CN110002402A - Raw coke oven gas extracts CO and H2Method - Google Patents
Raw coke oven gas extracts CO and H2Method Download PDFInfo
- Publication number
- CN110002402A CN110002402A CN201910328427.7A CN201910328427A CN110002402A CN 110002402 A CN110002402 A CN 110002402A CN 201910328427 A CN201910328427 A CN 201910328427A CN 110002402 A CN110002402 A CN 110002402A
- Authority
- CN
- China
- Prior art keywords
- gas
- coke oven
- raw coke
- oven gas
- removal
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000000571 coke Substances 0.000 title claims abstract description 46
- 239000000284 extract Substances 0.000 title claims description 11
- 238000000034 method Methods 0.000 claims abstract description 33
- 238000001179 sorption measurement Methods 0.000 claims abstract description 20
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000000926 separation method Methods 0.000 claims abstract description 17
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims abstract description 16
- 230000006835 compression Effects 0.000 claims abstract description 16
- 238000007906 compression Methods 0.000 claims abstract description 16
- 230000008929 regeneration Effects 0.000 claims abstract description 10
- 238000011069 regeneration method Methods 0.000 claims abstract description 10
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 8
- 230000023556 desulfurization Effects 0.000 claims abstract description 8
- 238000004519 manufacturing process Methods 0.000 claims abstract description 6
- 230000001172 regenerating effect Effects 0.000 claims abstract description 4
- 230000005540 biological transmission Effects 0.000 claims abstract description 3
- 238000005235 decoking Methods 0.000 claims abstract description 3
- 239000000446 fuel Substances 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 16
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 2
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 69
- 239000001257 hydrogen Substances 0.000 description 19
- 229910052739 hydrogen Inorganic materials 0.000 description 19
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 6
- 239000006227 byproduct Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000002737 fuel gas Substances 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- WINTXHPCODMMRI-UHFFFAOYSA-N benzene naphthalene Chemical compound C1=CC=CC=C1.C1=CC=CC=C1.C1=CC=CC2=CC=CC=C21 WINTXHPCODMMRI-UHFFFAOYSA-N 0.000 description 3
- 238000006392 deoxygenation reaction Methods 0.000 description 3
- 238000001784 detoxification Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000000740 bleeding effect Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 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
- C01B3/508—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by selective and reversible uptake by an appropriate medium, i.e. the uptake being based on physical or chemical sorption phenomena or on reversible chemical reactions
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses a kind of raw coke oven gas to extract CO and H2Method, technical solution is that raw coke oven gas is purified gas after decoking pretreatment, one stage of compression, TSA benzene-removal naphthalene-removal, two-stage compression, deoxidation, conversion reaction and desulfurization, and the purified gas successively isolates CO through three sections of PSA separation2, CO and H2After obtain stripping gas, some or all of described stripping gas is sent into TSA benzene-removal naphthalene-removal process as regenerating medium to be regenerated for adsorption tower, and the stripping gas of naphthalene containing benzene after regeneration is as fuel pneumatic transmission to out-of-bounds.Process of the present invention is simple, energy-saving, production cost and operating cost are low, effective CO and H2 extracted in raw coke oven gas, realizes making full use of, reducing environmental pollution for raw coke oven gas component.
Description
Technical field
The present invention relates to chemical field, specifically a kind of raw coke oven gas extracts CO and H2Method.
Background technique
Raw coke oven gas includes tail of semi coke, coke-stove gas etc., the total amount of H2 and CO in raw coke oven gas up to 40% or more, have compared with
High economic value.During existing raw coke oven gas utilizes, raw coke oven gas is generally used to power generation or fuel gas, i.e., mainly utilizes
It is its thermal energy.And the benefit of a large amount of active principle (CO and H2 etc.) does not give full play in raw coke oven gas, application number
201610699330.3 disclose the raw coke oven gas hydrogen manufacturing technique of a kind of low energy consumption, high yield, including preliminary clearning, de- naphthalene, become
The processes such as de-, sulfur recovery, essence de- benzene, pressure swing adsorption hydrogen production, tail gas recycle, nitrogen processed.Raw coke oven gas after pre-processing and taking off naphthalene, into
Enter to become de- process and improve the yield of hydrogen to obtain more hydrogen, then carries out desulfurization in desulfurizing tower.Pass through the de- benzene work of essence again
Sequence, pressure swing adsorption hydrogen production process obtain pure hydrogen.Effective hydrogen in tail gas recycle process and nitrogen process processed recycling stripping gas, so that
Hydrogen yield further increases.The purity nitrogen that purity is 99% or more is further also obtained by nitrogen unit processed.The present invention almost returns entirely
Effective hydrogen component in stripping gas is received；It can also the products such as by-product sulphur, purity nitrogen while making pure hydrogen.But it is asked there are following
Topic: (1) to improve hydrogen recovery rate, device for recovering tail gas carries out multiple hydrogen recycling using film separation system, although on surface
The rate of recovery of hydrogen is improved, but there is a problem of that hydrogen product purity obtained is low, hydrogen recycling energy consumption is high；(2) naphthalene work is taken off
Regeneration gas in sequence need to quote it is external through steam-heated nitrogen, after the nitrogen after regeneration also needs further to remove de- naphthalene
Circulating and recovering leads to the increase of operating cost and equipment；(3) shift conversion step low-grade heat cannot efficiently use, can only be using sky
Cold or water cooling.
Summary of the invention
The purpose of the present invention is to solve above-mentioned technical problem, provide that a kind of process is simple, energy-saving, production cost
And operating cost is low, the effective CO and H2 extracted in raw coke oven gas, realizes that raw coke oven gas component makes full use of, reduces environmental pollution
Raw coke oven gas extracts CO and H2Method.
Technical solution is by raw coke oven gas through decoking pretreatment, one stage of compression, TSA benzene-removal naphthalene-removal, two-stage compression, deoxidation, change
It is purified gas after changing reaction and desulfurization, the purified gas successively isolates CO through three sections of PSA separation2, CO and H2After solved
Air-breathing, some or all of described stripping gas is sent into TSA benzene-removal naphthalene-removal process as regenerating medium to be regenerated for adsorption tower, regeneration
The stripping gas of naphthalene containing benzene afterwards is as fuel pneumatic transmission to out-of-bounds；
The hot water of by-product provides heat source, the 5-10 of lithium bromide refrigerating output for lithium bromide refrigerating in the conversion reaction process
DEG C water at low temperature is for cooling down the raw coke oven gas before TSA benzene-removal naphthalene-removal.
In the TSA benzene-removal naphthalene-removal process, TSA operating pressure 0.3MPa (G), 15~20 DEG C of operation temperature.
In the deoxidation step, the raw coke oven gas pre-heating temperature elevation after two-stage compression is subjected to deoxidation to 150 DEG C or more again, is taken off
Purified gas after oxygen is first used to preheat the raw coke oven gas after two-stage compression.
H is controlled in the conversion reaction2O/CO value is 1.2-1.3, and operation temperature is at 180~240 DEG C.
Three sections of PSA separation processes include one section of CO2PSA separation, two sections of CO PSA separation and three sections of H2PSA
Separation.
The TSA refers to temp.-changing adsorption；The PSA refers to pressure-variable adsorption.
The utility model has the advantages that
The resolution gas substitution obtained after separation external world three sections of PSA is sent into TSA benzene-removal naphthalene-removal process as regeneration gas by 1 is
Adsorption tower regeneration, the interior benzene naphthalene adsorbed of absorption regeneration tower enter in resolution gas.Since resolution gas yield is big, nitrogen can be substituted completely
Gas is as regeneration gas, and minute quantity benzene naphthalene nor affects on the normal use of gas in fuel gas pipe network in resolution gas, does not need again
Benzene naphthalene is removed, fuel gas pipe network is sent directly into, seems simple, it is actually ingenious.
Although the hot water temperature of by-product is not high in 2 shift conversion steps, being introduced into lithium bromide refrigerating process can mention for it
Supplying heat source produces 5-10 DEG C of water at low temperature, and this part water at low temperature is just being used on the raw coke oven gas before cooling TSA benzene-removal naphthalene-removal, passes through
Reducing raw gas temperature can effectively improve the benzene-removal naphthalene-removal efficiency of TSA temp.-changing adsorption.3 use three sections of PSA separation processes, successively
Carbon monoxide and hydrogen is then demultiplex out in carbon dioxide removal, can be different according to institute's adsorbing medium, selects different type adsorbent,
It is segmented absorption, adsorption efficiency height, carbon monoxide and hydrogen recovery rate height and purity is guaranteed.
4 present invention process processes are simple, and what is used is commonly used equipment, equipment investment and operating cost is low, stability is good,
It is high reliablity, energy-saving, environmentally friendly.
Detailed description of the invention
Fig. 1 is process flow chart of the invention.
Specific embodiment
Explanation is further explained to the present invention with reference to the accompanying drawing:
Referring to Fig. 1, a kind of raw coke oven gas extracts the process of CO and H2, includes the following steps:
(1) raw coke oven gas is first pre-processed after buffer gas tank: the tar in removing raw coke oven gas is flutterred using electricity, after processing
The concentration of tar is lower than 1mg/Nm3, raw coke oven gas after being pre-processed in raw coke oven gas；
(2) raw coke oven gas after the pretreatment one stage of compression: is subjected to one stage of compression, raw coke oven gas after being pressurizeed, level-one pressure
Contracting outlet pressure 0.3MPa (G)；
(3) TSA benzene-removal naphthalene-removal: it is de- to carry out TSA after being cooled to 15~20 DEG C with water at low temperature heat exchange for raw coke oven gas cooling after pressurization
Benzene takes off naphthalene, obtains raw coke oven gas after benzene-removal naphthalene-removal, and the TSA operating pressure 0.3MPa (G), uses 7 by 15~20 DEG C of operation temperature
DEG C water at low temperature cools down raw coke oven gas.
(4) two-stage compression: raw coke oven gas after the benzene-removal naphthalene-removal is subjected to two-stage compression, obtains raw coke oven gas after two-stage compression；
Two-stage compression outlet pressure 1.6MPa (G).
(5) deoxidation: raw coke oven gas enters deoxidation preheater and is warming up to 150 DEG C or more after the two-stage compression, subsequently into de-
Oxygen slot carries out detoxification deoxygenation, obtains the purified gas of detoxification deoxygenation.
(6) it converts: the purified gas of detoxification deoxygenation being carried out to the conversion reaction of controlling depth, obtains conversion gas；The transformation
The H2O/CO value of reaction is 1.2-1.3, and operation temperature is at 180~240 DEG C；The hot water of by-product is as lithium bromide in shift conversion step
The heat source for process of freezing, lithium bromide refrigerating produce 5-10 DEG C of water at low temperature, and the water at low temperature is used for and the waste coal before TSA benzene-removal naphthalene-removal
Loopback lithium bromide refrigerating process after gas heat exchange is cooling.
(7) desulfurization: the conversion gas being sent into desulfurizing tower and carries out desulfurization, and the conversion gas sulfur-bearing 10 after controlling desulfurization~
50mg/Nm3；The tower bottoms of enrichment sulphur obtains sulfur product by sulfur recovery process；(8)CO2PSA separation: desulfurization will be passed through
Conversion gas afterwards is sent into first segment and carries out CO2PSA separation, pressure-variable adsorption emergence work obtains the conversion gas without CO2.?
In a cycle, adsorption tower is successively undergone: absorption, drop pressure, inverse put, flushing, boost pressure, whole pressurising.It is multiple
The operation of the alternately above each step of adsorption tower, is mutually matched, cooperating, makes package unit even running, realization pair
The removing of the impurity compositions such as CO2.
(9) the PSA separation of CO: the PSA that the conversion gas without CO2 is passed through second segment CO is separated, Pressure Swing Adsorption
CO obtains CO and hydrogen rich gas.Adsorption tower is discharged by inversely bleeding off pressure and vacuumizing mode in qualified CO in adsorption tower, into product
Gas surge tank.Process after a part of CO is sent into after being compressed to 0.5MPa (G) as product gas, a part of CO is through replacing air pressure
For impurity component remaining in displacement sorption tower after contracting machine.Each adsorption tower works alternatively to reach continuous separating-purifying CO's
Purpose.
(10)H2PSA separation: hydrogen rich gas is passed through third section H2PSA separation, obtain H2 and resolution gas.In a cycle
In, every adsorption tower is successively undergone: absorption, drop pressure, along put, inverse put, flushing, boost pressure, whole pressurising step.Every suction
The operation of the alternately above each step of attached tower, is mutually matched, cooperating, makes package unit even running, obtain qualification
H2 product.Obtained resolution gas is partly or entirely used as regenerating medium to be sent into TSA benzene-removal naphthalene-removal process as adsorption tower again
Raw, the stripping gas of naphthalene containing benzene after regeneration is sent into fuel gas pipe network.
Using the above method, can not only reduce that shift conversion step is air-cooled or water cooling energy consumption (if being not used to by-product hot water, only
Air-cooled or water cooling can be used), the hot water of by-product can also be used to produce cold water, cool down for TSA unstripped gas, reduce refrigeration process
Energy consumption.
Claims (6)
1. a kind of raw coke oven gas extracts CO and H2Method, it is characterised in that, by raw coke oven gas through decoking pretreatment, one stage of compression, TSA
Gas is purified after benzene-removal naphthalene-removal, two-stage compression, deoxidation, conversion reaction and desulfurization, the purified gas separates successively through three sections of PSA
Isolate CO2, CO and H2After obtain stripping gas, some or all of described stripping gas is sent into TSA benzene-removal naphthalene-removal as regenerating medium
It is regenerated in process for adsorption tower, the stripping gas of naphthalene containing benzene after regeneration is as fuel pneumatic transmission to out-of-bounds.
2. raw coke oven gas as described in claim 1 extracts CO and H2Method, it is characterised in that, it is secondary in the conversion reaction process
The hot water of production provides heat source for lithium bromide refrigerating, and 5-10 DEG C of water at low temperature of lithium bromide refrigerating output is for cooling down TSA benzene-removal naphthalene-removal
Preceding raw coke oven gas.
3. raw coke oven gas as claimed in claim 1 or 2 extracts CO and H2Method, it is characterised in that, the TSA benzene-removal naphthalene-removal work
In sequence, TSA operating pressure 0.3MPa (G), 15~20 DEG C of operation temperature.
4. raw coke oven gas as claimed in claim 1 or 2 extracts CO and H2Method, which is characterized in that in the deoxidation step, will
Raw coke oven gas pre-heating temperature elevation after two-stage compression carries out deoxidation to 150 DEG C or more again, and the purified gas after deoxidation is first used to preheat two
The compressed raw coke oven gas of grade.
5. raw coke oven gas as claimed in claim 1 or 2 extracts CO and H2Method, it is characterised in that, controlled in the conversion reaction
H2O/CO value is 1.2-1.3, and operation temperature is at 180~240 DEG C.
6. raw coke oven gas as claimed in claim 1 or 2 extracts CO and H2Method, it is characterised in that, three sections of PSA separate work
Sequence includes one section of CO2PSA separation, two sections of CO PSA separation and three sections of H2PSA separation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910328427.7A CN110002402A (en) | 2019-04-23 | 2019-04-23 | Raw coke oven gas extracts CO and H2Method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910328427.7A CN110002402A (en) | 2019-04-23 | 2019-04-23 | Raw coke oven gas extracts CO and H2Method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110002402A true CN110002402A (en) | 2019-07-12 |
Family
ID=67173661
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910328427.7A Pending CN110002402A (en) | 2019-04-23 | 2019-04-23 | Raw coke oven gas extracts CO and H2Method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110002402A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112678773A (en) * | 2020-12-28 | 2021-04-20 | 成都益志科技有限责任公司 | Process for producing hydrogen and coproducing LNG (liquefied Natural gas) by using raw gas |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2388961A1 (en) * | 1999-11-01 | 2001-05-10 | Acetex (Cyprus) Limited | Methanol plant retrofit for manufacture of acetic acid |
| CN102491269A (en) * | 2011-11-14 | 2012-06-13 | 四川同盛科技有限责任公司 | Method for extracting hydrogen gas from coke oven gas |
| CN106621696A (en) * | 2016-12-20 | 2017-05-10 | 上海华林工业气体有限公司 | HYCO synthetic gas separation and purification system with internal waste gas recycling |
| CN108117047A (en) * | 2017-12-22 | 2018-06-05 | 新疆宣力环保能源有限公司 | The low pressure sulfur resistant conversion of raw coke oven gas hydrogen manufacturing and proprietary adsorbent arrange lazy technology |
-
2019
- 2019-04-23 CN CN201910328427.7A patent/CN110002402A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA2388961A1 (en) * | 1999-11-01 | 2001-05-10 | Acetex (Cyprus) Limited | Methanol plant retrofit for manufacture of acetic acid |
| CN102491269A (en) * | 2011-11-14 | 2012-06-13 | 四川同盛科技有限责任公司 | Method for extracting hydrogen gas from coke oven gas |
| CN106621696A (en) * | 2016-12-20 | 2017-05-10 | 上海华林工业气体有限公司 | HYCO synthetic gas separation and purification system with internal waste gas recycling |
| CN108117047A (en) * | 2017-12-22 | 2018-06-05 | 新疆宣力环保能源有限公司 | The low pressure sulfur resistant conversion of raw coke oven gas hydrogen manufacturing and proprietary adsorbent arrange lazy technology |
Non-Patent Citations (5)
| Title |
|---|
| 《化工百科全书》编辑委员会: "《化工百科全书 第18卷》", 30 September 1998, 化学工业出版社, pages: 709 * |
| 上海师范大学，福建师范大学: "《化工基础 上》", 30 June 2000, 高等教育出版社 * |
| 中国炼焦行业协会: "《创新发展中的中国焦化业》", 东北师范大学出版社, pages: 236 - 237 * |
| 戴维 等: "《铁合金工程技术》", 30 June 2015, 冶金工业出版社, pages: 678 * |
| 江萍: "《建筑设备自动化》", 31 January 2016, 中国建材工业出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112678773A (en) * | 2020-12-28 | 2021-04-20 | 成都益志科技有限责任公司 | Process for producing hydrogen and coproducing LNG (liquefied Natural gas) by using raw gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101575540B (en) | Method for producing liquefied natural gas and carbinol simultaneously | |
| CN109999618B (en) | System and method for separating carbon dioxide from medium-high pressure gas source | |
| CN112625761B (en) | Process for removing low-partial pressure acid gas in low-pressure feed gas by using low-temperature methanol | |
| CN102491269A (en) | Method for extracting hydrogen gas from coke oven gas | |
| CN112678773B (en) | Process for producing hydrogen and coproducing LNG (liquefied Natural gas) by using raw gas | |
| CN109294645A (en) | It is a kind of to utilize coke-stove gas synthesis of methanol with joint production LNG, richness H2Device and method | |
| CN104515361A (en) | Method for producing liquid carbon dioxide | |
| CN106479578A (en) | A kind of acid gas removal technique of supporting coal gasification | |
| CN107285279A (en) | A kind of method using the purified synthesis gas of complete warm journey pressure-variable adsorption with separating | |
| CN113264507A (en) | Method for removing hydrogen in hydrogen chloride gas | |
| CN113277471A (en) | Method and device for recovering reduction tail gas in polycrystalline silicon production | |
| CN110228792B (en) | Deep decarburization process for synthesis gas | |
| CN103695043B (en) | Method for drying, purifying and cooling conversion rough synthesized gas and SNG product gas through low-temperature methanol washing and device thereof | |
| CN100384510C (en) | Method for removing sulfides and carbon dioxide by high pressure | |
| CN110002402A (en) | Raw coke oven gas extracts CO and H2Method | |
| CN102876828B (en) | Reducing gas purification process and system matched with gas-based shaft furnace | |
| CN101954233B (en) | Desorbing method and device of absorption rich liquor for absorbing sulfur dioxide by using citrate solution | |
| CN111004082A (en) | System and method for removing carbon dioxide from C2 fraction | |
| CN209940921U (en) | Device for treating low-temperature methanol-washed hydrocarbon-containing exhaust gas | |
| CN112126478B (en) | Regeneration method of TSA (TSA-TSA) tower in device for preparing LNG (liquefied natural gas) from coke oven gas | |
| CN212560126U (en) | Low-temperature methanol washing process device with low energy consumption and high carbon capture rate | |
| CN214243809U (en) | System for producing hydrogen and coproducing LNG (liquefied Natural gas) by using raw gas | |
| CN212316051U (en) | Poly-generation device for producing natural gas by using underground gasified gas | |
| CN211226357U (en) | Device for preparing dry ice and recovering dry ice tail gas to produce food-grade carbon dioxide | |
| CN210410096U (en) | Separation system for carbon dioxide in medium-high pressure gas source |
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 | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190712 |