CN214361201U - Device for preparing synthetic ammonia raw material and LNG (liquefied natural gas) from coke oven gas - Google Patents
Device for preparing synthetic ammonia raw material and LNG (liquefied natural gas) from coke oven gas Download PDFInfo
- Publication number
- CN214361201U CN214361201U CN202120723284.2U CN202120723284U CN214361201U CN 214361201 U CN214361201 U CN 214361201U CN 202120723284 U CN202120723284 U CN 202120723284U CN 214361201 U CN214361201 U CN 214361201U
- Authority
- CN
- China
- Prior art keywords
- pipeline
- heat exchanger
- lng
- communicated
- nitrogen
- 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
Images
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model discloses a device of synthetic ammonia raw materials and LNG is prepared to coke oven gas relates to coke oven gas treatment facility field, including pipeline, heat exchanger, separator, take off CO tower and LNG rectifying column to be equipped with gas treatment pipeline, first nitrogen gas treatment pipeline, second nitrogen gas treatment pipeline, synthetic ammonia raw materials pipeline and methane synthesis pipeline. Through the utility model discloses a setting draws out nitrogen hydrogen in with coke oven gas to adjust the raw materials of hydrogen nitrogen ratio as synthetic ammonia system through the benefit nitrogen, prepare LNG with the methane separation in the coke oven gas simultaneously, follow and take off CO tower and produce behind the rich CO liquid rewarming inflation and methane rectifying column T2 top rich CO gas and join the back and provide cold volume, rewarming to the normal atmospheric temperature after and deliver to fuel gas pipe network, this system operation is simple, the energy consumption is low, can be with coke oven gas make full use of, economic benefits is good.
Description
Technical Field
The utility model relates to a coke oven gas treatment facility technical field especially relates to a device of synthetic ammonia raw materials and LNG is prepared to coke oven gas.
Background
China is a large country for coke production, the yield accounts for more than half of the total world production, coke by-products are mainly coke oven gas, the coke yield in 2015 is 4.5 hundred million t, the total coke oven gas yield is about 1900 hundred million m3, and the total amount of the coke oven gas is 1.5 times (590 hundred million m3) of the total gas output of the western gas east in 2015 except for 50 percent of furnace return. At present, the utilization of coke oven gas is mainly divided into two aspects of civil use and industrial use. The fuel is mainly used as resident fuel gas in civil use; the industrial application field is that the steel and iron united enterprises use coke oven gas as fuel in the processes of steel making, sintering, steel rolling and the like, the coke oven gas is sent to a power plant as fuel for power generation, and the coke oven gas is deeply processed to produce chemical products with higher added value, such as methanol, synthetic ammonia, hydrogen, natural gas and the like. The coke oven gas is a coking byproduct, mainly comprises H2, N2/CH4, CO and CO2, and is a good chemical raw material and a high-calorific-value fuel. But the impurities (such as sulfur, tar, benzene, naphthalene, ammonia, HCN and the like in various forms) contained in the coke oven gas are various in types and complex in components, so that the application range of the coke oven gas is seriously influenced, the comprehensive utilization of the coke oven gas and the diversification of downstream products are realized, the environment is fundamentally controlled, and the inevitable choice of the trouble of coking enterprises is solved. The coke oven gas-to-natural gas project obtains pure environment-friendly energy through uniformly collecting and purifying the coke oven gas generated by a coke-oven plant, thereby prolonging the transportation radius of the natural gas, meeting the requirements of natural gas in remote places, reducing carbon emission and protecting the environment. The coke oven gas also contains a large amount of hydrogen and nitrogen, and the hydrogen and nitrogen ratio can be adjusted after purification treatment and nitrogen supplement to be used as a raw material for synthesizing ammonia. In order to improve the utilization rate of the coke oven gas, various coke oven gas synthetic natural gas devices are proposed in the prior art, but the coke oven gas synthetic natural gas device in the prior art is complex in operation, high in energy consumption and low in utilization rate of the coke oven gas.
Therefore, a device for preparing synthetic ammonia raw materials and LNG by using coke oven gas is provided.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the defects in the prior art and provides a device for preparing synthetic ammonia raw material and LNG from coke oven gas.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a device for preparing synthetic ammonia raw material and LNG by coke oven gas comprises a pipeline, a heat exchanger, a separator, a CO removal tower and an LNG rectifying tower, and is characterized in that,
a gas treatment pipeline: the gas treatment pipeline is communicated with the separator after passing through the primary heat exchanger and the secondary heat exchanger, and is respectively communicated with the LNG rectifying tower and the CO removal tower through a separator outlet pipeline, and a tertiary heat exchanger is arranged between the separator and the CO removal tower;
first nitrogen treatment line: the first nitrogen treatment pipeline is communicated with the CO removal tower through a primary heat exchanger, a secondary heat exchanger and a tertiary heat exchanger;
the second nitrogen gas treatment pipeline: the head end of the second nitrogen gas treatment pipeline is communicated with the nitrogen compressor and then communicated with the LNG rectifying tower through the first-stage heat exchanger, the second-stage heat exchanger and the third-stage heat exchanger
Synthetic ammonia raw material pipeline: the top of the CO removal tower is provided with a synthetic ammonia raw material pipeline which is communicated with a synthetic ammonia device after passing through a third-stage heat exchanger, a second-stage heat exchanger and a first-stage heat exchanger;
a methane synthesis pipeline: the bottom of the CO removal tower is provided with a methane synthesis pipeline which is communicated with the LNG rectifying tower through a tertiary heat exchanger and a secondary heat exchanger, the bottom of the LNG rectifying tower is provided with a condensing device, and the methane synthesis pipeline at the condensing device at the bottom of the LNG rectifying tower is communicated with the LNG tank through the secondary heat exchanger.
Further, the separator comprises an inlet and two outlets, wherein the outlets are respectively communicated with a lower pipeline and an upper pipeline, the upper pipeline releases a gas phase, and the lower pipeline releases a liquid phase.
Furthermore, the CO removal tower comprises two inlets and three outlets, wherein the inlets are respectively communicated with the nitrogen processing pipeline and the coal gas processing pipeline, and the outlets are respectively a nitrogen-hydrogen pipeline at the upper part, a CO-rich liquid pipeline at the lower part and a methane-rich liquid pipeline at the bottom.
Further, a condensing device is arranged at the bottom of the LNG rectifying tower, the LNG rectifying tower comprises three inlets and three outlets, wherein the inlets are respectively communicated with a gas treatment pipeline, a nitrogen treatment pipeline and a methane synthesis pipeline; and an outlet is respectively communicated with a CO-rich gas pipeline at the top, a nitrogen reflux pipeline at the upper part and an LNG collecting pipeline at the bottom, and the LNG collecting pipeline is communicated with the LNG tank through a condensing device.
Furthermore, the CO-rich liquid pipeline is communicated with a turboexpander after passing through a third-stage heat exchanger and a second-stage heat exchanger, and an outlet pipeline of the turboexpander is communicated with a fuel gas pipe network through the second-stage heat exchanger and the first-stage heat exchanger.
Furthermore, the CO-rich gas pipeline is communicated with a fuel gas pipe network through a secondary heat exchanger and a primary heat exchanger.
Furthermore, the nitrogen reflux pipeline is communicated with a nitrogen compressor after passing through the secondary heat exchanger and the primary heat exchanger.
Furthermore, mixed refrigerant is arranged in the condensing device and supplied by the refrigerant compressor, an outlet pipeline of the refrigerant compressor is communicated with the condensing device after passing through the first-stage heat exchanger, and the mixed refrigerant discharged by the condensing device flows back to the refrigerant compressor after passing through the second-stage heat exchanger and the first-stage heat exchanger through pipelines.
Compared with the prior art, the beneficial effects of the utility model reside in that:
through the utility model discloses a setting is drawed out nitrogen hydrogen in the coke oven gas to adjust the raw materials of hydrogen nitrogen ratio as synthetic ammonia system through the benefit nitrogen, prepare LNG with the methane separation in the coke oven gas simultaneously, follow and take off CO tower and produce the rich CO liquid and expand after rewarming and provide cold volume after converging with the rich CO gas at methane rectifying column T2 top, send to the fuel gas pipe network after rewarming to the normal atmospheric temperature. The system is simple to operate, low in energy consumption, capable of fully utilizing the coke oven gas and good in economic benefit.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention, and together with the description serve to explain the invention and not to limit the invention.
FIG. 1 is a schematic view of the piping arrangement of a device for producing synthetic ammonia raw material and LNG from coke oven gas according to the present invention.
In the figure: c1-refrigerant compressor; C2-Nitrogen compressor; EX 1-primary heat exchanger; EX 2-secondary heat exchanger; EX 3-three stage heat exchanger; v1-separator; T1-CO removal tower; T2-LNG rectification column; TU 1-turboexpander.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "front", "rear", "left", "right", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention.
With reference to figure 1 of the drawings,
a device for preparing synthetic ammonia raw material and LNG by coke oven gas, which comprises a nitrogen compressor C2, a pipeline, a heat exchanger, a separator V1, a CO removal tower T1 and an LNG rectifying tower,
the nitrogen compressor C2 is provided with an outlet and an inlet,
the separator V1 includes an inlet and two outlets, wherein the outlets are respectively communicated with a lower pipe (lower outlet) and an upper pipe (upper outlet), the upper pipe releases a gas phase, and the lower pipe releases a liquid phase;
the bottom of the LNG rectifying tower is provided with a condensing device, the LNG rectifying tower comprises three inlets and three outlets, wherein the inlets are respectively communicated with a gas treatment pipeline (a middle inlet), a nitrogen treatment pipeline (an upper inlet) and a methane synthesis pipeline (a lower inlet); the outlet is respectively communicated with a CO-rich gas pipeline (top outlet) at the top, a nitrogen reflux pipeline (upper outlet) at the upper part and an LNG collection pipeline (bottom outlet) at the bottom, and the LNG collection pipeline is communicated with an LNG tank through a condensing device;
the CO removal tower T1 comprises two inlets and three outlets, wherein the inlets are respectively communicated with a nitrogen processing pipeline (an upper inlet) and a coal gas processing pipeline (a lower inlet), and the outlets are respectively a nitrogen-hydrogen pipeline at the upper part (an upper outlet), a CO-rich liquid pipeline at the lower part (a lower outlet) and a methane-rich liquid pipeline at the bottom (a bottom outlet);
a gas treatment pipeline: the pipeline is communicated with a separator V1 after passing through a first-stage heat exchanger EX1 and a second-stage heat exchanger EX2, two pipelines are respectively arranged by the separator V1, the lower pipeline is communicated with an LNG rectifying tower, and the upper pipeline is communicated with a CO removal tower T1 through a third-stage heat exchanger EX 3;
first nitrogen treatment line: the pipeline is communicated with a CO removal tower T1 after passing through a primary heat exchanger EX1, a secondary heat exchanger EX2 and a tertiary heat exchanger EX 3;
the second nitrogen gas treatment pipeline: the head end of the pipeline is communicated with a nitrogen compressor C2 and then communicated with an LNG rectifying tower through a first-stage heat exchanger EX1, a second-stage heat exchanger EX2 and a third-stage heat exchanger EX3
Synthetic ammonia raw material pipeline: the top of the CO removal tower T1 is provided with a pipeline which is communicated with the synthetic ammonia device after passing through a three-stage heat exchanger EX3, a two-stage heat exchanger EX2 and a first-stage heat exchanger EX 1;
a methane synthesis pipeline: the bottom of the CO removal tower T1 is provided with a pipeline which is communicated with the LNG rectifying tower through a third-stage heat exchanger EX3 and a second-stage heat exchanger EX2, the bottom of the LNG rectifying tower is provided with a condensing device, and the condensing device at the bottom of the LNG rectifying tower is provided with a pipeline which is communicated with an LNG tank through a second-stage heat exchanger EX 2;
the CO-rich liquid pipeline is communicated with a turboexpander TU1 after passing through a third-stage heat exchanger EX3 and a second-stage heat exchanger EX2, and an outlet pipeline of the turboexpander TU1 is communicated with a fuel gas pipe network through a second-stage heat exchanger EX2 and a first-stage heat exchanger EX 1; the CO-rich gas pipeline is communicated with a fuel gas pipe network through a secondary heat exchanger EX2 and a primary heat exchanger EX 1;
the nitrogen reflux pipeline is communicated with a nitrogen compressor C2 after passing through a secondary heat exchanger EX2 and a primary heat exchanger EX 1;
mixed refrigerant is arranged in the condensing device and is supplied by a refrigerant compressor C1, an outlet pipeline of the refrigerant compressor C1 is communicated with the condensing device after passing through a primary heat exchanger EX1, and the mixed refrigerant discharged by the condensing device flows back to the refrigerant compressor C1 after passing through a secondary heat exchanger EX2 and a primary heat exchanger EX1 by pipelines;
wherein, the CO removing tower T1 and the LNG rectifying tower T2 can be a packed tower, a plate tower and a sieve plate tower; the turbo-expander can adopt an oil bearing turbo-expander and a gas bearing expander.
The utility model discloses a theory of operation and use flow:
the pipeline of the coke oven gas is communicated with the inlet of the separator V1 after passing through the primary heat exchanger EX1 and the secondary heat exchanger EX2, the gas and the liquid phases formed after the temperature of the gas is reduced enter the separator V1 for gas and liquid separation,
the gas phase is communicated with the lower inlet of a CO removal tower T1 through an upper outlet pipeline of a separator V1 and a three-stage heat exchanger EX3,
the liquid phase is communicated with an inlet in the LNG rectifying tower through a lower outlet pipeline of the separator V1;
an upper inlet of the CO removal tower T1 receives nitrogen in a medium-pressure nitrogen pipe network, wherein the nitrogen in the medium-pressure nitrogen pipe network is cooled into liquid through a first-stage heat exchanger EX1, a second-stage heat exchanger EX2 and a third-stage heat exchanger EX3 after passing through a regulating valve, the liquid enters the CO removal tower T1, the liquid and the gas phase of the liquid nitrogen are mixed, methane-rich liquid, CO-rich liquid and nitrogen and hydrogen are produced at the bottom of the CO removal tower T1,
the nitrogen and hydrogen are discharged through an outlet pipeline on a CO removal tower T1 and are sent to an ammonia synthesis device as raw materials after being provided with cold energy by a tertiary heat exchanger EX3, a secondary heat exchanger EX2 and a primary heat exchanger EX1,
the CO-rich liquid is discharged from an outlet pipeline below a CO removal tower T1, enters a turbine expander TU1 for expansion and temperature reduction after being reheated by a three-stage heat exchanger EX3 and a two-stage heat exchanger EX2, is converged with the CO-rich gas discharged from the top outlet of the LNG rectifying tower, returns to a first-stage heat exchanger EX1 and a two-stage heat exchanger EX2 for providing cold energy, is reheated to normal temperature and then is sent to a fuel gas pipe network,
the methane-rich liquid is decompressed from a bottom outlet of a CO removal tower T1, reheated by a tertiary heat exchanger EX3 and a secondary heat exchanger EX2 and then enters an LNG rectifying tower through a lower inlet of the LNG rectifying tower;
the upper inlet of the LNG rectifying tower receives nitrogen in a nitrogen compressor C2, the nitrogen is compressed by the nitrogen compressor C2 and then enters a first-stage heat exchanger EX1, a second-stage heat exchanger EX2 and a third-stage heat exchanger EX3 to be cooled into liquid, the liquid enters a condenser at the top of the LNG rectifying tower to provide cold energy required by the top of the tower, the liquid returns to the third-stage heat exchanger EX3, the second-stage heat exchanger EX2 and the first-stage heat exchanger EX1 through the upper outlet of the LNG rectifying tower to be reheated to normal temperature and returns to the inlet of the compressor,
the middle inlet of the LNG rectifying tower receives the liquid phase part separated from the coke oven gas,
the lower inlet of the LNG fractionating tower receives methane-rich liquid,
condensed methane liquid discharged from the bottom pipeline of the LNG rectifying tower is subcooled by a secondary heat exchanger EX2 and then sent to an LNG storage tank,
the condensing device is arranged at the bottom of the LNG rectifying tower, mixed refrigerant is arranged in the condensing device and supplied by a refrigerant compressor C1, an outlet pipeline of the refrigerant compressor C1 is communicated with the condensing device after passing through a primary heat exchanger EX1, and the mixed refrigerant discharged by the condensing device flows back to the refrigerant compressor C1 after passing through a secondary heat exchanger EX2 and a primary heat exchanger EX1 by pipelines.
The above, only be the concrete implementation of the preferred embodiment of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, the concept of which is equivalent to replace or change, should be covered within the protection scope of the present invention.
Claims (8)
1. A device for preparing synthetic ammonia raw material and LNG by coke oven gas comprises a pipeline, a heat exchanger, a separator, a CO removal tower and an LNG rectifying tower, and is characterized in that,
a gas treatment pipeline: the gas treatment pipeline is communicated with the separator after passing through the primary heat exchanger and the secondary heat exchanger, and is respectively communicated with the LNG rectifying tower and the CO removal tower through a separator outlet pipeline, and a tertiary heat exchanger is arranged between the separator and the CO removal tower;
first nitrogen treatment line: the first nitrogen treatment pipeline is communicated with the CO removal tower through a primary heat exchanger, a secondary heat exchanger and a tertiary heat exchanger;
the second nitrogen gas treatment pipeline: the head end of the second nitrogen gas treatment pipeline is communicated with the nitrogen compressor and then communicated with the LNG rectifying tower through the first-stage heat exchanger, the second-stage heat exchanger and the third-stage heat exchanger
Synthetic ammonia raw material pipeline: the top of the CO removal tower is provided with a synthetic ammonia raw material pipeline which is communicated with a synthetic ammonia device after passing through a third-stage heat exchanger, a second-stage heat exchanger and a first-stage heat exchanger;
a methane synthesis pipeline: the bottom of the CO removal tower is provided with a methane synthesis pipeline which is communicated with the LNG rectifying tower through a tertiary heat exchanger and a secondary heat exchanger, the bottom of the LNG rectifying tower is provided with a condensing device, and the methane synthesis pipeline at the condensing device at the bottom of the LNG rectifying tower is communicated with the LNG tank through the secondary heat exchanger.
2. The apparatus of claim 1, wherein the separator comprises an inlet and two outlets, wherein the outlets are respectively provided with a lower pipeline and an upper pipeline, the upper pipeline releases the gas phase, and the lower pipeline releases the liquid phase.
3. The apparatus of claim 1, wherein the CO removal column comprises two inlets and three outlets, wherein the inlets are respectively communicated with the nitrogen treatment pipeline and the gas treatment pipeline, and the outlets are respectively an upper nitrogen-hydrogen pipeline, a lower CO-rich liquid pipeline and a bottom methane-rich liquid pipeline.
4. The device for preparing the synthetic ammonia raw material and the LNG from the coke oven gas as claimed in claim 1, wherein a condensing device is arranged at the bottom of the LNG rectifying tower, the LNG rectifying tower comprises three inlets and three outlets, wherein the inlets are respectively communicated with a gas treatment pipeline, a nitrogen treatment pipeline and a methane synthesis pipeline; and an outlet is respectively communicated with a CO-rich gas pipeline at the top, a nitrogen reflux pipeline at the upper part and an LNG collecting pipeline at the bottom, and the LNG collecting pipeline is communicated with the LNG tank through a condensing device.
5. The device for preparing the synthetic ammonia raw material and the LNG from the coke oven gas according to claim 3, wherein the CO-rich liquid pipeline is communicated with a turbo expander after passing through a third-stage heat exchanger and a second-stage heat exchanger, and an outlet pipeline of the turbo expander is communicated with a fuel gas pipe network through the second-stage heat exchanger and a first-stage heat exchanger.
6. The device for preparing the synthetic ammonia raw material and the LNG from the coke oven gas as claimed in claim 4, wherein the CO-rich gas pipeline is communicated with a fuel gas pipe network through a secondary heat exchanger and a primary heat exchanger.
7. The device for preparing the synthetic ammonia raw material and the LNG from the coke oven gas as claimed in claim 4, wherein the nitrogen return pipeline is communicated with a nitrogen compressor after passing through the secondary heat exchanger and the primary heat exchanger.
8. The device for preparing the synthetic ammonia raw material and the LNG from the coke oven gas as claimed in claim 1, wherein a mixed refrigerant is arranged in the condensing device, the mixed refrigerant is supplied by a refrigerant compressor, an outlet pipeline of the refrigerant compressor is communicated with the condensing device after passing through the primary heat exchanger, and the mixed refrigerant discharged by the condensing device flows back to the refrigerant compressor after passing through the secondary heat exchanger and the primary heat exchanger through pipelines.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120723284.2U CN214361201U (en) | 2021-04-09 | 2021-04-09 | Device for preparing synthetic ammonia raw material and LNG (liquefied natural gas) from coke oven gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120723284.2U CN214361201U (en) | 2021-04-09 | 2021-04-09 | Device for preparing synthetic ammonia raw material and LNG (liquefied natural gas) from coke oven gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214361201U true CN214361201U (en) | 2021-10-08 |
Family
ID=77974261
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120723284.2U Active CN214361201U (en) | 2021-04-09 | 2021-04-09 | Device for preparing synthetic ammonia raw material and LNG (liquefied natural gas) from coke oven gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214361201U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
-
2021
- 2021-04-09 CN CN202120723284.2U patent/CN214361201U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101968298B (en) | Separation and recovery device and method for argon and methane in synthetic ammonia relief gas | |
| CN108795508B (en) | Method for separating coke oven gas by utilizing expansion refrigeration of nitrogen and helium | |
| CN107328166B (en) | Double-circulation CO cryogenic separation system and separation method thereof | |
| CN102942972B (en) | Method for producing liquefied natural gas by coke oven gas | |
| CN113865263B (en) | Production system for extracting crude helium and co-producing liquefied natural gas by natural gas | |
| CN110762392A (en) | Device for producing LNG (liquefied Natural gas) and CNG (compressed Natural gas) by separating methane in coal-to-synthesis gas through double refrigeration cycles | |
| CN214361201U (en) | Device for preparing synthetic ammonia raw material and LNG (liquefied natural gas) from coke oven gas | |
| CN210625119U (en) | CO cryogenic separation system capable of reducing nitrogen circulation energy consumption | |
| CN107082736B (en) | Liquefied natural gas light hydrocarbon recovery method | |
| CN114111217B (en) | Device and method for preparing LNG and synthetic ammonia feed gas by liquid nitrogen washing | |
| CN102435045A (en) | Liquid nitrogen washing purified synthetic gas and device for cryogenically separating and recovering LNG (liquefied natural gas) thereof | |
| CN201945138U (en) | Separating and recovering device for argon and methane from exhausted gases from synthesis ammonia | |
| CN113862051B (en) | Double refrigeration cycle methane washing synthetic gas cryogenic separation device and separation method | |
| CN110553464A (en) | CO cryogenic separation system and method for reducing nitrogen circulation energy consumption | |
| CN103213946B (en) | Method for synthesizing ammonia by comprehensively utilizing liquefied natural gas | |
| CN114963691B (en) | Low pressure CO 2 Gas low-temperature separation method and device | |
| CN114017993B (en) | Device and method for producing hydrogen and byproduct oxygen by utilizing green electrolysis water | |
| CN105482861A (en) | Method for preparing LNG by utilizing low-pressure tower refluxing liquid as high-pressure tower washing liquid | |
| CN104974810A (en) | Method for producing liquefied natural gas (LNG) from semi-coke exhaust and calcium carbide furnace gas | |
| CN114087846A (en) | Device for producing dry ice by coupling photoelectric hydrogen production energy storage and cold energy recovery and use method | |
| CN210855900U (en) | Equipment for producing polyol by utilizing steelmaking blast furnace gas | |
| CN102757016B (en) | Method and device for cogeneration of synthesis ammonia gas and liquefied natural gas prepared through pressure gasification of crushed coal in fixed bed | |
| CN209558777U (en) | A kind of cryogenic liquefying separator of tail of semi coke | |
| CN114777414B (en) | Device and method for co-producing hydrogen, liquid hydrogen and liquefied natural gas by using industrial tail gas | |
| CN114353433B (en) | Nitrogen cycle refrigeration synthetic gas cryogenic separation device and system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |