizing valve A, a forward discharge/secondary pressure-equalizing valve A and a flushing valve A;
the raw material gas buffer tank A is connected with a raw material gas input pipeline A and a raw material gas output pipeline A, the raw material gas output pipeline A is connected with a first transition pipeline, and different positions of the first transition pipeline are respectively connected with four raw material gas inlet valves A;
The product gas buffer tank A is connected with a product gas input pipeline A and a product gas output pipeline A, the product gas input pipeline A is connected with a product inlet valve A, the product inlet valve A is connected with a second transition pipeline, different positions of the second transition pipeline are respectively connected with four product outlet valves A and a third transition pipeline, and different positions of the third transition pipeline are respectively connected with four final pressure boosting/primary pressure equalizing valves A;
the forward-air discharge tank is respectively connected with a forward-air discharge input pipeline and a forward-air discharge output pipeline, the forward-air discharge input pipeline is connected with a forward-air discharge inlet valve, the forward-air discharge inlet valve is connected with a fourth transition pipeline, different positions of the fourth transition pipeline are respectively connected with four forward-air discharge/secondary pressure equalizing valves A, the forward-air discharge output pipeline is connected with a fifth transition pipeline, and different positions of the fifth transition pipeline are respectively connected with four flushing valves A;
the reverse deflation tank is connected with a reverse deflation input pipeline and a reverse deflation output pipeline, the reverse deflation input pipeline is connected with a sixth transition pipeline, different positions of the sixth transition pipeline are respectively connected with four reverse deflation valves A and a reverse deflation auxiliary valve, and the reverse deflation auxiliary valve is connected with a seventh transition pipeline;
The analytic gas tank is connected with an analytic gas input pipeline and an analytic gas output pipeline, and the analytic gas input pipeline is connected with the seventh transition pipeline;
the adsorption unit B comprises four adsorption towers B, the bottom and the top of each adsorption tower B are respectively connected with a bottom pipeline B and a top pipeline B, different positions of the bottom pipeline B are respectively connected with a raw gas inlet valve B, a reverse discharge valve B and a blow-down valve B, and different positions of the top pipeline B are respectively connected with a product outlet valve B, a final pressure-increasing/primary pressure-equalizing valve B, a forward discharge/secondary pressure-equalizing valve B and a flushing valve B;
the raw material gas buffer tank B is connected with a raw material gas input pipeline B and a raw material gas output pipeline B, the raw material gas output pipeline B is connected with an eighth transition pipeline, and different positions of the eighth transition pipeline are respectively connected with four raw material gas inlet valves B;
the product gas buffer tank B is connected with a product gas input pipeline B and a product gas output pipeline B, the product gas input pipeline B is connected with a product inlet valve B, the product inlet valve B is connected with a ninth transition pipeline, different positions of the ninth transition pipeline are respectively connected with four product outlet valves B and a tenth transition pipeline, and different positions of the tenth transition pipeline are respectively connected with four final boosting/primary equalizing valves B;
The four forward/secondary equalizing valves B are respectively connected with different positions of an eleventh transition pipeline;
the four flushing valves B are respectively connected with different positions of a twelfth transition pipeline;
the four reverse discharge valves B are respectively connected with different positions of a thirteenth transition pipeline;
the tail gas tank is connected with a tail gas input pipeline and a tail gas output pipeline, and the tail gas input pipeline is connected with a thirteenth transition pipeline;
the four emptying valves A are respectively connected with different positions of a fourteenth transition pipeline;
the four emptying valves B are respectively connected with different positions of a fifteenth transition pipeline;
the analysis gas output pipeline is connected with the raw material gas input pipeline B;
the raw material gas input pipeline A is connected with the product gas output pipeline B.
In the above technical scheme, the product gas output pipeline A is connected with a system pressure regulating valve A.
In the above technical scheme, the second transition pipeline is connected with the third transition pipeline through the final stamping force regulating valve.
In the technical scheme, the forward-discharge gas output pipeline is connected with the fifth transition pipeline through the forward-discharge pressure regulating valve.
In the technical scheme, the reverse deflation output pipeline is connected with a reverse deflation pressure regulating valve, and the analysis gas output pipeline is connected with an analysis gas pressure regulating valve.
In the above technical scheme, the product gas output pipeline B is connected with a system pressure regulating valve B.
In the above technical scheme, the ninth transition pipeline is connected with the tenth transition pipeline through a final flushing flow regulating valve.
In the above technical scheme, a forward flow regulating valve is further arranged between each forward/secondary equalizing valve B and the eleventh transition pipeline.
In the above technical scheme, the tail gas output pipeline is connected with a tail gas pressure regulating valve.
The invention also provides another technical scheme: a high-purity hydrogen purification method adopts the purification device, the purification method comprises a main purification procedure and an auxiliary purification procedure, the main purification procedure comprises four main purification procedures, the auxiliary purification procedure comprises four auxiliary purification procedures,
each main purification process comprises the following steps:
the method comprises the steps of (1.1) an adsorption step, namely opening a feed gas inlet valve A and a product outlet valve A of a first adsorption tower A, enabling feed gas to enter the first adsorption tower A from bottom to top after being subjected to water-gas separation through a feed gas buffer tank A, adsorbing impurity components under working pressure, enabling non-adsorbed product components to flow out through the product outlet valve A of the first adsorption tower A, enabling most of the non-adsorbed product components to enter the product gas buffer tank A as products, enabling the rest of the non-adsorbed product components to enter a second adsorption tower A from top to bottom through a final stamping force regulating valve and a sequential/secondary pressure equalizing valve A for final pressurization, and closing the feed gas inlet valve A and the product outlet valve A of the first adsorption tower A after the adsorption step of the first adsorption tower A is finished;
(1.2) a first uniform pressure reducing step of opening a final pressure increasing/equalizing valve A of the first adsorption tower A, opening a final pressure increasing/equalizing valve A of the third adsorption tower A which just ends the second uniform pressure increasing step, performing first-stage pressure balance on the first adsorption tower A and the third adsorption tower A, reducing the pressure of the first adsorption tower A until the pressure of the first adsorption tower A and the pressure of the third adsorption tower A are basically equal, and closing the final pressure increasing/equalizing valve A of the first adsorption tower A and the final pressure increasing/equalizing valve A of the third adsorption tower A after the first uniform pressure reducing step of the first adsorption tower A is ended;
(1.3) a second uniform pressure reducing step, namely opening a forward/secondary pressure equalizing valve A of the first adsorption tower A, opening a forward/secondary pressure equalizing valve A of the fourth adsorption tower A, enabling residual gas in the first adsorption tower A to enter the fourth adsorption tower A from top to bottom, performing second-stage pressure balance on the first adsorption tower A and the fourth adsorption tower A, and further reducing the pressure of the first adsorption tower A until the pressure of the first adsorption tower A is basically equal to the pressure of the fourth adsorption tower A, and closing the forward/secondary pressure equalizing valve A of the fourth adsorption tower A after the second uniform pressure reducing step of the first adsorption tower A is finished;
(1.4) a forward discharging step of opening a forward discharging inlet valve of the forward discharging tank, enabling residual gas in the first adsorption tower A to enter the forward discharging tank through a forward discharging/secondary equalizing valve A and the forward discharging inlet valve of the forward discharging inlet valve, stopping forward discharging after the pressure in the first adsorption tower A is reduced to a specified value, and closing the forward discharging/secondary equalizing valve A and the forward discharging inlet valve of the first adsorption tower A after the forward discharging step of the first adsorption tower A is finished;
(1.5) a reverse discharge step of sequentially opening a reverse discharge valve A and a reverse discharge auxiliary valve of the first adsorption tower A, sequentially discharging the residual gas in the first adsorption tower A to a reverse discharge tank and a desorption gas tank until the pressure in the first adsorption tower A is reduced to normal pressure or nearly 0.02MPa (G), and closing the reverse discharge valve A of the first adsorption tower A after the reverse discharge step of the first adsorption tower A is finished;
(1.6) a flushing step of opening a flushing valve A and a venting valve A of the first adsorption tower A, flushing the bed layer of the first adsorption tower A from top to bottom by the forward-venting gas in the forward-venting gas tank to further desorb impurities in the tower, venting the analysis gas through the venting valve A, and closing the flushing valve A, the venting valve A and the reverse-venting auxiliary valve of the first adsorption tower A after the flushing step of the first adsorption tower A is finished;
(1.7) a second equalizing step of opening the forward/equalizing valve A of the first adsorption tower A and the forward/equalizing valve A of the third adsorption tower A, wherein the first adsorption tower A is communicated with the third adsorption tower A which just ends the first equalizing step, the first adsorption tower A and the third adsorption tower A perform second-stage pressure equalization, the pressure of the first adsorption tower A is increased until the pressure of the first adsorption tower A and the pressure of the third adsorption tower A are basically equal, and after the second equalizing step of the first adsorption tower A is ended, the opened forward/equalizing valve A of the first adsorption tower A and the opened forward/equalizing valve A of the third adsorption tower A are closed;
(1.8) a step of uniform pressure rise, namely opening a final pressure rising/primary pressure equalizing valve A of a first adsorption tower A and a final pressure rising/primary pressure equalizing valve A of a fourth adsorption tower A, wherein the first adsorption tower A is communicated with the fourth adsorption tower A which just finishes the adsorption step, the first adsorption tower A and the fourth adsorption tower A perform first-stage pressure balance, and the pressure of the first adsorption tower A is further raised until the pressure of the first adsorption tower A and the pressure of the fourth adsorption tower A are basically equal;
(1.9) a final pressure increasing step of continuing to open the final pressure increasing/primary pressure equalizing valve A of the first adsorption tower A and the final pressure increasing/primary pressure equalizing valve A of the fourth adsorption tower A, wherein the product gas of the fourth adsorption tower A enters the first adsorption tower A, the final pressure increasing of the first adsorption tower A is carried out until the pressure of the first adsorption tower A is basically close to the adsorption pressure, and the step (1.1) is returned after the final pressure increasing step of the first adsorption tower A is finished;
the four adsorption towers A are respectively used as the first adsorption towers A of the four main purification processes, the first, the second, the third and the fourth adsorption towers A of any two main purification processes are different, and the same steps of any two main purification processes are carried out at different times;
Each auxiliary purification process comprises the following steps:
(2.1) an adsorption step of opening a feed gas inlet valve B and a product outlet valve B of a first adsorption tower B, enabling feed gas to enter the first adsorption tower B from bottom to top after being subjected to water-gas separation through the feed gas buffer tank B, adsorbing impurity components under working pressure, enabling non-adsorbed product components to flow out through the product outlet valve B of the first adsorption tower B, enabling most of the non-adsorbed product components to enter the product gas buffer tank B as products, enabling the rest of the non-adsorbed product components to enter a second adsorption tower B from top to bottom through a final flushing flow regulating valve and a sequential/secondary equalizing valve B for final pressure increase, and closing the feed gas inlet valve B and the product outlet valve B of the first adsorption tower B after the adsorption step of the first adsorption tower B is finished;
(2.2) a step of uniform pressure reduction, namely opening a final pressure increasing/primary pressure equalizing valve B of the first adsorption tower B, opening a final pressure increasing/primary pressure equalizing valve B of the third adsorption tower B which just finishes the step of uniform pressure increase, performing first-stage pressure balance on the first adsorption tower B and the third adsorption tower B, reducing the pressure of the first adsorption tower B until the pressure of the first adsorption tower B and the pressure of the third adsorption tower B are basically equal, and closing a final pressure increasing/primary pressure equalizing valve A of the first adsorption tower B and a final pressure increasing/primary pressure equalizing valve B of the third adsorption tower B after the step of uniform pressure reduction of the first adsorption tower B is finished;
(2.3) a forward discharging step, namely opening a forward discharging/secondary equalizing valve B of the first adsorption tower B, opening a reverse discharging valve B of the fourth adsorption tower B, flushing the fourth adsorption tower B which just finishes reverse discharging by residual gas in the first adsorption tower B until the pressure of the first adsorption tower B is reduced to a specified value, finishing the forward discharging step of the first adsorption tower B, and closing the reverse discharging valve B of the fourth adsorption tower B;
(2.4) continuing to open the forward/secondary equalizing valve B of the first adsorption tower B, opening the forward/secondary equalizing valve B of the fourth adsorption tower B, enabling residual gas in the first adsorption tower B to enter the fourth adsorption tower B from top to bottom, performing second-stage pressure balance on the first adsorption tower B and the fourth adsorption tower B, and further reducing the pressure of the first adsorption tower B until the pressure of the first adsorption tower B is basically equal to the pressure of the fourth adsorption tower B, and closing the forward/secondary equalizing valve B of the fourth adsorption tower B after the second equalizing step of the first adsorption tower B is finished;
(2.5) a reverse discharge step, namely continuously opening a reverse discharge valve B of a fourth adsorption tower B, discharging the residual gas in the first adsorption tower B to a tail gas tank until the pressure in the first adsorption tower B is lower than the pressure of the tail gas tank, and opening a discharge valve B to discharge until the pressure in the first adsorption tower B is reduced to approximately 0.02MPa (G), wherein the reverse discharge step of the first adsorption tower B is finished;
(2.6) a flushing step of flushing the bed layer of the first adsorption tower B from top to bottom by opening a flushing valve B of the first adsorption tower B and a forward/secondary equalizing valve B of the second adsorption tower B, flushing impurities still remained in the first adsorption tower B, further desorbing the impurities in the first adsorption tower B, exhausting the analysis gas through an exhaust valve B of the first adsorption tower B, and closing the flushing valve B of the first adsorption tower B, the forward/secondary equalizing valve B of the second adsorption tower B and the exhaust valve B after the flushing step of the first adsorption tower B is finished;
(2.7) a second uniform pressure step, namely opening the forward/uniform pressure valve B of the first adsorption tower B and the forward/uniform pressure valve B of the second adsorption tower B, wherein the first adsorption tower B is communicated with the second adsorption tower B which just finishes the first uniform pressure step, the first adsorption tower B and the second adsorption tower B perform second-stage pressure balance, the pressure of the first adsorption tower B is increased until the pressure of the first adsorption tower B is basically equal to the pressure of the second adsorption tower B, and after the second uniform pressure step of the first adsorption tower B is finished, closing the opened forward/uniform pressure valve B of the first adsorption tower B and the opened forward/uniform pressure valve B of the second adsorption tower B;
(2.8) a step of uniform pressure rise, namely opening a final pressure rising/primary pressure equalizing valve B of the first adsorption tower B and a final pressure rising/primary pressure equalizing valve B of the third adsorption tower B, wherein the first adsorption tower B is communicated with the third adsorption tower B which just finishes the adsorption step, the first adsorption tower B and the third adsorption tower B perform first-stage pressure balance, and the pressure of the first adsorption tower B is further raised until the pressure of the first adsorption tower B and the pressure of the third adsorption tower B are basically equal;
(2.9) a final pressure increasing step of continuing to open the final pressure increasing/primary pressure equalizing valve B of the first adsorption tower B and the final pressure increasing/primary pressure equalizing valve B of the third adsorption tower B, enabling the product gas of the third adsorption tower B to enter the first adsorption tower B, and returning to the step (2.1) after the final pressure increasing step of the first adsorption tower B is finished until the pressure of the first adsorption tower B is basically close to the adsorption pressure;
the four adsorption towers B are respectively used as the first adsorption towers B of the four auxiliary purification processes, the first adsorption tower A, the second adsorption tower B, the third adsorption tower A and the fourth adsorption tower A of any two auxiliary purification processes are different, and the same steps of any two auxiliary purification processes are carried out at different times.
Due to the application of the technical scheme, the invention has the following advantages: the invention discloses a high-purity hydrogen purification system and a purification method, wherein hydrogen extraction tail gas of a main PSA hydrogen extraction device is compressed to be used as raw material gas of an auxiliary PSA hydrogen extraction device, output gas of the auxiliary device is used as raw material gas of the main PSA hydrogen extraction device, the auxiliary PSA hydrogen extraction device is used for purifying tail gas of the main PSA hydrogen extraction device, the hydrogen yield is improved, and substances such as carbon monoxide, carbon dioxide, methane, nitrogen, water vapor, nitrogen and the like in crude hydrogen are effectively removed by adopting a PSA process, so that the hydrogen purity is improved.
Drawings
FIG. 1 is a schematic illustration of a primary PSA hydrogen-stripping apparatus of the present disclosure;
fig. 2 is a schematic diagram of an auxiliary PSA hydrogen-extracting apparatus of the present disclosure.
110, a raw material gas buffer tank A; 111. a raw material gas input pipeline A; 112. a raw material gas output pipeline A; 113. a first transition line; 120. a product gas buffer tank A; 121. a product gas input line; 122. a product gas output line; 123. a second transition line; 124. a third transition line; 130. c, smoothly discharging the gas tank; 131. a forward-air-discharging input pipeline; 132. a forward-air discharge pipeline; 133. a fourth transition line; 134. a fifth transition line; 140. reversely discharging the air tank; 141. a reverse air discharge input pipeline; 142. a reverse bleed air output pipeline; 143. a sixth transition line; 144. a seventh transition line; 150. analyzing a gas tank; 151. a resolving gas input pipeline; 152. a desorption gas output pipeline; 160. an adsorption tower A; 1601. a bottom pipeline A; 1602. a top pipeline A; 1603. a feed gas inlet valve; 1604. a reverse discharge valve; 1605. an emptying valve A; 1606. a product outlet valve a; 1607. a final pressure boosting/primary equalizing valve A; 1608. a forward/secondary equalizing valve A; 1609. a flushing valve A; 1610. a product inlet valve; 1611. a forward-bleed air inlet valve; 1612. a reverse-discharge auxiliary valve; 1613. a system pressure regulating valve A; 1614. a final ram pressure regulating valve; 1615. a forward pressure regulating valve; 1616. a reverse discharge pressure regulating valve; 1617. analyzing the air pressure regulating valve; 1618. purging the replacement valve A; 1619. a heating valve A;
171. A fourteenth transition line; 172. a sixteenth transition duct; 173. a seventeenth transition duct;
210. a raw material gas buffer tank B; 211. a raw material gas input pipeline B; 212. a raw material gas output pipeline B; 213. an eighth transition line; 220. a product gas buffer tank B; 221. a product gas input line; 222. a product gas output line; 223. a ninth transition line; 224. a tenth transition line; 230. a tail gas tank; 231. a tail gas input pipeline; 232. a tail gas output pipeline; 240. an adsorption tower B; 2401. a bottom pipeline B; 2402. a top pipeline B; 2403. a feed gas inlet valve; 2404. a reverse discharge valve; 2405. a blow-off valve B; 2406. a product outlet valve B; 2407. a final pressure boosting/primary equalizing valve B; 2408. a forward/secondary equalizing valve B; 2409. a flushing valve B; 2410. a product inlet valve; 2411. a system pressure regulating valve B; 2412. a final impulse flow regulating valve; 2413. a forward discharge flow regulating valve; 2414. a tail gas pressure regulating valve; 2415. purging and replacing B; 2416. a heating valve B;
251. an eleventh transition line; 252. a twelfth transition duct; 253. a thirteenth transition duct; 254. a fifteenth transition duct; 255. an eighteenth transition line; 256. nineteenth transition duct.
Detailed Description
The invention will be further described with reference to the accompanying drawings and examples:
referring to fig. 1 and 2, as illustrated therein, a high purity hydrogen purification system includes a main PSA hydrogen-extracting apparatus including an adsorption unit a, a raw gas buffer tank a110, a product gas buffer tank a120, a co-bleed gas tank 130, a reverse bleed gas tank 140, and a desorption gas tank 150, and an auxiliary PSA hydrogen-extracting apparatus including an adsorption unit B, a raw gas buffer tank B210, a product gas buffer tank B220, and a tail gas tank 230,
the adsorption unit A comprises four adsorption towers A160, wherein the bottom and the top of each adsorption tower A160 are respectively connected with a bottom pipeline A1601 and a top pipeline A1602, different positions of the bottom pipeline A1601 are respectively connected with a raw gas inlet valve A1603, a reverse discharge valve A1604 and a discharge valve A1605, and different positions of the top pipeline A1602 are respectively connected with a product outlet valve A1606, a final pressure-increasing/primary pressure-equalizing valve A1607, a forward discharge/secondary pressure-equalizing valve A1608 and a flushing valve A1609;
the raw material gas buffer tank A110 is connected with a raw material gas input pipeline A111 and a raw material gas output pipeline A112, the raw material gas output pipeline A112 is connected with a first transition pipeline 113, and different positions of the first transition pipeline 113 are respectively connected with four raw material gas inlet valves A1603;
The product gas buffer tank A120 is connected with a product gas input pipeline A121 and a product gas output pipeline A122, the product gas input pipeline A121 is connected with a product inlet valve A1610, the product inlet valve A123 is connected with a second transition pipeline 123, different positions of the second transition pipeline 123 are respectively connected with four product outlet valves A1606 and a third transition pipeline 124, and different positions of the third transition pipeline 124 are respectively connected with four final pressure boosting/primary pressure equalizing valves A1607;
the forward-air tank 130 is respectively connected with a forward-air input pipeline 131 and a forward-air output pipeline 132, the forward-air input pipeline 131 is connected with a forward-air inlet valve 1611, the forward-air inlet valve 1611 is connected with a fourth transition pipeline 133, different positions of the fourth transition pipeline 133 are respectively connected with four forward-air/secondary equalizing valves A1608, the forward-air output pipeline 132 is connected with a fifth transition pipeline 134, and different positions of the fifth transition pipeline 134 are respectively connected with four flushing valves A1609;
the reverse air discharge tank 140 is connected with a reverse air discharge input pipeline 141 and a reverse air discharge output pipeline 142, the reverse air discharge input pipeline 141 is connected with a sixth transition pipeline 143, different positions of the sixth transition pipeline 143 are respectively connected with four reverse air discharge valves A1604 and a reverse air discharge auxiliary valve 1612, and the reverse air discharge auxiliary valve 1612 is connected with a seventh transition pipeline 144;
The analysis gas tank 150 is connected with an analysis gas input pipeline 151 and an analysis gas output pipeline 152, and the analysis gas input pipeline 151 is connected with a seventh transition pipeline 144;
the adsorption unit B comprises four adsorption towers B240, wherein the bottom and the top of each adsorption tower B240 are respectively connected with a bottom pipeline B2401 and a top pipeline B2402, different positions of the bottom pipeline B2401 are respectively connected with a raw gas inlet valve B2403, a reverse discharge valve B2404 and a discharge valve B2405, and different positions of the top pipeline B2402 are respectively connected with a product outlet valve B2406, a final pressure-increasing/primary pressure-equalizing valve B2407, a forward discharge/secondary pressure-equalizing valve B2408 and a flushing valve B2409;
the raw material gas buffer tank B210 is connected with a raw material gas input pipeline B211 and a raw material gas output pipeline B212, the raw material gas output pipeline B212 is connected with an eighth transition pipeline 213, and different positions of the eighth transition pipeline 213 are respectively connected with four raw material gas inlet valves B2403;
the product gas buffer tank B220 is connected with a product gas input pipeline B221 and a product gas output pipeline B222, the product gas input pipeline B221 is connected with a product inlet valve B2410, the product inlet valve B2410 is connected with a ninth transition pipeline 223, different positions of the ninth transition pipeline 223 are respectively connected with four product outlet valves B2406 and a tenth transition pipeline 224, and different positions of the tenth transition pipeline 224 are respectively connected with four final pressure boosting/primary pressure equalizing valves B2407;
Four forward/secondary equalizing valves B2408 are respectively connected with different positions of an eleventh transition pipeline 251;
the four flushing valves B2409 are respectively connected with different positions of a twelfth transition pipeline 252;
the four reverse discharge valves B2404 are respectively connected with different positions of a thirteenth transition pipeline 253;
the tail gas tank 230 is connected with a tail gas input pipeline 231 and a tail gas output pipeline 232, and the tail gas input pipeline 231 is connected with a thirteenth transition pipeline 254;
the four vent valves A1605 are respectively connected with different positions of a fourteenth transition pipeline 171;
the four blow-off valves B2405 are respectively connected with different positions of a fifteenth transition pipeline 254;
the analysis gas output pipeline 152 is connected with a raw material gas input pipeline B211;
the raw gas input line a111 is connected to the product gas output line B222.
In the preferred embodiment of this example, feed gas inlet valve A1603, reverse vent valve A1604, vent valve A1605, product outlet valve A1606, final boost/primary pressure equalizing valve A1607, forward vent/secondary pressure equalizing valve A1608, flush valve A1609, product inlet valve A1610, forward vent inlet valve 1611, reverse vent auxiliary valve 1612, feed gas inlet valve B2403, reverse vent valve B2404, vent valve B2405, product outlet valve B2406, final boost/primary pressure equalizing valve B2407, forward vent/secondary pressure equalizing valve B2408, flush valve B2409, and product inlet valve B2410 are all programmable valves.
In the preferred embodiment of this embodiment, the product gas output line A212 is connected to a system pressure regulating valve A1613, and the system pressure regulating valve A1613 is an automatic regulating valve.
In the preferred embodiment of the present example, the second transition line 123 is connected to the third transition line 124 via a final ram pressure regulator valve 1614, the final ram pressure regulator valve 1614 being a manual valve.
In the preferred embodiment of the present embodiment, the bleed air output line 132 is connected to the fifth transition line 134 via a bleed air pressure regulator valve 1615, the bleed air pressure regulator valve 1615 being an automatic regulator valve.
In the preferred embodiment of this example, the reverse bleed air output line 142 is connected to a reverse bleed pressure regulator valve 1616, and the reverse bleed pressure regulator valve 1616 is a manual valve.
In the preferred embodiment of the present embodiment, the analysis gas output line 152 is connected to an analysis gas pressure regulating valve 1617, and the analysis gas pressure regulating valve 1617 is an automatic regulating valve.
In the preferred embodiment of the present invention, the top pipeline a1602 is further connected to a purge and replace valve a1618, and the four purge and replace valves a1618 are respectively connected to different positions of a sixteenth transition pipeline 172, and the sixteenth transition pipeline 172 is connected in parallel to a nitrogen inlet valve a (not shown) and a hydrogen inlet valve a (not shown), wherein the nitrogen inlet valve a is connected to a nitrogen source a (not shown), and the hydrogen inlet valve a is connected to a hydrogen source a (not shown).
In the preferred embodiment of the present invention, the top pipeline a1602 is further connected to a heating valve a1619, and the four heating valves a1619 are respectively connected to different positions of a seventeenth transition pipeline 173, where the seventeenth transition pipeline 173 is connected to a heating fluid source a (not shown), and the heating fluid source a is a hot water source or a hot steam source.
In the preferred embodiment of this embodiment, the product gas output line B222 is connected to a system pressure regulating valve B2411, and the system pressure regulating valve B2411 is an automatic regulating valve.
In the preferred embodiment of the present embodiment, the ninth transition pipe 223 is connected to the tenth transition pipe 224 through a final-impulse-flow-adjusting valve 2412, and the final-impulse-flow-adjusting valve 2412 is a manual valve.
In the preferred embodiment of this embodiment, a forward flow rate adjusting valve 2413 is further disposed between each forward/secondary equalizing valve B2408 and the eleventh transition pipe 251, and the forward flow rate adjusting valve 2413 is a manual valve.
In the preferred embodiment of the present embodiment, the exhaust gas output line 132 is connected to an exhaust gas pressure adjusting valve 2414, and the exhaust gas pressure adjusting valve 2414 is an automatic adjusting valve.
In the preferred embodiment of this example, the top pipeline B2402 is further connected with purge and replace valves B2415, and the four purge and replace valves B2415 are respectively connected to different positions of an eighteenth transition pipeline 255, and the eighteenth transition pipeline 255 is connected in parallel with a nitrogen inlet valve B (not shown) and a hydrogen inlet valve B (not shown), wherein the nitrogen inlet valve B is connected to a nitrogen source B (not shown), and the hydrogen inlet valve B is connected to a hydrogen source B (not shown).
In the preferred embodiment of this embodiment, the top pipeline B2402 is further connected with a heating valve B2416, and four heating valves B2416 are respectively connected to different positions of a nineteenth transition pipeline 256, and the nineteenth transition pipeline 256 is connected to a heating fluid source B (not shown), where the heating fluid source B is a hot water source or a hot steam source
The following describes a purification method of high purity hydrogen gas, employing the purification apparatus as above, comprising a main purification process comprising four main purification processes and an auxiliary purification process comprising four auxiliary purification processes,
each main purification process comprises the following steps:
(1.1) an adsorption step of opening a feed gas inlet valve A1603 and a product outlet valve A1606 of a first adsorption column A160, allowing feed gas to enter the first adsorption column A160 from bottom to top after being subjected to water-gas separation by a feed gas buffer tank A110, adsorbing impurity components under working pressure, allowing non-adsorbed product components to flow out through the product outlet valve A1606 of the first adsorption column A160, wherein most of the non-adsorbed product components enter the product gas buffer tank A120 as a product, allowing the rest of the non-adsorbed product components to enter a second adsorption column A160 from top to bottom by a final pressure regulating valve 1614 and a sequential/secondary pressure equalizing valve A1608 for final pressure boosting, and closing the feed gas inlet valve A1603 and the product outlet valve A1606 of the first adsorption column A160 after the adsorption step of the first adsorption column A160 is finished;
(1.2) a first equalization step of opening the final pressure-increasing/primary pressure-equalizing valve a1607 of the first adsorption column a160, opening the final pressure-increasing/primary pressure-equalizing valve a1607 of the third adsorption column a160 immediately after the second equalization step, performing first-stage pressure equalization on the first adsorption column a160 and the third adsorption column a160, and reducing the pressure of the first adsorption column a160 until the pressures of the first adsorption column a160 and the third adsorption column a160 are substantially equal, and closing the final pressure-increasing/primary pressure-equalizing valve a1607 of the first adsorption column a160 and the final pressure-increasing/primary pressure-equalizing valve a1607 of the third adsorption column a160 after the first equalization step of the first adsorption column a160 is completed;
(1.3) a second uniform pressure reducing step of opening the forward/secondary pressure equalizing valve A1608 of the first adsorption tower A1607, opening the forward/secondary pressure equalizing valve A1608 of the fourth adsorption tower A160, enabling the residual gas in the first adsorption tower A160 to enter the fourth adsorption tower A160 from top to bottom, performing second-stage pressure balance on the first adsorption tower A160 and the fourth adsorption tower A160, further reducing the pressure of the first adsorption tower A160 until the pressure of the first adsorption tower A160 and the fourth adsorption tower A160 is basically equal, and closing the forward/secondary pressure equalizing valve A1608 of the fourth adsorption tower A160 after the second uniform pressure reducing step of the first adsorption tower A160 is finished;
(1.4) a forward discharging step of opening the forward discharging inlet valve 1611 of the forward discharging tank 130, allowing the residual gas in the first adsorption tower a160 to enter the forward discharging tank 130 through the forward discharging/secondary equalizing valve a1608 and the forward discharging inlet valve 1611 thereof, stopping the forward discharging after the pressure in the first adsorption tower a160 is reduced to a predetermined value, and closing the forward discharging/secondary equalizing valve a1608 and the forward discharging inlet valve 1611 of the first adsorption tower a160 after the forward discharging step of the first adsorption tower a160 is completed;
(1.5) a reverse discharge step of sequentially opening a reverse discharge valve a1604 and a reverse discharge auxiliary valve 1612 of the first adsorption tower a160, sequentially discharging the remaining gas in the first adsorption tower a160 to the reverse discharge gas tank 140 and the analysis gas tank 150 until the pressure in the first adsorption tower a160 drops to normal pressure or near 0.02MPa (G), and closing the reverse discharge valve a1604 of the first adsorption tower a160 after the reverse discharge step of the first adsorption tower a160 is completed;
(1.6) a flushing step of opening a flushing valve A1609 and a vent valve A1605 of the first adsorption tower A160, flushing the bed layer of the first adsorption tower A160 from top to bottom by the forward-bleed air in the forward-bleed air tank 130 while impurities remained in the first adsorption tower A160, further desorbing the impurities in the tower, and venting the desorption air through the vent valve A1605, and closing the flushing valve A1609, the vent valve A1605 and the reverse-vent auxiliary valve 1612 of the first adsorption tower A160 after the flushing step of the first adsorption tower A160 is finished;
(1.7) a second equalization step of opening the forward/equalization valve a1608 of the first adsorption tower a160 and the forward/equalization valve a1608 of the third adsorption tower a160, the first adsorption tower a160 being connected to the third adsorption tower a160 immediately after the first equalization step, the first adsorption tower a160 being subjected to a second-stage pressure equalization with the third adsorption tower a160, the first adsorption tower a160 being subjected to a pressure equalization until the pressure of the first adsorption tower a160 is substantially equal to the pressure of the third adsorption tower a160, and closing the opened forward/equalization valve a1608 of the first adsorption tower a160 and the forward/equalization valve a1608 of the third adsorption tower a160 after the second equalization step of the first adsorption tower a160 is completed;
(1.8) a step of equalizing the pressure, namely opening a final pressure-increasing/primary pressure-equalizing valve A1607 of the first adsorption tower A160 and a final pressure-increasing/primary pressure-equalizing valve A1607 of the fourth adsorption tower A160, wherein the first adsorption tower A160 is communicated with the fourth adsorption tower A160 of which the adsorption step is just finished, the first adsorption tower A160 and the fourth adsorption tower A160 perform first-stage pressure equalization, and the pressure of the first adsorption tower A160 is further increased until the pressures of the first adsorption tower A160 and the fourth adsorption tower A160 are basically equal;
(1.9) a final pressure increasing step of continuing to open the final pressure increasing/primary pressure equalizing valve a1607 of the first adsorption column a160 and the final pressure increasing/primary pressure equalizing valve a1607 of the fourth adsorption column a160, and allowing the product gas of the fourth adsorption column a160 to enter the first adsorption column a160, wherein the final pressure increasing of the first adsorption column a160 is performed until the pressure of the first adsorption column a160 is substantially close to the adsorption pressure, and returning to the step (1.1) after the final pressure increasing step of the first adsorption column a160 is completed;
The four adsorption towers A are respectively used as the first adsorption towers A of the four main purification processes, the first, the second, the third and the fourth adsorption towers A of any two main purification processes are different, and the same steps of any two main purification processes are carried out at different times;
each auxiliary purification process comprises the following steps:
(2.1) an adsorption step of opening a feed gas inlet valve B2403 and a product outlet valve B2606 of a first adsorption tower B240, allowing feed gas to enter the first adsorption tower B240 from bottom to top after being subjected to water-gas separation by a feed gas buffer tank B210, adsorbing impurity components under working pressure, allowing non-adsorbed product components to flow out through the product outlet valve B2406 of the first adsorption tower B240, wherein most of the non-adsorbed product components enter the product gas buffer tank B220 as products, allowing the rest of the non-adsorbed product components to enter a second adsorption tower B240 from top to bottom by a final flushing flow regulating valve 2412 and a sequential/secondary equalizing valve B2408 for final pressure rising, and closing the feed gas inlet valve B2403 and the product outlet valve B2406 of the first adsorption tower B240 after the adsorption step of the first adsorption tower B240 is finished;
(2.2) a first equalization step of opening the final pressure increasing/primary pressure equalizing valve B2407 of the first adsorption tower B240, opening the final pressure increasing/primary pressure equalizing valve B2407 of the third adsorption tower B240 immediately after the second equalization step, performing first-stage pressure equalization on the first adsorption tower B240 and the third adsorption tower B240, and reducing the pressure of the first adsorption tower B240 until the pressures of the first adsorption tower B240 and the third adsorption tower B240 are substantially equal, and closing the final pressure increasing/primary pressure equalizing valve a2407 of the first adsorption tower B240 and the final pressure increasing/primary pressure equalizing valve B2407 of the third adsorption tower B240 after the first equalization step of the first adsorption tower B240 is completed;
(2.3) a sequential discharging step of opening a sequential discharging/secondary equalizing valve B2408 of the first adsorption tower B240, opening a reverse discharging valve B2404 of the fourth adsorption tower B240, flushing the fourth adsorption tower B240 which just ends reverse discharging with residual gas in the first adsorption tower B240 until the pressure of the first adsorption tower B240 is reduced to a specified value, and closing the reverse discharging valve B2404 of the fourth adsorption tower B240 after the sequential discharging step of the first adsorption tower B240 is ended;
(2.4) continuing to open the forward/secondary equalizing valve B2408 of the first adsorption tower B240, opening the forward/secondary equalizing valve B2408 of the fourth adsorption tower B240, enabling the residual gas in the first adsorption tower B240 to enter the fourth adsorption tower B240 from top to bottom, performing second-stage pressure balance on the first adsorption tower B240 and the fourth adsorption tower B240, and further reducing the pressure of the first adsorption tower B240 until the pressures of the first adsorption tower B240 and the fourth adsorption tower B240 are basically equal, and closing the forward/secondary equalizing valve B2408 of the fourth adsorption tower B240 after the second equalizing step of the first adsorption tower B240 is finished;
(2.5) a reverse discharge step of continuously opening a reverse discharge valve B2408 of the fourth adsorption tower B240, discharging the residual gas in the first adsorption tower B240 to the tail gas tank 230 until the pressure in the first adsorption tower B240 is lower than the pressure in the tail gas tank 230, and opening a discharge valve B2405 to discharge until the pressure in the first adsorption tower B240 is reduced to approximately 0.02MPa (G), wherein the reverse discharge step of the first adsorption tower B240 is finished;
(2.6) a flushing step of flushing the bed layer of the first adsorption tower B240 from top to bottom by opening a flushing valve B2409 of the first adsorption tower B240 and a forward/secondary pressure equalizing valve B2408 of the second adsorption tower B240, flushing impurities still remained in the first adsorption tower B240, further desorbing the impurities in the first adsorption tower B240, discharging the resolved gas through a blow-down valve B2405 of the first adsorption tower B240, and closing the flushing valve B2409 of the first adsorption tower B240, the forward/secondary pressure equalizing valve B2408 of the second adsorption tower B240 and the blow-down valve B2405 when the flushing step of the first adsorption tower B240 is finished;
(2.7) a second equalization step of opening the downstream/equalization valve B2408 of the first adsorption tower B240 and the downstream/equalization valve B2408 of the second adsorption tower B240, the first adsorption tower B240 being connected to the second adsorption tower B240 immediately after the first equalization step, the first adsorption tower B240 being subjected to a second-stage pressure equalization with the second adsorption tower B240, the first adsorption tower B240 being subjected to a pressure equalization, until the pressures of the first adsorption tower B240 and the second adsorption tower B240 are substantially equal, and closing the opened downstream/equalization valve B2408 of the first adsorption tower B240 and the downstream/equalization valve B2408 of the second adsorption tower B240 after the second equalization step of the first adsorption tower B240 is completed;
(2.8) a step of equalizing the pressure, opening the final pressure-increasing/primary equalizing valve B2407 of the first adsorption column B240 and the final pressure-increasing/primary equalizing valve B2407 of the third adsorption column B240, the first adsorption column B240 being connected to the third adsorption column B240 immediately after the completion of the adsorption step, the first adsorption column B240 being subjected to the first-stage pressure equalization with the third adsorption column B240, the first adsorption column B240 being further increased in pressure until the pressures of the first adsorption column B240 and the third adsorption column B240 are substantially equal;
(2.9) a final pressure increasing step of continuing to open the final pressure increasing/primary pressure equalizing valve B2407 of the first adsorption column B240 and the final pressure increasing/primary pressure equalizing valve B2407 of the third adsorption column B240, and allowing the product gas of the third adsorption column B240 to enter the first adsorption column B240, wherein the final pressure increasing of the first adsorption column B240 is performed until the pressure of the first adsorption column B240 is substantially close to the adsorption pressure, and returning to the step (2.1) after the final pressure increasing step of the first adsorption column B240 is completed;
the four adsorption towers B are respectively used as the first adsorption towers B of the four auxiliary purification processes, the first adsorption tower A, the second adsorption tower B, the third adsorption tower A and the fourth adsorption tower A of any two auxiliary purification processes are different, and the same steps of any two auxiliary purification processes are carried out at different times.
