CN106931722B - A kind of separation of synthesis gas components and recyclable device and method - Google Patents
A kind of separation of synthesis gas components and recyclable device and method Download PDFInfo
- Publication number
- CN106931722B CN106931722B CN201710276715.3A CN201710276715A CN106931722B CN 106931722 B CN106931722 B CN 106931722B CN 201710276715 A CN201710276715 A CN 201710276715A CN 106931722 B CN106931722 B CN 106931722B
- Authority
- CN
- China
- Prior art keywords
- gas
- hydrogen
- stream
- carbon dioxide
- permeate
- 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
- 238000000926 separation method Methods 0.000 title claims abstract description 40
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 34
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims abstract description 27
- 239000007789 gas Substances 0.000 claims abstract description 155
- 230000007246 mechanism Effects 0.000 claims abstract description 97
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 65
- 239000012528 membrane Substances 0.000 claims abstract description 54
- 239000001257 hydrogen Substances 0.000 claims abstract description 46
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 46
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 42
- 230000006835 compression Effects 0.000 claims abstract description 38
- 238000007906 compression Methods 0.000 claims abstract description 38
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 33
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 31
- 238000011084 recovery Methods 0.000 claims abstract description 19
- 239000012466 permeate Substances 0.000 claims abstract description 16
- 239000002994 raw material Substances 0.000 claims abstract description 6
- 239000012465 retentate Substances 0.000 claims abstract 5
- 238000001816 cooling Methods 0.000 claims description 46
- 239000007788 liquid Substances 0.000 claims description 28
- 239000000203 mixture Substances 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 5
- 239000012071 phase Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims 2
- 238000005265 energy consumption Methods 0.000 abstract description 11
- 230000032258 transport Effects 0.000 abstract 1
- 230000008595 infiltration Effects 0.000 description 37
- 238000001764 infiltration Methods 0.000 description 37
- 229960004424 carbon dioxide Drugs 0.000 description 21
- 238000004064 recycling Methods 0.000 description 15
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 7
- QPILHXCDZYWYLQ-UHFFFAOYSA-N 2-nonyl-1,3-dioxolane Chemical compound CCCCCCCCCC1OCCO1 QPILHXCDZYWYLQ-UHFFFAOYSA-N 0.000 description 6
- 101000851593 Homo sapiens Separin Proteins 0.000 description 6
- 102100036750 Separin Human genes 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 239000008246 gaseous mixture Substances 0.000 description 5
- 239000007792 gaseous phase Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000005057 refrigeration Methods 0.000 description 4
- 239000002250 absorbent Substances 0.000 description 3
- 230000002745 absorbent Effects 0.000 description 3
- 239000005431 greenhouse gas Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 239000003507 refrigerant Substances 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- 241001415395 Spea Species 0.000 description 1
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
- F25J3/0625—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/0655—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of hydrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D2053/221—Devices
- B01D2053/223—Devices with hollow tubes
- B01D2053/224—Devices with hollow tubes with hollow fibres
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation step
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/02—Multiple feed streams, e.g. originating from different sources
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/04—Separating impurities in general from the product stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
本发明公开了一种用于合成气组分分离与回收的装置及方法。该装置包括：压缩机构，其用于接收膜分离机构输送的渗透气，将渗透气压力压缩到与原料气同一等级，将两者混合后输送至深冷机构；深冷机构，其用于接收来自所述压缩机构的混合气，并分离回收其中的二氧化碳气体，并排出富氢气体；膜分离机构，其用于接收来自所述深冷机构的富氢气体，对气体中氢气和二氧化碳做进一步分离，可得到氢纯度较高的渗余气和含二氧化碳较多的渗透气。本发明的装置通过压缩机构、深冷机构和膜分离机构的协调配合工作，不仅能够高效回收合成气中氢气及二氧化碳，而且实现了在低能耗回收的情况下同时获得高回收率。
The invention discloses a device and method for separation and recovery of synthesis gas components. The device includes: a compression mechanism, which is used for receiving the permeate gas delivered by the membrane separation mechanism, compresses the permeate gas pressure to the same level as the raw material gas, and mixes the two and transports them to the cryogenic mechanism; the cryogenic mechanism is used for receiving The mixed gas from the compression mechanism, and the carbon dioxide gas in it is separated and recovered, and the hydrogen-rich gas is discharged; the membrane separation mechanism is used to receive the hydrogen-rich gas from the cryogenic mechanism, and further the hydrogen and carbon dioxide in the gas are After separation, retentate gas with higher hydrogen purity and permeate gas with more carbon dioxide can be obtained. Through the coordinated work of the compression mechanism, the cryogenic mechanism and the membrane separation mechanism, the device of the invention can not only efficiently recover the hydrogen and carbon dioxide in the synthesis gas, but also achieve a high recovery rate with low energy consumption.
Description
Technical field
The invention belongs to synthesis gas process fields, and in particular to a kind of device and the side of synthesis gas components separation and recycling
Method.
Background technique
In synthesis gas production with preparation process, due to the difference of raw material sources and processing technology, reacts and be prepared
Synthesis gas contains in addition to hydrogen also a large amount of foreign gases (carbon dioxide, hydrogen sulfide, nitrogen etc.).From purifying hydrogen of hydrogen, control
Greenhouse gas emission reduces the angle that sour gas corrodes follow-up equipment and sets out, it is necessary to separate synthesis gas, with preparation
Required product, and guarantee the safety of downstream process and product.
Compression condensation method is that a kind of traditional gas separating method is passed through using the difference of each component dew point in unstripped gas
Pressurization and cooling by its partial liquefaction, at low temperature rectifying and realize gas and separate.This method simple, treating capacity with process
Greatly, the advantages that rate of recovery is high has been widely used in synthesis gas separation and recycling.But compression condensation method mainly have with
Lower shortcoming: the starting time is long, flexibility is poor, energy consumption is high.It furthermore is that gas is avoided to block pipeline, it is also necessary to which removing is former in advance
Expect carbon dioxide and moisture in gas.
Pressure swing adsorption method is different using selectivity of the different component in gaseous mixture in particular adsorbent and realizes separation mesh
's.Which are mainly applied to separating synthetic gas at present, and to hydrogen purification.Although the purity is high of hydrogen product obtained by pressure swing adsorption method,
But its process is complicated, and number of devices is more, and a large amount of absorption tower is repeatedly boosted and is depressured, this needs additional energy consumption and public affairs
With engineering, operating cost and investment is caused to be increased significantly.
Domestic and international synthesis gas preparation facilities has increased separation and recovery of the membrane separation device for synthesis gas.Patent
CN101417799A, washed using low-temp methanol-desulfurization decarbonization purification system pre-processes synthesis gas, obtaining mainly includes CO
And H2Purified gas, later using heat exchanger heating enter the isolated high-purity CO of membrane separator and H2.There is investment in the method
Height, the device is complicated, recycling H2The disadvantages of purity is lower.
In patent CN202156925U, pre-separation is carried out to synthesis gas using membrane separation device, then inhale with the use of transformation
Adsorption device obtains high-purity hydrogen.Its shortcoming is that impermeable gas does not recycle, returning for the products such as hydrogen is directly reduced
Yield, while voltage raising and reducing, energy consumption are higher repeatedly for pressure-swing absorption apparatus.
In patent CN101875484A, the synthesis gas more for acid gas-containing removes synthesis using Physical Absorption solvent
H in gas2S simultaneously removes CO by chemical absorption solvents from synthesis gas2, obtain the higher H of purity2, finally by absorbent
Processing obtains high-purity CO2.Its shortcoming is that needing to carry out regeneration treatment to absorbent, energy consumption is bigger, and needs
Lasting supplement is carried out to absorbent, complicated operation.
Although H in synthesis gas may be implemented in the above method2Etc. components separation and recycling, but generally existing operation is multiple
It is miscellaneous, energy consumption is excessively high, processing it is inflexible the disadvantages of.Because the invention one kind efficiently separates synthesis gas, synthesis gas point can be especially reduced
Device and method from energy consumption in recycling has great economic interests and realistic meaning.
Summary of the invention
One of the objects of the present invention is to provide a kind of devices of synthesis gas components separation and recycling.It includes compressor
Structure, deep cooling mechanism and UF membrane mechanism.The device of the invention is matched by the collaboration of compression mechanism, deep cooling mechanism and UF membrane mechanism
Work is closed, the hydrogen and carbon dioxide of high-recovery are realized in low energy consumption while obtaining.
Another object of the present invention is to provide a kind of return using the separation of above-mentioned synthesis gas components with recyclable device to separate conjunction
At the method for gas comprising compression step, cryogenic separation step and UF membrane step.
According to an aspect of the present invention, described the present invention provides a kind of device of synthesis gas components separation and recycling
Device includes:
Compression mechanism is used to receive the infiltration gas of unstripped gas and the conveying of UF membrane mechanism, and infiltration atmospheric pressure is compressed to
With the same grade of unstripped gas, is cooled down after the two is mixed and be delivered to deep cooling mechanism；
Deep cooling mechanism is used to receive the gaseous mixture from the compression mechanism, and separates and recovers carbon dioxide therein
Gas, and hydrogen-rich gas is discharged；
UF membrane mechanism is used to receive the hydrogen-rich gas from the deep cooling mechanism, to hydrogen in gas and titanium dioxide
Carbon is further separated, and can be obtained seeping residual air and be permeated gas, wherein infiltration gas is entered compression mechanism and does circular treatment；
The device of the invention is worked by the coordinated of compression mechanism, deep cooling mechanism and UF membrane mechanism three parts, high
Effect has recycled hydrogen in synthesis gas.And the sour gas such as carbon dioxide, hydrogen sulfide present in synthesis gas are effectively recycled, it avoids
It corrodes follow-up equipment.The rate of recovery of the wherein rate of recovery of hydrogen about 99%, carbon dioxide is greater than 90%, vulcanizes hydrogen retrieval
Rate about 98%.
A specific embodiment according to the present invention, the compression mechanism includes: at least one compressor, for receiving film
Infiltration atmospheric pressure is compressed to and the same grade of unstripped gas by the infiltration gas of separating mechanism conveying；At least one mixer, being used for will
Unstripped gas and infiltration gas mixing, obtain high pressure gas first stream；At least one heat exchanger, for cooling down first stream.
A specific embodiment according to the present invention, the entrance of compression mechanism are connected with mixer first entrance, compressor
Outlet be connected with second entrance of mixer, mixer outlet is connected with the entrance of heat exchanger, the outlet and pressure of heat exchanger
The outlet of contracting mechanism is connected.
A specific embodiment according to the present invention, the deep cooling mechanism include: at least one heat exchanger, for receiving simultaneously
The cooling first stream from compression mechanism, and output temperature lower than first stream dew-point temperature containing gas-liquid mixture the
Two streams；At least one gas-liquid separator is used to receive second stream to carry out gas-liquid separation, and export back in liquid-phase outlet
The high purity liquid carbon dioxide of receipts, and third stream is exported in gaseous phase outlet；At least one expanding machine comes from film for receiving
The infiltration residual air of separator is freezed using high pressure gas expansion and obtains part electric energy.
One entrance of a specific embodiment according to the present invention, deep cooling mechanism is connected with the outlet of compression mechanism, pressure
The outlet of contracting machine is connected with the entrance of a heat exchanger, and the one outlet of heat exchanger is connected with the entrance of gas-liquid separator, gas-liquid point
Gaseous phase outlet from device is connected with an outlet of deep cooling mechanism, and the liquid-phase outlet of gas-liquid separator exports phase with the one of deep cooling mechanism
Even, expander inlet is connected with the one outlet of UF membrane mechanism, an entrance phase of expander outlet and First Heat Exchanger group
Even.
A specific embodiment according to the present invention, First Heat Exchanger is pipe heat exchanger, and effect is by using just
Compressed first stream is cooled to alap temperature by suitable cold media, such as recirculated cooling water, to save subsequent machine
The energy consumption of structure.
A specific embodiment according to the present invention avoids cryogenic gas to subsequent film group to improve device energy efficiency
The damage of part, third stream enter First Heat Exchanger group as cold logistics, are warming up to 25~35 DEG C, while will be after the expansion
Residual air is seeped to enter First Heat Exchanger group and exchange heat, thus using high pressure gas acting cool down resulting part/whole cooling capacity as
The cold source of First Heat Exchanger group.
First stream from compression mechanism is passed through heat exchanger by a specific embodiment according to the present invention, deep cooling mechanism
Group is cooled to -25~-35 DEG C, thus the sour gas such as condensing recovery carbon dioxide.
A specific embodiment according to the present invention, the UF membrane mechanism includes: at least one membrane separator, is used for
The third stream from the deep cooling mechanism is received, hydrogen in gas and carbon dioxide are further separated, can be obtained more than infiltration
Gas and infiltration gas.
A specific embodiment according to the present invention, the entrance of UF membrane mechanism are connected with the first outlet of deep cooling mechanism,
Membrane separator entrance is connected with UF membrane mechanism entrance, the output of the first outlet of UF membrane mechanism seep residual air and with the deep cooling machine
One entrance of expanding machine in structure is connected, the second outlet output infiltration gas of UF membrane mechanism.
A specific embodiment according to the present invention, the infiltration gas enter the compression mechanism and do circular treatment, by
This significantly improves the rate of recovery of hydrogen and carbon dioxide.
According to a further aspect of the present invention, it separates to come with the device recycled using synthesis gas components the present invention provides a kind of
The method for separating and recovering synthesis gas comprising following steps:
Compression step, receives infiltration gas and unstripped gas, and will infiltration atmospheric pressure be compressed to the same grade of unstripped gas, by two
It is exported after person's mixing；
Cryogenic separation step receives gaseous mixture, and separates and recovers carbon dioxide gas therein, and hydrogen-rich gas is discharged；
UF membrane step receives hydrogen-rich gas, is further separated to hydrogen in gas and carbon dioxide, and residual air is seeped in discharge
With infiltration gas, and by infiltration gas make circular treatment.
Compression deep cooling, UF membrane are all common separation means, and the present invention passes through the reasonably optimizing to different separation modules
With combine, provide a kind of device and method of synthesis gas components separation and recycling, sufficiently use high pressure feed, avoid repeatedly
Energy waste caused by voltage raising and reducing.And in view of the deficiencies of the prior art, have the following prominent advantages: 1, to gas-liquid separator
Gained gas phase stream carries out cold recovery, and seeps residual air swell refrigeration using high pressure, reduces the consumption of expensive low-temperature refrigerant
2, infiltration gas circular treatment obtained by UF membrane mechanism is improved to the rate of recovery 3, swollen using turbine of the gases such as hydrogen, carbon dioxide
Swollen machine produces electric power, and the whole energy consumption 4 of reduction, plant investment are few, and high financial profit is environment friendly and pollution-free.
Detailed description of the invention
To describe the technical solutions in the embodiments of the present invention more clearly, make required in being described below to embodiment
Attached drawing, which is done, simply to be introduced, it is therefore apparent that the attached drawing in brief description is only some embodiments of the present invention, for this
For the those of ordinary skill of field, without creative efforts, it can also be obtained according to these attached drawings others
Attached drawing.
Fig. 1 shows a kind of schematic devices of synthesis gas components of the invention separation and recycling.
Fig. 2 indicates the schematic device of a preferred embodiment of the present invention.
Identical component is indicated by identical appended drawing reference in the figure.The attached drawing is not drawn according to the actual ratio.
Specific embodiment
Below with reference to attached drawing of the invention, technical solution in the embodiment of the present invention understand be fully described by.It is aobvious
So, described embodiments are only a part of the embodiments of the present invention, and is not all whole embodiments.Based in the present invention
Embodiment, every other embodiment obtained by those of ordinary skill in the art without making creative efforts, all
Belong to the scope of protection of the invention.
As shown in Fig. 1, it is separated the present invention provides a kind of synthesis gas components and includes: with the device of recycling
Compression mechanism X is used to receive the infiltration gas FP of unstripped gas Feed and UF membrane mechanism Z conveying, will permeate gas FP
Pressure be compressed to the same grade of unstripped gas, cooled down after the two is mixed and be delivered to deep cooling mechanism；
Deep cooling mechanism Y is used to receive the gaseous mixture F1 from the compression mechanism, and separates and recovers titanium dioxide therein
Carbon gas FL, and hydrogen-rich gas FG is discharged；
UF membrane mechanism Z is used to receive the hydrogen-rich gas FG from the deep cooling mechanism, to hydrogen in gas and dioxy
Change carbon to be further separated, can obtain seeping residual air FR and permeate gas FP, wherein infiltration gas FP is entered compression mechanism X and does at circulation
Reason；
In the present embodiment, the molar flow rate of unstripped gas is 30000kmol/h, and pressure 5MPa, temperature is 20 DEG C, wherein
Each component molar fraction is as follows: hydrogen 56.4%, carbon dioxide 41.3%, carbon monoxide 1.1%, nitrogen 0.7%, hydrogen sulfide
0.5%.
In the present embodiment, compression mechanism X includes a compressor COM, for receiving the infiltration of UF membrane mechanism Z conveying
Gas FP, and its pressure is promoted to 5MPa by 0.61MPa；One mixer MIX, for mixing unstripped gas Feed and infiltration gas FP
It closes, obtains first stream F1, pressure 5MPa；One heat exchanger HEAT1, for first stream F1 to be cooled to by 133.5 DEG C
35 DEG C, and output stream stock F2.
In the present embodiment, the entrance T1 of compression mechanism X is connected with mixer MIX first entrance T2, and compressor COM's goes out
Mouth T7 is connected with second entrance T4 of mixer MIX, and mixer outlet T3 is connected with the entrance T8 of heat exchanger HEAT1, heat exchange
The outlet T9 of device HEAT1 is connected with the one outlet T10 of compression mechanism X.
In the present embodiment, the heat exchanger HEAT1 is pipe heat exchanger, and effect is by using cheap refrigerant
It is situated between, such as recirculated cooling water, compressed first stream F1 is cooled to alap temperature, to save the energy of follow-up mechanism
Consumption.
In the present embodiment, the deep cooling mechanism includes Y: one multithread stock heat exchanger MHEX, is exchanged heat with matching between stream stock
Cooling capacity is recycled, and stream stock F2 is cooled to -15 DEG C；Stream stock F3 is cooled to -30 DEG C by one heat exchanger HEAT2；One gas-liquid point
From device SEPA, it is used to receive second stream F4 to carry out gas-liquid separation, and in the purity of liquid-phase outlet T17 output up to 96%
Liquid CO 2, ult rec 90.0%, while the also hydrogen sulfide being discharged, the rate of recovery 98.3%, and
Gaseous phase outlet exports third stream T15；One turbo-expander TURB, for receiving the infiltration residual air FR from UF membrane mechanism Z,
And its pressure is down to 3.1MPa by 5MPa, temperature is reduced to 2.3 DEG C by 30 DEG C, while generating the electric power of 4.1MW, after cooling
It seeps residual air and is admitted to multithread stock heat exchanger MHEX recycling cooling capacity.
In the present embodiment, the entrance T11 of deep cooling mechanism is connected with the outlet T10 of compression mechanism, the outlet heat exchanger HEAT1
T9 is connected with an entrance a1 of multithread stock heat exchanger, the one outlet a2 of multithread stock heat exchanger and the entrance of the second heat exchanger
T12 is connected, and the second heat exchanger exit T13 is connected with gas-liquid separator entrance T14, the liquid-phase outlet T17 and depth of gas-liquid separator
The one outlet T18 of cold structure is connected, and gaseous phase outlet T15 is connected with one entrance b1 of multithread stock heat exchanger, multithread stock heat exchanger
One outlet b2 be connected with the one outlet T16 of deep cooling mechanism, an entrance T24 of turbo-expander TURB and deep cooling mechanism
An entrance T23, the one outlet T25 of turbo-expander is connected with an entrance c1 of multithread stock heat exchanger MHEX, multithread
The one outlet c2 of stock heat exchanger MHEX is connected with the one outlet T26 of deep cooling mechanism.
In a preferred embodiment of the invention, as shown in Fig. 2, first stream F1 will by multithread stock heat exchanger MHEX
Stream stock is cooled to -30 DEG C.The outlet T5 of heat exchanger HEAT1 is connected with an entrance a1 of multithread stock heat exchanger MHEX, multithread stock
Heat exchanger MHEX one outlet a2 is connected with an entrance T14 of gas-liquid separator SEPA.
In a preferred embodiment of the invention, the multithread stock heat exchanger MHEX introduces low temperature stream stock C-1, and ingredient is
LPG, effect are to provide enough cooling capacity for other heat exchange stream stocks.The temperature of low temperature stream stock C1 is -35 DEG C, through multithread stock
An entrance f1 of heat exchanger MHEX enters, and is flowed out after heat exchange by the one outlet f2 of MHEX.
In a preferred embodiment of the invention, the infiltration residual air FR from membrane separator MEMB is introduced into the heat exchange of multithread stock
Device MHEX is cooled to -20 DEG C, then by turbo-expander TURB swell refrigeration, its temperature is made to become -56.2 DEG C, is lower than the second material
The dew-point temperature for flowing F3 subsequently enters multithread stock heat exchanger MHEX recycling cooling capacity, and final output mixture temperature is 30 DEG C, pressure
For 3.1MPa, wherein hydrogen content can be directly entered pressure-swing absorption apparatus and do further purification processes up to 90.1%.Membrane separator
The infiltration residual air outlet T21 of MEMB is connected with an entrance c1 of multithread stock heat exchanger MHEX in deep cooling mechanism Y, multithread stock heat exchanger
The entrance T24 of the one outlet c2 and turbo-expander TURB of MHEX are connected, the outlet T25 and multithread stock of turbo-expander TURB
An entrance d1 of heat exchanger MHEX is connected, the one outlet of the one outlet d2 and deep cooling mechanism Y of multithread stock heat exchanger MHEX
T26 is connected.
In a preferred embodiment of the invention, for sufficiently recycling cooling capacity, the condensate liquid from gas-liquid separator SEPA
FL becomes gas into being warming up to 30 DEG C in multithread stock heat exchanger MHEX, and from liquid, pressure 4.9MPa, and after the recovery two
Carbonoxide can inject underground, reduce greenhouse gas emission.Gas-liquid separator SEPA one outlet T15 and multithread stock heat exchanger MHEX
An entrance e1 be connected, the one outlet e2 of multithread stock heat exchanger MHEX is connected with the outlet T18 of deep cooling mechanism.
In a preferred embodiment of the invention, to residual air FR is seeped using the method for first cooling reflation refrigeration, make its temperature
Degree can satisfy the demand with second stream F3 heat exchange, reduces the use of expensive cryogenic coolant, effectively reduces flow operations
Expense and equipment requirement.
In the present embodiment, the UF membrane mechanism Z includes: a membrane separator MEMB, is used to receive from described
The third stream FG of deep cooling mechanism Y, is further separated hydrogen in gas and carbon dioxide, can obtain seeping residual air FR and infiltration
Gas FP.
In the present embodiment, the entrance T19 of UF membrane mechanism Z is connected with the outlet T16 of deep cooling mechanism, membrane separator MEMB
Entrance T20 be connected with the entrance T19 of UF membrane mechanism Z, membrane separator MEMB seeps residual air outlet T21 and expanding machine TURB and enters
Mouth T24 is connected, and membrane separator MEMB seeps vent outlet T27 and is connected with an outlet T28 of film separating structure Z, film separating structure Z's
Outlet T28 is connected with an entrance T5 of compression mechanism X.
In the present embodiment, the used film type of membrane separator MEMB is hollow-fibre membrane, CO2/H2Selectivity be 10,
Membrane area is 1620m2。
In the present embodiment, the infiltration gas FP does circular treatment into the compression mechanism X, thus significantly improves
The rate of recovery of hydrogen and carbon dioxide.
In a preferred embodiment of the invention, the infiltration gas FP is introduced into swollen by turbine in the deep cooling mechanism Y
In the coaxial compressor TURB-COM that swollen machine drives, pressure is increased to 1.03MPa by 0.61MPa.Enter the compression later to tie
Pressure rise is to 5MPa in the compressor COM of structure X.The infiltration vent outlet T27 of membrane separator MEMB is coaxial with turbo-expander
The entrance T30 of compressor TURB-COM is connected, and compressor enters in the outlet T31 and compression mechanism X of coaxial compressor TURB-COM
Mouth T7 is connected.
From the above embodiment of the present invention as it can be seen that apparatus of the present invention are cooperated by cryogenic separation and membrane separator, separation is closed
At hydrogen in gas and other gases, gas reclaiming rate, reasonable employment expander refrigeration, reduction pair are improved by setting circulator
The dependence of expensive refrigerant has the advantages that low energy consumption, small investment, high financial profit is environment friendly and pollution-free.
The present invention also provides a kind of to separate the device with recycling using synthesis gas components to separate and recover the side of synthesis gas
Method comprising following steps:
Compression step, receives infiltration gas and unstripped gas, and will infiltration atmospheric pressure be compressed to the same grade of unstripped gas, by two
It is exported after person's mixing, concrete operation step are as follows: (1) the infiltration gas FP from membrane separator structure Z is forced by compressor COM
5MPa；(2) compressed infiltration gas FP is all that 5MPa unstripped gas Feed mixes output first stream F1, pressure with pressure by mixer
Power is 5MPa, 133.5 DEG C of temperature；(3) first stream F1 is cooled to 35 DEG C by heat exchanger HEAT1.
Cryogenic separation step receives gaseous mixture, and separates and recovers carbon dioxide gas therein, and hydrogen-rich gas is discharged,
Concrete operation step are as follows: (1) utilize multithread stock heat exchanger MHEX, stream stock F2 temperature is reduced to -30 DEG C, exports second stream F3
Into gas-liquid separator SPEA；(2) second stream F3 carries out gas-liquid separation in gas-liquid separator SEPA, gaseous phase outlet output the
Three stream FG, liquid-phase outlet output liquid carbon dioxide etc.；(3) simultaneously for recycling cooling capacity, cryogenic gas is avoided to damage film unit
Evil, third stream FG enter multithread stock heat exchanger MHEX and carry out re-heat, and temperature rises to 30 DEG C by -30 DEG C, finally from deep cooling mechanism Y
Middle output enters UF membrane mechanism Z；(4) it receives and cools down more than the infiltration from membrane separator MEMB using multithread stock heat exchanger MHEX
Gas FR makes its temperature be reduced to -20 DEG C by 30 DEG C, is transported to turbo-expander TURB；(5) residual air FR is seeped in turbine expansion
Heating is depressured in machine TURB, pressure becomes 3.1MPa from 5MPa, and temperature is reduced to -56.2 DEG C by -20 DEG C；(6) after reducing temperature
Infiltration residual air FR be transported in multithread stock heat exchanger MHEX and carry out cold recovery, finally in the exit multithread stock heat exchanger MHEX
Its temperature is 28.1 DEG C, and hydrogen content can be used for subsequent technique processing up to 90.1%, the rate of recovery 99.6%；(7) it is returned to be abundant
Receipts cooling capacity, the condensate liquid FL from gas-liquid separator SEPA, into temperature in multithread stock heat exchanger MHEX by -30 DEG C to 30 DEG C,
And gas, pressure 4.9MPa are become from liquid, carbon dioxide after the recovery can inject underground, reduce greenhouse gas emission.
UF membrane step receives hydrogen-rich gas, is further separated to hydrogen in gas and carbon dioxide, and residual air is seeped in discharge
With infiltration gas, and by infiltration gas make circular treatment；Concrete operation step are as follows: (1) third stream FG inputs membrane separator MEMB (film
Area 1620m2, osmotic lateral pressure 0.61MPa) in, membrane module will shut off most of hydrogen, and output infiltration gas FP seeps residual air FR
The multithread stock heat exchanger MHEX being then delivered in deep cooling mechanism Y；(2) the first coaxial pressure through turbo-expander of infiltration gas FP exported
Contracting machine TURB-COM compression, pressure rise to 1.02MPa by 0.61MPa, are transported to compression mechanism X later.
It should be noted that embodiment described above for explaining only the invention, is not constituted to of the invention any
Limitation.By referring to exemplary embodiments, invention has been described, it should be appreciated that word used in it is descriptive
With explanatory vocabulary, rather than limited vocabulary.The present invention can be made within the scope of the claims by regulation
Modification, and the present invention is revised in without departing substantially from scope and spirit of the present invention.Although the present invention described in it relates to
And specific method, material and embodiment, it is not intended that the present invention is limited to particular case disclosed in it, on the contrary, this hair
It is bright to can be extended to other all methods and applications with the same function.
Claims (5)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710276715.3A CN106931722B (en) | 2017-04-25 | 2017-04-25 | A kind of separation of synthesis gas components and recyclable device and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710276715.3A CN106931722B (en) | 2017-04-25 | 2017-04-25 | A kind of separation of synthesis gas components and recyclable device and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106931722A CN106931722A (en) | 2017-07-07 |
| CN106931722B true CN106931722B (en) | 2019-05-31 |
Family
ID=59437145
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710276715.3A Active CN106931722B (en) | 2017-04-25 | 2017-04-25 | A kind of separation of synthesis gas components and recyclable device and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106931722B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107514873A (en) * | 2017-08-30 | 2017-12-26 | 浙江大学 | Device and method for separating and purifying syngas |
| CN107381504B (en) * | 2017-08-30 | 2020-01-10 | 浙江大学 | Device and method for preparing high-purity hydrogen from synthesis gas |
| CN110173960A (en) * | 2019-06-28 | 2019-08-27 | 正和集团股份有限公司 | A kind of recycle device and technique of hydrogen-rich gas |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63247582A (en) * | 1987-03-31 | 1988-10-14 | 株式会社神戸製鋼所 | Low-temperature separating method of carbon monoxide |
| JPH02157101A (en) * | 1988-12-09 | 1990-06-15 | Ube Ind Ltd | Method for purifying hydrogen gas or helium gas |
| US6568206B2 (en) * | 2001-07-18 | 2003-05-27 | Air Products And Chemicals, Inc. | Cryogenic hydrogen and carbon monoxide production with membrane permeate expander |
| US8911519B2 (en) * | 2007-07-27 | 2014-12-16 | Nippon Oil Corporation | Method and apparatus for hydrogen production and carbon dioxide recovery |
| EP2457048B1 (en) * | 2009-07-24 | 2020-07-01 | BP Technology Ventures Limited | Separation of carbon dioxide and hydrogen |
| US8911535B2 (en) * | 2010-10-06 | 2014-12-16 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Carbon dioxide removal process |
| CN202156925U (en) * | 2011-07-08 | 2012-03-07 | 南京荣欣化工有限公司 | Device for extracting hydrogen gas by using synthesis gas |
-
2017
- 2017-04-25 CN CN201710276715.3A patent/CN106931722B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN106931722A (en) | 2017-07-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US20220152552A1 (en) | Method for purifying biogas through membranes at negative temperatures | |
| CN105531015B (en) | Method of the final purification biogas to prepare biological methane | |
| CN109690215A (en) | Industrial gasses place produces integrated with liquid hydrogen | |
| CN201199120Y (en) | Separated liquefaction equipment of air conditioner back heating type mine gas | |
| CN106931722B (en) | A kind of separation of synthesis gas components and recyclable device and method | |
| US11344842B2 (en) | Apparatus and method for separating CO2 at low temperature comprising a step of separation by permeation | |
| CN111483987A (en) | Helium production process and equipment based on membrane separation | |
| EP0270040A2 (en) | Process for removing carbon dioxide from a gas | |
| CN103663368A (en) | Method for recycling hydrogen and ammonia in synthetic ammonia exhausted gas | |
| CN107381504B (en) | Device and method for preparing high-purity hydrogen from synthesis gas | |
| CN107514873A (en) | Device and method for separating and purifying syngas | |
| RU145348U1 (en) | INSTALLATION OF A MEMBRANE SEPARATION OF A HIGH PRESSURE GAS MIXTURE | |
| CN203593618U (en) | Device for recycling hydrogen and ammonia in synthesis ammonia purge gas | |
| CN107108244A (en) | The apparatus and method of production ammonia and the remodeling method of correlation are purified for deep cooling | |
| CN119607813A (en) | A room temperature natural gas helium extraction and purification system and purification method thereof | |
| CN106969597B (en) | A kind of oxygen-enriched space division technique | |
| CN201359420Y (en) | Low temperature separation equipment of mine gas | |
| EP4209260B1 (en) | Apparatus and method for mixing transmission and separation of hydrogen gas and natural gas recovered based on pressure energy | |
| CN114877619B (en) | System and method for liquefying carbon dioxide | |
| US20250205658A1 (en) | Power reduction membrane processes | |
| US10516180B2 (en) | Carbon dioxide removal system for anode exhaust of a fuel cell | |
| CN216171118U (en) | Device system for purifying helium by using composite process | |
| CN101493277B (en) | Low temperature separation method and apparatus for mine gas | |
| US11913718B2 (en) | Argon and power production by integration with power plant | |
| CN211177620U (en) | Hydrogen device for co-production of fuel cell vehicle by PDH separation system |
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 |