CN208952531U - A kind of clean gas produces the device of LNG coproduction nitrogen hydrogen, richness CO - Google Patents
A kind of clean gas produces the device of LNG coproduction nitrogen hydrogen, richness CO Download PDFInfo
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- CN208952531U CN208952531U CN201821516094.8U CN201821516094U CN208952531U CN 208952531 U CN208952531 U CN 208952531U CN 201821516094 U CN201821516094 U CN 201821516094U CN 208952531 U CN208952531 U CN 208952531U
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- 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
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- 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
Abstract
The utility model discloses a kind of clean gas production LNG coproduction nitrogen hydrogen, the device of richness CO, including sequentially connected drying unit, absorbing unit, purification unit and separative unit；Drying unit includes drying tower, absorbing unit includes adsorption tower, purification unit includes the purification column being sequentially connected in series and dust filter unit, separative unit is located in ice chest, separative unit includes heat exchanger group, heavy hydrocarbon separator, dehydrogenation rectifying column, scrubbing tower and decarburization rectifying column, it based on clean gas, is dried, removes mercury, removes carbon dioxide, heavy hydrocarbon and dust, finally obtain LPG, hydrogen rich gas gas, richness CO gas and LNG；The utility model solves the problems, such as that heavy hydrocarbon frozen block occurs for ice chest channel, and scrubbing tower is arranged in ice chest, removes CO and methane in hydrogen rich gas.
Description
[technical field]
The utility model belongs to coke oven gas purification processing, liquefaction separation technical field more particularly to a kind of clean gas
Produce the device of LNG coproduction nitrogen hydrogen, richness CO.
[background technique]
Coke-stove gas, also known as oven gas, combustible component is more, belongs to high heating value gas, raw gas or raw coke oven gas.It is that coking is used
Coal in coke oven after high-temperature retorting, output coke and tar product while a kind of generated imflammable gas, be
The byproduct of coking industry.Its main component is hydrogen (55%~60%) and methane (23%~27%), in addition also containing few
Carbon monoxide (5%~8%), the C of amount2The above unsaturated hydrocarbons (2%~4%), carbon dioxide (1.5%~3%), oxygen
(0.3%~0.8%)), nitrogen (3%~7%) and sulfide etc..Wherein hydrogen, methane, carbon monoxide, C2The above unsaturation
Hydrocarbon is combustible component, and carbon dioxide, nitrogen, oxygen are non-combustible component.
Coke-stove gas a part is used to generate electricity at present, and a part is used to produce methanol and hydrogen manufacturing, and it is straight that there are also quite a few
Burning and discharge are connect, capacity usage ratio is about 55%, while wasting precious resources, also causes great dirt to environment
Dye, so, the processing of coke-stove gas is concerned by people.
Meanwhile LNG (liquefied natural gas) be it is a kind of cleaning, the efficient energy.Since imported L NG facilitates energy-consuming state
It realizes energy supply diversification, ensure energy security, and exporting LNG facilitates natural gas producing nation effective exploitation natural gas money
Source increases foreign exchange earnings, promotes national economic development, thus LNG trade is just becoming the new hot spot of global energy markets.
The application of coke-stove gas at present predominantly increases production methane using hydrogen methanol or synthesis ammonia, or using methanation
LNG, two ways otherwise to the economic value utilization rate of methane it is not high or to the utility value of hydrogen it is not high, synthesize ammonia
Conventional production method is that purified coke-stove gas produces LNG, and it is raw that hydrogen rich gas is mixed into certain proportion outside ice chest with nitrogen
Synthesis ammonia, therefore this technique simultaneous hydrogen production gas, CO and LNG are produced, realizes that coke-stove gas economic value maximally utilizes.
[utility model content]
The purpose of the utility model is to provide a kind of clean gas production LNG coproduction nitrogen hydrogen, the device of richness CO, to solve
Clean gas production LNG crosses Cheng Qian, need to carry out film dehydration；Heavy hydrocarbon causes Cold box blocking and freezing during production LNG；Output
It is sent to the problem that nitrogen content is few in the hydrogen rich gas gas of synthesis ammonia.
A kind of clean gas produces the device of LNG coproduction nitrogen hydrogen, richness CO, including sequentially connected drying unit, absorption
Unit, purification unit and separative unit；
Drying unit includes drying tower, and absorbing unit includes adsorption tower, purification unit include the purification column being sequentially connected in series and
Dust filter unit, separative unit are located in ice chest, and separative unit includes heat exchanger group, heavy hydrocarbon separator, dehydrogenation rectifying column, washing
Tower and decarburization rectifying column；
Drying tower is used for based on clean gas, and clean gas is dried, and is removed moisture, is obtained the first processing
Gas, drying tower are connected to adsorption tower by pipeline, and adsorption tower enters from its bottom from bottom to top through activity for the first processing gas
Charcoal removes mercury, obtains second processing gas, and adsorption tower is connected to purification column by pipeline, and purification column is used for second processing gas from its bottom
Portion enters from bottom to top through bed adsorption agent carbon dioxide removal and heavy hydrocarbon, and purification column is connected to dust filter unit by pipeline,
Dust filter unit is used to filter the dust in second processing gas, obtains third processing gas, and dust filter unit is connected by heat exchanger group
It is connected to heavy hydrocarbon separator, heavy hydrocarbon separator is used to obtain gas-liquid mixture and LPG after being separated third processing gas；
Heavy hydrocarbon separator is connected to dehydrogenation rectifying column by secondary heat exchanger group and three-level heat exchanger group, and dehydrogenation rectifying column is used
In gas-liquid mixture is separated into hydrogen rich gas gas and the first treatment fluid, the top and bottom of dehydrogenation rectifying column pass through pipeline respectively
It is connected to scrubbing tower and decarburization rectifying column, the top duct of dehydrogenation rectifying column flows into scrubbing tower, dehydrogenation essence for hydrogen rich gas gas
The bottom pipe for evaporating tower flows into decarburization rectifying column for the first treatment fluid, and scrubbing tower enters removing richness from top for liquid nitrogen
The bottom of methane and CO in hydrogen gas, scrubbing tower is additionally coupled to decarburization rectifying column, decarburization rectifying by three-level heat exchanger group
Tower is used to the remaining liq of the first treatment fluid and inflow decarburization rectifier bottoms being separated into rich CO gas and LNG.
Further, the top of dehydrogenation rectifying column is connected to scrubbing tower by separator, separator be used for hydrogen rich gas into
Row gas-liquid separation.
Further, separator bottom is connected with subcooler by pipeline, and subcooler is for further to hydrogen rich gas gas
Cooling, subcooler is connected to the decarburization rectifying column by three-level heat exchanger group.
The beneficial effects of the utility model are: LPG low temperature extraction in 1, setting purification unit and ice chest, it is logical to solve ice chest
The problem of heavy hydrocarbon frozen block, occurs for road, and the LPG of extraction is sent to the tank field LPG and sells as byproduct, increases added value of product.2, it mixes
It closes refrigeration process and uses the heat exchanger of double cold sources, and carry out cryogenic separation throttling, keep thermal field temperature adjusting feedback sensitiveer,
System energy consumption substantially reduces.3, scrubbing tower is set in ice chest, washes principle according to low temperature liquid nitrogen, passes through low temperature liquid nitrogen and hydrogen rich gas pair
Stream removes CO and methane, and nitrogen content in the hydrogen rich gas of tower top output is high, and only need to be incorporated a small amount of nitrogen i.e. can reach nitrogen hydrogen
Than being used for Ammonia Production after 3:1, compared with outside hydrogen rich gas ice chest with nitrogen, energy consumption is reduced.4. being kept away by setting auxiliary drying tower
Exempt from clean gas production LNG and cross Cheng Qian, carried out film dehydration, and reduced energy consumption, and reduced production cost.
[Detailed description of the invention]
Fig. 1 is the structural schematic diagram of the utility model.
Wherein: 1. drying towers；2. adsorption tower；3. purification column；4. dust filter unit；5. heavy hydrocarbon separator；6. dehydrogenation rectifying
Tower；7. subcooler；8. scrubbing tower；9. decarburization rectifying column；10. three-level heat exchanger group；11. separator；12. first-class heat exchanger group；
13. secondary heat exchanger group.
[specific embodiment]
The utility model is described in detail with reference to the accompanying drawings and detailed description.
The invention also discloses a kind of clean gas production LNG coproduction nitrogen hydrogen, the device of richness CO, as shown in Figure 1,
Including sequentially connected drying unit, absorbing unit, purification unit and separative unit；
Drying unit:
Drying unit includes drying tower 1, and the drying tower 1 of drying unit is used for based on clean gas, to clean gas
It is dried, removes moisture, obtain the first processing gas；Drying tower 1 is connected to adsorption tower 2 by pipeline, and drying unit is by 2
1,1, drying tower, 1,1, auxiliary drying tower heater, 1 cooler, 1 separator 11 and 1 condensate drum composition.When one
During absorption, in addition a drying tower 1 and auxiliary drying tower 1 are being heated and are being cooled down platform drying tower 1, two dryings
1 operated in turn of tower, the adsorption cycle of every drying tower 1 are 8 hours, and the implementation of entire drying process is automatically switched by sequencing valve
Realize continuous operation, the product gas dew point after drying is lower than -70 DEG C.
Absorbing unit:
Absorbing unit includes adsorption tower 2, and the adsorption tower 2 of absorbing unit is connected to drying tower 1 by pipeline, and adsorption tower 2 is used
Enter in the first processing gas from its bottom and remove mercury through active carbon from bottom to top, obtains second processing gas, adsorption tower 2 passes through pipeline
It is connected to purification column 3；Gas is handled from the first of drying process, temperature is 40 DEG C, flow 127000Nm3/ h, from bottom into
Enter adsorption tower 2 from bottom to top through the mercury in active carbon removing the first processing gas, subsequently into purification procedures.
Purification unit:
Purification unit has been sequentially connected in series purification column 3 and dust filter unit 4, and purification column 3 is connected to adsorption tower 2 by pipeline,
Purification column 3 enters from bottom to top from its bottom through bed adsorption agent carbon dioxide removal and heavy hydrocarbon, purifying for second processing gas
Tower 3 is connected to dust filter unit 4 by pipeline, and dust filter unit 4 is used to filter the dust in second processing gas, obtain at third
Qi-regulating, dust filter unit 4 are connected to heavy hydrocarbon separator 5 by heat exchanger group；Second processing gas after absorption process enters
Purification procedures.Purification unit uses " molecular sieve+active carbon " three tower purifying process, using meeting bed adsorption agent in different pressures
Power adsorption capacity at a temperature of has differences and selects the characteristic of absorption, and the carbon dioxide, heavy hydrocarbon in removing unstripped gas are to meet
The requirement of liquefaction separation unit.
Purification unit is by 3 purification columns, 3,1 heaters, 1 cooler, 1 separator 11 and 1 condensate drum group
At.When a purification column 3 is during absorption, in addition two purification columns 3 are being heated and are being cooled down, and three purification columns 3 are taken turns
Stream operation, the adsorption cycle of every purification column 3 are 8 hours, and the automatic switchover for being implemented with sequencing valve of entire drying process is realized
Continuous operation, the product gas dew point after drying are lower than -70 DEG C.
Separative unit:
Separative unit is located in ice chest, and separative unit includes heat exchanger group, heavy hydrocarbon separator 5, dehydrogenation rectifying column 6, washing
Tower 8 and decarburization rectifying column 9, heavy hydrocarbon separator 5 are connected to dust filter unit 4 by first-class heat exchanger group 12, and heavy hydrocarbon separator 5 is used
Gas-liquid mixture and LPG are obtained after being separated third processing gas, heavy hydrocarbon separator 5 also passes through 13 He of secondary heat exchanger group
Three-level heat exchanger group 10 is connected to dehydrogenation rectifying column 6, dehydrogenation rectifying column 6 be used to for gas-liquid mixture being separated into hydrogen rich gas gas and
First treatment fluid, the top and bottom of dehydrogenation rectifying column 6 pass through pipeline respectively and are connected to scrubbing tower 8 and decarburization rectifying column 9, dehydrogenation
The top duct of rectifying column 6 enters scrubbing tower 8 for hydrogen rich gas gas, and the bottom pipe of dehydrogenation rectifying column 6 is for the first processing
Liquid stream enters decarburization rectifying column 9, and scrubbing tower 8 enters methane and CO in removing hydrogen rich gas gas from top for liquid nitrogen, takes off
Carbon rectifying column 9 be used for by the first treatment fluid and enter 9 bottom of decarburization rectifying column remaining liq be separated into rich CO gas and
LNG。
Third processing gas enters ice chest, is cooled to -55 DEG C by first-class heat exchanger group 12, into heavy hydrocarbon separator 5, obtains
To LPG and gas-liquid mixture, 5 bottom of heavy hydrocarbon separator produces LPG and sends out ice chest, and gas-liquid mixture enters secondary heat exchanger group 13
Continue to cool down, enters dehydrogenation rectifying column 6 after the cooling of heat exchanger group.
The top of dehydrogenation rectifying column 6 is connected to scrubbing tower 8 by separator 11, and separator 11 is for carrying out gas to hydrogen rich gas
Liquid separation, hydrogen rich gas gas are that the gaseous fluid based on hydrogen comes out at the top of dehydrogenation rectifying column 6, are carried out into separator 11
Gas-liquid separation processing, the gas isolated enter scrubbing tower 8, and the bottom of scrubbing tower 8 is additionally coupled to by three-level heat exchanger group 10
Decarburization rectifying column 9, the liquid isolated enter decarburization rectifying column 9, separation after subcooler 7 and three-level heat exchanger group 10 cool down
11 bottom of device is connected with subcooler 7 by pipeline, and for subcooler 7 for further cooling down to hydrogen rich gas gas, subcooler 7 passes through three
Grade heat exchanger group 10 is connected to decarburization rectifying column 9, and the first treatment fluid is directly entered decarburization rectifying column 9, after separator 11 separates
Liquid flows into decarburization rectifying column 9 after subcooler 7 and three-level heat exchanger group 10 cool down, and is exchanged by caloic, constantly by concentrate
It is produced after being higher than 90% to LNG purity from 9 tower bottom of decarburization rectifying column, finally through supercooling, becomes supercooling LNG product and be sent to LNG
Storage tank, throttling generates the liquid product of atmospheric low-temperature at the top of LNG storage tank.
Medium pressure nitrogen gas enters the top of scrubbing tower 8 after the cooling of heat exchanger group, liquid nitrogen in scrubbing tower 8 from tower top with
Unstripped gas from tower bottom comes into full contact with, and exchanges in tower through caloic, by hydrogen rich gas gas methane and carbon monoxide remove
To 1ppm hereinafter, then the cooling box after heat exchanger group rewarming, the interior setting scrubbing tower 8 of ice chest are washed principle according to low temperature liquid nitrogen, led to
It crosses low temperature liquid nitrogen and hydrogen rich gas convection current to remove CO and methane, nitrogen content in the hydrogen rich gas of tower top output is high, only needs to be incorporated
A small amount of nitrogen is used for Ammonia Production after can reach nitrogen hydrogen ratio 3:1, and compared with outside hydrogen rich gas ice chest with nitrogen, energy consumption is reduced.
First treatment fluid flows directly into decarburization rectifying column 9, and the liquid after separator 11 separates passes through subcooler 7 and three-level
Heat exchanger group 10 enters decarburization rectifying column 9 after cooling down, in decarburization rectifying column 9, the rich carbon monoxide gas being discharged from tower top, through changing
Go out battery limit (BL), LNG product out-of-bounds after heat exchanger group is cooled to -162 DEG C of 9 tower bottom of decarburization rectifying column extraction after hot device group rewarming
Area.
The workflow of the utility model is made of following steps:
A. based on clean gas, clean gas is dried, moisture is removed, obtains the first processing gas；
B. mercury in the first processing gas is removed, second processing gas is obtained；
C. carbon dioxide, heavy hydrocarbon and the dust in second processing gas are removed, third processing gas is obtained；The dew of third processing gas
< -65 degrees Celsius of temperature of point, CO20.01 μ g/m of content < 50ppm, mercury <3, heavy hydrocarbons content reduction；
D. LPG and gas-liquid mixture are obtained through heavy hydrocarbon separator 5 after the cooling of first-class heat exchanger group 12 to third processing gas,
The qualified coal gas of purification enters ice chest, successively passes through first-class heat exchanger group 12, and it is logical to solve ice chest for LPG low temperature extraction in ice chest
The problem of heavy hydrocarbon frozen block, occurs for road, and the LPG of extraction is sent to the tank field LPG and sells as byproduct, increases added value of product, at this time
Most methane and part carbon monoxide and a small amount of nitrogen in unstripped gas become liquid and obtain gas-liquid mixture；
E. hydrogen rich gas gas and the first treatment fluid are obtained by Dehydroepiandrosterone derivative to after gas-liquid mixture cooling；Gas-liquid mixture
Hydrogen rich gas gas and the first treatment fluid are obtained after the separation of dehydrogenation rectifying column 6, hydrogen rich gas gas is the gaseous state based on hydrogen
Fluid comes out at the top of dehydrogenation rectifying column 6, carries out gas-liquid separation processing into separator 11, the gas isolated enters scrubbing tower
8, the liquid isolated enters decarburization rectifying column 9 after subcooler 7 and three-level heat exchanger group 10 cool down；
F. using liquid nitrogen in scrubbing tower 8 in hydrogen rich gas gas methane and CO remove, obtain methane and
CO content be lower than 1ppm nitrogen hydrogen gas, after scrubbing with liquid nitrogen by hydrogen rich gas gas CO and methane deviate from, then
Hydrogen rich gas gas successively returns to heat exchanger group re-heat from scrubbing tower 8, and last cooling box is sent to chemical fertilizer factory as production synthesis ammonia
Raw material.
Liquid carbonization treatment after separating to the first treatment fluid and separator 11 obtains rich CO gas and LNG, at first
Reason liquid is directly entered decarburization rectifying column 9, and the liquid after the separation of separator 11 is after subcooler 7 and three-level heat exchanger group 10 cool down
It into decarburization rectifying column 9, is exchanged by caloic, is constantly higher than after 90% by concentrate to LNG purity and is adopted from 9 tower bottom of decarburization rectifying column
Out, finally become supercooling LNG product through supercooling and be sent to LNG storage tank, throttling generates the liquid of atmospheric low-temperature at the top of LNG storage tank
Body product.
The tail gas come out at the top of decarburization rectifying column 9 has nitrogen, hydrogen and trace methane referred to as based on carbon monoxide
Rich carbon monoxide gas successively returns to the re-heat of heat exchanger group, finally sends out ice chest, obtain rich carbon monoxide gas product.
The cooling step of step d and e carry out cryogenic separation throttling using the twin-channel heat exchanger group of double cold sources, make temperature
Field temperature adjusting feedback is sensitiveer, and system energy consumption substantially reduces, and heat exchanger is plate-fin heat exchanger, and heat exchanger group includes successively going here and there
First-class heat exchanger group 12, secondary heat exchanger group 13 and the three-level heat exchanger group 10 of connection, first-class heat exchanger group 12, secondary heat exchanger group
13 and the number of heat exchanger of three-level heat exchanger group 10 be respectively 8,8 and 4, double cold sources are that liquid phase cold source and gas phase are cold
Source, liquid phase cold source and gas phase cold source are made of nitrogen, methane, ethylene, propane and isopentane, and nitrogen content of liquid phase cold source is
10-15%, methane content 35-45%, ethylene contents 20-25%, propane content 8-15%, isopentane content be
10-20%, nitrogen content as preferred liquid phase cold source is 12.3%, methane content 40.9%, ethylene contents are
18.4%, propane content 12.6%, isopentane content be 15.8%, although the constituent of liquid phase cold source and gas phase cold source
Unanimously, but the state of the cold source in two channels is inconsistent, and the cold source in liquid phase cold source channel is liquid phase, gas phase cold source channel
Interior cold source is gas phase, and the state in two channels can gradually change with the variation of temperature.
Liquid phase cold source enters main heat exchanger, is cooled to -55 DEG C, after throttle valve throttles, provides cooling capacity for heat exchanger；Gas
Phase cold source enters ice chest, successively after first-class heat exchanger group 12, secondary heat exchanger group 13 cool down, send to 9 tower bottom of decarburization rectifying column
Boiling hot amount again is provided, then is cooled to -160 DEG C through three-level heat exchanger group 10, after throttle valve throttles, successively returns to main heat exchanger
Cooling capacity is provided for it, goes out battery limit (BL) after abundant rewarming.
The top of dehydrogenation rectifying column 6,9 top of decarburization rectifying column condenser need temperature very low, therefore use nitrogen for
It provides necessary low temperature cooling capacity, and nitrogen enters ice chest, after three-level heat exchanger group 10 and subcooler 7 exchange heat, temperature is down to-
180 DEG C, respectively after throttling, the condenser respectively at the top of dehydrogenation rectifying column 6, at the top of decarburization rectifying column 9 provides cooling capacity, and
After pass sequentially through cooling box after subcooler 7, main heat exchanger, abundant rewarming.
Claims (3)
1. the device of a kind of clean gas production LNG coproduction nitrogen hydrogen, richness CO, which is characterized in that including sequentially connected drying
Unit, absorbing unit, purification unit and separative unit；
The drying unit includes drying tower (1), and the absorbing unit includes adsorption tower (2), and the purification unit includes successively
Concatenated purification column (3) and dust filter unit (4), the separative unit are located in ice chest, and the separative unit includes heat exchanger
Group, heavy hydrocarbon separator (5), dehydrogenation rectifying column (6), scrubbing tower (8) and decarburization rectifying column (9)；
The drying tower (1) is used for based on clean gas, and clean gas is dried, and removes moisture, obtains at first
Qi-regulating, the drying tower (1) are connected to the adsorption tower (2) by pipeline, and the adsorption tower (2) is for the first processing gas
Enter from its bottom and remove mercury through active carbon from bottom to top, obtains second processing gas, the adsorption tower (2) is connected to by pipeline
The purification column (3), the purification column (3) enter from its bottom from bottom to top through bed adsorption agent for the second processing gas
Carbon dioxide removal and heavy hydrocarbon, the purification column (3) are connected to the dust filter unit (4), the dust-filtering by pipeline
Device (4) is used to filter the dust in the second processing gas, obtains third processing gas, and the dust filter unit (4) passes through heat exchange
Device group is connected to the heavy hydrocarbon separator (5), and the heavy hydrocarbon separator (5) is used to after being separated third processing gas obtain
To gas-liquid mixture and LPG；
The heavy hydrocarbon separator (5) is connected to the dehydrogenation rectifying by secondary heat exchanger group (13) and three-level heat exchanger group (10)
Tower (6), the dehydrogenation rectifying column (6) is used to the gas-liquid mixture being separated into hydrogen rich gas gas and the first treatment fluid, described
The top and bottom of dehydrogenation rectifying column (6) pass through pipeline respectively and are connected to the scrubbing tower (8) and the decarburization rectifying column (9),
The top duct of the dehydrogenation rectifying column (6) flows into the scrubbing tower (8), the dehydrogenation rectifying column for the hydrogen rich gas gas
(6) bottom pipe flows into the decarburization rectifying column (9) for first treatment fluid, and the scrubbing tower (8) is used for liquid nitrogen
Gas enters the methane and CO removed in the hydrogen rich gas gas from top, and the bottom of the scrubbing tower (8) is changed by the three-level
Hot device group (10) is additionally coupled to the decarburization rectifying column (9), the decarburization rectifying column (9) be used for first treatment fluid and
The remaining liq for flowing into decarburization rectifying column (9) bottom is separated into rich CO gas and LNG.
2. the device of a kind of clean gas production LNG coproduction nitrogen hydrogen according to claim 1, richness CO, which is characterized in that
The top of the dehydrogenation rectifying column (6) is connected to the scrubbing tower (8) by separator (11), the separator (11) for pair
Hydrogen rich gas carries out gas-liquid separation.
3. the device of a kind of clean gas production LNG coproduction nitrogen hydrogen according to claim 1, richness CO, which is characterized in that
Separator (11) bottom is connected with subcooler (7) by pipeline, and the subcooler (7) is for further to hydrogen rich gas gas
Cooling, the subcooler (7) is connected to the decarburization rectifying column (9) by the three-level heat exchanger group (10).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109099642A (en) * | 2018-09-17 | 2018-12-28 | 陕西黑猫焦化股份有限公司 | A kind of clean gas produces the method and device of LNG coproduction nitrogen hydrogen, richness CO |
| CN114276846A (en) * | 2021-12-16 | 2022-04-05 | 陕西黑猫焦化股份有限公司 | Method and system for preparing LNG (liquefied Natural gas) and coproducing synthetic ammonia by using coke oven gas |
-
2018
- 2018-09-17 CN CN201821516094.8U patent/CN208952531U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109099642A (en) * | 2018-09-17 | 2018-12-28 | 陕西黑猫焦化股份有限公司 | A kind of clean gas produces the method and device of LNG coproduction nitrogen hydrogen, richness CO |
| CN114276846A (en) * | 2021-12-16 | 2022-04-05 | 陕西黑猫焦化股份有限公司 | Method and system for preparing LNG (liquefied Natural gas) and coproducing synthetic ammonia by using coke oven gas |
| CN114276846B (en) * | 2021-12-16 | 2023-11-07 | 陕西黑猫焦化股份有限公司 | Method and system for preparing LNG and co-producing synthetic ammonia by using coke oven gas |
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