The principle of purifying hydrogen from raw material gas by adopting PSA separation gas process technology is to utilize the selectivity of the adsorbent to different adsorbents and the characteristic that the adsorption capacity of the adsorbent to the adsorbents is different along with the pressure change, adsorb impurity components in raw material under high pressure and desorb the impurities under low pressure so as to regenerate the adsorbent. The whole operation process is carried out at the ambient temperature
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. The high-purity hydrogen purification system is characterized by comprising a main PSA hydrogen extraction device and an auxiliary PSA hydrogen extraction device, wherein hydrogen extraction tail gas of the main PSA hydrogen extraction device is compressed to be used as raw material gas of the auxiliary PSA hydrogen extraction device, output gas of the auxiliary device is used as raw material gas of the main PSA hydrogen extraction device, the main PSA hydrogen extraction device comprises an adsorption unit A, a raw material gas buffer tank A, a product gas buffer tank A, a forward-discharge gas tank, a reverse-discharge gas tank and an analysis gas tank, the auxiliary PSA hydrogen extraction device comprises an adsorption unit B, a raw material gas buffer tank B, a product gas buffer tank B and a tail gas tank,
The adsorption unit A comprises four adsorption towers A, wherein the bottom and the top of each adsorption tower A are respectively connected with a bottom pipeline A and a top pipeline A, different positions of the bottom pipeline A are respectively connected with a raw gas inlet valve A, a reverse discharge valve A and a blow-down valve A, and different positions of the top pipeline A are respectively connected with a product outlet valve A, a final pressure-increasing/primary pressure-equalizing valve A, a forward discharge/secondary pressure-equalizing valve A and a flushing valve A;
the raw material gas buffer tank A is connected with a raw material gas input pipeline A and a raw material gas output pipeline A, the raw material gas output pipeline A is connected with a first transition pipeline, and different positions of the first transition pipeline are respectively connected with four raw material gas inlet valves A;
the product gas buffer tank A is connected with a product gas input pipeline A and a product gas output pipeline A, the product gas input pipeline A is connected with a product inlet valve A, the product inlet valve A is connected with a second transition pipeline, different positions of the second transition pipeline are respectively connected with four product outlet valves A and a third transition pipeline, and different positions of the third transition pipeline are respectively connected with four final pressure boosting/primary pressure equalizing valves A;
the forward-air discharge tank is respectively connected with a forward-air discharge input pipeline and a forward-air discharge output pipeline, the forward-air discharge input pipeline is connected with a forward-air discharge inlet valve, the forward-air discharge inlet valve is connected with a fourth transition pipeline, different positions of the fourth transition pipeline are respectively connected with four forward-air discharge/secondary pressure equalizing valves A, the forward-air discharge output pipeline is connected with a fifth transition pipeline, and different positions of the fifth transition pipeline are respectively connected with four flushing valves A;
The reverse deflation tank is connected with a reverse deflation input pipeline and a reverse deflation output pipeline, the reverse deflation input pipeline is connected with a sixth transition pipeline, different positions of the sixth transition pipeline are respectively connected with four reverse deflation valves A and a reverse deflation auxiliary valve, and the reverse deflation auxiliary valve is connected with a seventh transition pipeline;
the analytic gas tank is connected with an analytic gas input pipeline and an analytic gas output pipeline, and the analytic gas input pipeline is connected with the seventh transition pipeline;
the adsorption unit B comprises four adsorption towers B, the bottom and the top of each adsorption tower B are respectively connected with a bottom pipeline B and a top pipeline B, different positions of the bottom pipeline B are respectively connected with a raw gas inlet valve B, a reverse discharge valve B and a blow-down valve B, and different positions of the top pipeline B are respectively connected with a product outlet valve B, a final pressure-increasing/primary pressure-equalizing valve B, a forward discharge/secondary pressure-equalizing valve B and a flushing valve B;
the raw material gas buffer tank B is connected with a raw material gas input pipeline B and a raw material gas output pipeline B, the raw material gas output pipeline B is connected with an eighth transition pipeline, and different positions of the eighth transition pipeline are respectively connected with four raw material gas inlet valves B;
the product gas buffer tank B is connected with a product gas input pipeline B and a product gas output pipeline B, the product gas input pipeline B is connected with a product inlet valve B, the product inlet valve B is connected with a ninth transition pipeline, different positions of the ninth transition pipeline are respectively connected with four product outlet valves B and a tenth transition pipeline, and different positions of the tenth transition pipeline are respectively connected with four final boosting/primary equalizing valves B;
The four forward/secondary equalizing valves B are respectively connected with different positions of an eleventh transition pipeline;
the four flushing valves B are respectively connected with different positions of a twelfth transition pipeline;
the four reverse discharge valves B are respectively connected with different positions of a thirteenth transition pipeline;
the tail gas tank is connected with a tail gas input pipeline and a tail gas output pipeline, and the tail gas input pipeline is connected with a thirteenth transition pipeline;
the four emptying valves A are respectively connected with different positions of a fourteenth transition pipeline;
the four emptying valves B are respectively connected with different positions of a fifteenth transition pipeline;
the analysis gas output pipeline is connected with the raw material gas input pipeline B;
the raw material gas input pipeline A is connected with the product gas output pipeline B.
2. The high purity hydrogen purification system according to claim 1 wherein the product gas output line a is connected to a system pressure regulator valve a.
3. The high purity hydrogen purification system of claim 1 wherein the second transition line is connected to the third transition line by a final ram pressure regulator valve.
4. The high purity hydrogen purification system of claim 1 wherein the downdraft gas output line is connected to the fifth transition line through a downdraft pressure regulating valve.
5. The high purity hydrogen purification system according to claim 1, wherein the reverse bleed gas output line is connected with a reverse bleed pressure regulating valve, and the purge gas output line is connected with a purge gas pressure regulating valve.
6. The high purity hydrogen purification system according to claim 1 wherein the product gas output line B is connected to a system pressure regulator B.
7. The high purity hydrogen purification system of claim 1 wherein the ninth transition line is connected to the tenth transition line through a final flush flow regulator valve.
8. The high purity hydrogen purification system according to claim 1 wherein a forward flow rate regulating valve is further provided between each of said forward/secondary equalization valve B and said eleventh transition line.
9. The high purity hydrogen purification system of claim 1 wherein the off-gas output line is connected to an off-gas pressure regulator valve.
10. A method for purifying high purity hydrogen, characterized in that the purification device of any one of claims 1 to 9 is employed, the purification method comprises a main purification process and an auxiliary purification process, the main purification process comprises four main purification processes, the auxiliary purification process comprises four auxiliary purification processes,
Each main purification process comprises the following steps:
the method comprises the steps of (1.1) an adsorption step, namely opening a feed gas inlet valve A and a product outlet valve A of a first adsorption tower A, enabling feed gas to enter the first adsorption tower A from bottom to top after being subjected to water-gas separation through a feed gas buffer tank A, adsorbing impurity components under working pressure, enabling non-adsorbed product components to flow out through the product outlet valve A of the first adsorption tower A, enabling most of the non-adsorbed product components to enter the product gas buffer tank A as products, enabling the rest of the non-adsorbed product components to enter a second adsorption tower A from top to bottom through a final stamping force regulating valve and a sequential/secondary pressure equalizing valve A for final pressurization, and closing the feed gas inlet valve A and the product outlet valve A of the first adsorption tower A after the adsorption step of the first adsorption tower A is finished;
(1.2) a first uniform pressure reducing step of opening a final pressure increasing/equalizing valve A of the first adsorption tower A, opening a final pressure increasing/equalizing valve A of the third adsorption tower A which just ends the second uniform pressure increasing step, performing first-stage pressure balance on the first adsorption tower A and the third adsorption tower A, reducing the pressure of the first adsorption tower A until the pressure of the first adsorption tower A and the pressure of the third adsorption tower A are basically equal, and closing the final pressure increasing/equalizing valve A of the first adsorption tower A and the final pressure increasing/equalizing valve A of the third adsorption tower A after the first uniform pressure reducing step of the first adsorption tower A is ended;
(1.3) a second uniform pressure reducing step, namely opening a forward/secondary pressure equalizing valve A of the first adsorption tower A, opening a forward/secondary pressure equalizing valve A of the fourth adsorption tower A, enabling residual gas in the first adsorption tower A to enter the fourth adsorption tower A from top to bottom, performing second-stage pressure balance on the first adsorption tower A and the fourth adsorption tower A, and further reducing the pressure of the first adsorption tower A until the pressure of the first adsorption tower A is basically equal to the pressure of the fourth adsorption tower A, and closing the forward/secondary pressure equalizing valve A of the fourth adsorption tower A after the second uniform pressure reducing step of the first adsorption tower A is finished;
(1.4) a forward discharging step of opening a forward discharging inlet valve of the forward discharging tank, enabling residual gas in the first adsorption tower A to enter the forward discharging tank through a forward discharging/secondary equalizing valve A and the forward discharging inlet valve of the forward discharging inlet valve, stopping forward discharging after the pressure in the first adsorption tower A is reduced to a specified value, and closing the forward discharging/secondary equalizing valve A and the forward discharging inlet valve of the first adsorption tower A after the forward discharging step of the first adsorption tower A is finished;
(1.5) a reverse discharge step of sequentially opening a reverse discharge valve A and a reverse discharge auxiliary valve of the first adsorption tower A, sequentially discharging the residual gas in the first adsorption tower A to a reverse discharge tank and a desorption gas tank until the pressure in the first adsorption tower A is reduced to normal pressure or nearly 0.02MPa (G), and closing the reverse discharge valve A of the first adsorption tower A after the reverse discharge step of the first adsorption tower A is finished;
(1.6) a flushing step of opening a flushing valve A and a venting valve A of the first adsorption tower A, flushing the bed layer of the first adsorption tower A from top to bottom by the forward-venting gas in the forward-venting gas tank to further desorb impurities in the tower, venting the analysis gas through the venting valve A, and closing the flushing valve A, the venting valve A and the reverse-venting auxiliary valve of the first adsorption tower A after the flushing step of the first adsorption tower A is finished;
(1.7) a second equalizing step of opening the forward/equalizing valve A of the first adsorption tower A and the forward/equalizing valve A of the third adsorption tower A, wherein the first adsorption tower A is communicated with the third adsorption tower A which just ends the first equalizing step, the first adsorption tower A and the third adsorption tower A perform second-stage pressure equalization, the pressure of the first adsorption tower A is increased until the pressure of the first adsorption tower A and the pressure of the third adsorption tower A are basically equal, and after the second equalizing step of the first adsorption tower A is ended, the opened forward/equalizing valve A of the first adsorption tower A and the opened forward/equalizing valve A of the third adsorption tower A are closed;
(1.8) a step of uniform pressure rise, namely opening a final pressure rising/primary pressure equalizing valve A of a first adsorption tower A and a final pressure rising/primary pressure equalizing valve A of a fourth adsorption tower A, wherein the first adsorption tower A is communicated with the fourth adsorption tower A which just finishes the adsorption step, the first adsorption tower A and the fourth adsorption tower A perform first-stage pressure balance, and the pressure of the first adsorption tower A is further raised until the pressure of the first adsorption tower A and the pressure of the fourth adsorption tower A are basically equal;
(1.9) a final pressure increasing step of continuing to open the final pressure increasing/primary pressure equalizing valve A of the first adsorption tower A and the final pressure increasing/primary pressure equalizing valve A of the fourth adsorption tower A, wherein the product gas of the fourth adsorption tower A enters the first adsorption tower A, the final pressure increasing of the first adsorption tower A is carried out until the pressure of the first adsorption tower A is basically close to the adsorption pressure, and the step (1.1) is returned after the final pressure increasing step of the first adsorption tower A is finished;
the four adsorption towers A are respectively used as the first adsorption towers A of the four main purification processes, the first, the second, the third and the fourth adsorption towers A of any two main purification processes are different, and the same steps of any two main purification processes are carried out at different times;
each auxiliary purification process comprises the following steps:
(2.1) an adsorption step of opening a feed gas inlet valve B and a product outlet valve B of a first adsorption tower B, enabling feed gas to enter the first adsorption tower B from bottom to top after being subjected to water-gas separation through the feed gas buffer tank B, adsorbing impurity components under working pressure, enabling non-adsorbed product components to flow out through the product outlet valve B of the first adsorption tower B, enabling most of the non-adsorbed product components to enter the product gas buffer tank B as products, enabling the rest of the non-adsorbed product components to enter a second adsorption tower B from top to bottom through a final flushing flow regulating valve and a sequential/secondary equalizing valve B for final pressure increase, and closing the feed gas inlet valve B and the product outlet valve B of the first adsorption tower B after the adsorption step of the first adsorption tower B is finished;
(2.2) a step of uniform pressure reduction, namely opening a final pressure increasing/primary pressure equalizing valve B of the first adsorption tower B, opening a final pressure increasing/primary pressure equalizing valve B of the third adsorption tower B which just finishes the step of uniform pressure increase, performing first-stage pressure balance on the first adsorption tower B and the third adsorption tower B, reducing the pressure of the first adsorption tower B until the pressure of the first adsorption tower B and the pressure of the third adsorption tower B are basically equal, and closing a final pressure increasing/primary pressure equalizing valve A of the first adsorption tower B and a final pressure increasing/primary pressure equalizing valve B of the third adsorption tower B after the step of uniform pressure reduction of the first adsorption tower B is finished;
(2.3) a forward discharging step, namely opening a forward discharging/secondary equalizing valve B of the first adsorption tower B, opening a reverse discharging valve B of the fourth adsorption tower B, flushing the fourth adsorption tower B which just finishes reverse discharging by residual gas in the first adsorption tower B until the pressure of the first adsorption tower B is reduced to a specified value, finishing the forward discharging step of the first adsorption tower B, and closing the reverse discharging valve B of the fourth adsorption tower B;
(2.4) continuing to open the forward/secondary equalizing valve B of the first adsorption tower B, opening the forward/secondary equalizing valve B of the fourth adsorption tower B, enabling residual gas in the first adsorption tower B to enter the fourth adsorption tower B from top to bottom, performing second-stage pressure balance on the first adsorption tower B and the fourth adsorption tower B, and further reducing the pressure of the first adsorption tower B until the pressure of the first adsorption tower B is basically equal to the pressure of the fourth adsorption tower B, and closing the forward/secondary equalizing valve B of the fourth adsorption tower B after the second equalizing step of the first adsorption tower B is finished;
(2.5) a reverse discharge step, namely continuously opening a reverse discharge valve B of a fourth adsorption tower B, discharging the residual gas in the first adsorption tower B to a tail gas tank until the pressure in the first adsorption tower B is lower than the pressure of the tail gas tank, and opening a discharge valve B to discharge until the pressure in the first adsorption tower B is reduced to approximately 0.02MPa (G), wherein the reverse discharge step of the first adsorption tower B is finished;
(2.6) a flushing step of flushing the bed layer of the first adsorption tower B from top to bottom by opening a flushing valve B of the first adsorption tower B and a forward/secondary equalizing valve B of the second adsorption tower B, flushing impurities still remained in the first adsorption tower B, further desorbing the impurities in the first adsorption tower B, exhausting the analysis gas through an exhaust valve B of the first adsorption tower B, and closing the flushing valve B of the first adsorption tower B, the forward/secondary equalizing valve B of the second adsorption tower B and the exhaust valve B after the flushing step of the first adsorption tower B is finished;
(2.7) a second uniform pressure step, namely opening the forward/uniform pressure valve B of the first adsorption tower B and the forward/uniform pressure valve B of the second adsorption tower B, wherein the first adsorption tower B is communicated with the second adsorption tower B which just finishes the first uniform pressure step, the first adsorption tower B and the second adsorption tower B perform second-stage pressure balance, the pressure of the first adsorption tower B is increased until the pressure of the first adsorption tower B is basically equal to the pressure of the second adsorption tower B, and after the second uniform pressure step of the first adsorption tower B is finished, closing the opened forward/uniform pressure valve B of the first adsorption tower B and the opened forward/uniform pressure valve B of the second adsorption tower B;
(2.8) a step of uniform pressure rise, namely opening a final pressure rising/primary pressure equalizing valve B of the first adsorption tower B and a final pressure rising/primary pressure equalizing valve B of the third adsorption tower B, wherein the first adsorption tower B is communicated with the third adsorption tower B which just finishes the adsorption step, the first adsorption tower B and the third adsorption tower B perform first-stage pressure balance, and the pressure of the first adsorption tower B is further raised until the pressure of the first adsorption tower B and the pressure of the third adsorption tower B are basically equal;
(2.9) a final pressure increasing step of continuing to open the final pressure increasing/primary pressure equalizing valve B of the first adsorption tower B and the final pressure increasing/primary pressure equalizing valve B of the third adsorption tower B, enabling the product gas of the third adsorption tower B to enter the first adsorption tower B, and returning to the step (2.1) after the final pressure increasing step of the first adsorption tower B is finished until the pressure of the first adsorption tower B is basically close to the adsorption pressure;
the four adsorption towers B are respectively used as the first adsorption towers B of the four auxiliary purification processes, the first adsorption tower A, the second adsorption tower B, the third adsorption tower A and the fourth adsorption tower A of any two auxiliary purification processes are different, and the same steps of any two auxiliary purification processes are carried out at different times.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811081138.3A CN108910824B (en) | 2018-09-17 | 2018-09-17 | High-purity hydrogen purification system and purification method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811081138.3A CN108910824B (en) | 2018-09-17 | 2018-09-17 | High-purity hydrogen purification system and purification method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108910824A CN108910824A (en) | 2018-11-30 |
| CN108910824B true CN108910824B (en) | 2023-08-04 |
Family
ID=64408467
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811081138.3A Active CN108910824B (en) | 2018-09-17 | 2018-09-17 | High-purity hydrogen purification system and purification method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108910824B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112987824B (en) * | 2021-02-05 | 2022-04-08 | 阳光电源股份有限公司 | Control method and related device of hydrogen production purification system |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4772420A (en) * | 1984-10-18 | 1988-09-20 | Imperial Chemical Industries Plc | Gas separation |
| CN1032115A (en) * | 1987-09-16 | 1989-04-05 | 日本酸素株式会社 | Adsorption separation method |
| EP0314040A1 (en) * | 1987-10-24 | 1989-05-03 | Saibu Gas Co.,Ltd. | Method for removing carbon dioxide gas and moisture in a city gas production |
| EP0398339A2 (en) * | 1989-05-18 | 1990-11-22 | Air Products And Chemicals, Inc. | Adsorptive process for producing two gas streams from a gas mixture |
| CN1903703A (en) * | 2006-08-04 | 2007-01-31 | 四川亚联高科技有限责任公司 | Technological method of purifying hydrogen of hydrogen enriched gas source |
| CN101700874A (en) * | 2009-09-09 | 2010-05-05 | 张文波 | Hydrogen making method by pressure swing adsorption |
| CN101874962A (en) * | 2010-04-28 | 2010-11-03 | 上海戊正工程技术有限公司 | Process and matching system for separating carbonylation feed gas |
| CN201873514U (en) * | 2010-07-15 | 2011-06-22 | 苏州金宏气体股份有限公司 | Push-type small-sized purification device using super-pure hydrogen |
| CN102343196A (en) * | 2011-07-08 | 2012-02-08 | 杭州普菲科空分设备有限公司 | Method and device for one-stage pressure swing adsorption hydrogen extraction and carbon-rich gas recovery |
| CN202136904U (en) * | 2011-07-08 | 2012-02-08 | 杭州普菲科空分设备有限公司 | Device for extracting hydrogen and recovering carbon-rich gas by one-stage process variable pressure adsorption |
| CN102701151A (en) * | 2012-06-12 | 2012-10-03 | 四川亚连科技有限责任公司 | High-purity and high-recovery hydrogen purifying method and realizing device |
| CN108310909A (en) * | 2017-01-17 | 2018-07-24 | 四川天采科技有限责任公司 | A method of p-phthalic acid's tail gas pressure-variable adsorption containing CO extracts H2 |
-
2018
- 2018-09-17 CN CN201811081138.3A patent/CN108910824B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4772420A (en) * | 1984-10-18 | 1988-09-20 | Imperial Chemical Industries Plc | Gas separation |
| CN1032115A (en) * | 1987-09-16 | 1989-04-05 | 日本酸素株式会社 | Adsorption separation method |
| EP0314040A1 (en) * | 1987-10-24 | 1989-05-03 | Saibu Gas Co.,Ltd. | Method for removing carbon dioxide gas and moisture in a city gas production |
| EP0398339A2 (en) * | 1989-05-18 | 1990-11-22 | Air Products And Chemicals, Inc. | Adsorptive process for producing two gas streams from a gas mixture |
| CN1903703A (en) * | 2006-08-04 | 2007-01-31 | 四川亚联高科技有限责任公司 | Technological method of purifying hydrogen of hydrogen enriched gas source |
| CN101700874A (en) * | 2009-09-09 | 2010-05-05 | 张文波 | Hydrogen making method by pressure swing adsorption |
| CN101874962A (en) * | 2010-04-28 | 2010-11-03 | 上海戊正工程技术有限公司 | Process and matching system for separating carbonylation feed gas |
| CN201873514U (en) * | 2010-07-15 | 2011-06-22 | 苏州金宏气体股份有限公司 | Push-type small-sized purification device using super-pure hydrogen |
| CN102343196A (en) * | 2011-07-08 | 2012-02-08 | 杭州普菲科空分设备有限公司 | Method and device for one-stage pressure swing adsorption hydrogen extraction and carbon-rich gas recovery |
| CN202136904U (en) * | 2011-07-08 | 2012-02-08 | 杭州普菲科空分设备有限公司 | Device for extracting hydrogen and recovering carbon-rich gas by one-stage process variable pressure adsorption |
| CN102701151A (en) * | 2012-06-12 | 2012-10-03 | 四川亚连科技有限责任公司 | High-purity and high-recovery hydrogen purifying method and realizing device |
| CN108310909A (en) * | 2017-01-17 | 2018-07-24 | 四川天采科技有限责任公司 | A method of p-phthalic acid's tail gas pressure-variable adsorption containing CO extracts H2 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108910824A (en) | 2018-11-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101088591A (en) | Pressure swing adsorption process with improved recovery of high purity product | |
| CA2550403A1 (en) | Valve operation diagnostic method for pressure swing adsorption systems | |
| EP2938423B1 (en) | Method and device for separating a gas mixture by means of pressure swing adsorption | |
| EP1549413A4 (en) | High recovery psa cycles and apparatus with reduced complexity | |
| CN103101891A (en) | Method for producing nitrogen gas, method for separating gas and device for producing nitrogen gas | |
| JP6468659B2 (en) | Helium gas purification method and purification system | |
| CN111871149B (en) | Two-stage pressure swing adsorption system for recovering adsorbed components and application method thereof | |
| US8828118B2 (en) | Staged blowdown of adsorbent bed | |
| EP3549657B1 (en) | Gas separation and recovery method and equipment | |
| CN108910824B (en) | High-purity hydrogen purification system and purification method | |
| Das et al. | Development of a helium purification system using pressure swing adsorption | |
| KR100856912B1 (en) | Refined Nitrogen Feeder | |
| KR20160113969A (en) | Purification method and purification system for helium gas | |
| CN109502547B (en) | Method for separating and purifying hydrogen from refinery tail gas | |
| US4475930A (en) | Pressure swing adsorption system using product gas as replacement for purge gas | |
| CN110639328A (en) | A method for removing trace carbon impurities in the process of tail gas recovery hydrogen treatment | |
| GB2154465A (en) | Gas separation method and apparatus | |
| CN109276973B (en) | Method for separating and purifying hydrogen from refining vent gas | |
| WO2015146213A1 (en) | Method and system for purifying carbon dioxide gas | |
| US4522637A (en) | Integrated adsorption system for the purification of separate crude gases | |
| JP7319830B2 (en) | Nitrogen production method and apparatus | |
| CN220424946U (en) | Carbon dioxide purification device | |
| JP7502962B2 (en) | Gas purification device and gas purification method | |
| CN116474519A (en) | Three-tower series pressure swing adsorption device and pressure equalizing process thereof | |
| CN110252083B (en) | Pressure swing adsorption method for synthetic tail gas in PVC production |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |