CN114576927A - Cryogenic method for preparing LNG (liquefied Natural gas) from coke oven gas - Google Patents
Cryogenic method for preparing LNG (liquefied Natural gas) from coke oven gas Download PDFInfo
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- CN114576927A CN114576927A CN202210290028.8A CN202210290028A CN114576927A CN 114576927 A CN114576927 A CN 114576927A CN 202210290028 A CN202210290028 A CN 202210290028A CN 114576927 A CN114576927 A CN 114576927A
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- refrigerant
- coke oven
- lng
- mixed refrigerant
- oven gas
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- 239000000571 coke Substances 0.000 title claims abstract description 16
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000007789 gas Substances 0.000 title claims description 29
- 239000003949 liquefied natural gas Substances 0.000 title claims description 26
- 239000003507 refrigerant Substances 0.000 claims abstract description 69
- 238000005057 refrigeration Methods 0.000 claims abstract description 15
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 47
- 238000001816 cooling Methods 0.000 claims description 7
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 claims description 3
- 238000004781 supercooling Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 abstract description 20
- 238000002360 preparation method Methods 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 22
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 description 16
- 229910052757 nitrogen Inorganic materials 0.000 description 11
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 description 8
- 239000001294 propane Substances 0.000 description 8
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 7
- 239000005977 Ethylene Substances 0.000 description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 238000006467 substitution reaction Methods 0.000 description 3
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Images
Classifications
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- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts of nitrogen
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- 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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
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- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
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- 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
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
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- 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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- 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
- F25J2210/14—Coke-ovens gas
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- 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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- 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
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- 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
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/902—Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers etc.
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- 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
- F25J2280/00—Control of the process or apparatus
- F25J2280/02—Control in general, load changes, different modes ("runs"), measurements
Abstract
The invention relates to the technical field of LNG preparation, in particular to a cryogenic method for preparing LNG from coke oven gas, which comprises the following steps that a refrigerant is pressurized in an MRC mixed refrigerant compressor, then enters a liquefaction cold box for heat exchange through a circulating pipeline, enters a denitrification tower and an inlet separator in sequence after heat exchange, and finally enters the MRC mixed refrigerant compressor for pressurization again through the circulating pipeline, wherein the refrigerant is a mixed refrigerant, and the mixed refrigerant comprises the following components in parts by weight: n is a radical of2 12.12％、CH4 43.18％、C2H4 21.7％、C3H8 12.5％、C5H128.6 percent. The invention saves the refrigeration cost of the compressor and improves the running performance of the compressor by optimizing the component proportion of the mixed refrigerant.
Description
Technical Field
The invention relates to the technical field of LNG preparation, in particular to a cryogenic method for preparing LNG from coke oven gas.
Background
In the cryogenic liquefaction process for preparing LNG (liquefied natural gas) from coke oven gas, a mixed refrigerant refrigeration compressor is connected with a liquefaction cold box, and the methane-rich gas in the upper working section is cooled to a temperature below-162 ℃ to separate a hydrogen component and a nitrogen component to form the LNG. The main refrigerating capacity of the cryogenic liquefying device is derived from an MRC mixed refrigerant compressor, circulating stepped refrigeration is carried out in a cold box according to the difference of the boiling points of five refrigerants, propane and isopentane participate in the refrigeration of the upper part of the cold box, ethylene participates in the refrigeration of the middle part, and methane and nitrogen participate in the refrigeration of the lower part of the cold box.
In operation, the problems in the operation of the MRC mixed refrigerant cycle are found: (1) in the existing refrigerant proportion, propane, isopentane and ethylene account for 49%, the work of an MRC mixed refrigerant compressor is increased, and the power consumption of the compressor is high. (2) Heavy refrigerants (propane, isopentane and ethylene) in the refrigerants are increased, and the top of the cold box can also reach a high heat exchange interval under the low-pressure environment of the compressor, so that the heat exchange efficiency is improved.
Disclosure of Invention
Aiming at the problems of high energy consumption of mixed refrigeration, influence on the operation of a compressor and the like in the prior art, the invention provides the cryogenic method for preparing the LNG from the coke oven gas, so that the refrigeration cost of the compressor is saved, and the operation performance of the compressor is improved.
The invention provides a cryogenic method for preparing LNG (liquefied natural gas) from coke oven gas, which comprises the following steps that after being pressurized in an MRC mixed refrigerant compressor, a refrigerant enters a liquefaction cold box through a circulating pipeline for heat exchange, the refrigerant after heat exchange sequentially enters a denitrification tower and an inlet separator, and finally enters the MRC mixed refrigerant compressor through the circulating pipeline for repressurization, wherein the refrigerant is a mixed refrigerant, and the mixed refrigerant comprises the following components in parts by weight: n is a radical of hydrogen 2 12.12％、CH4 43.18％、C2H4 21.7％、C3H8 12.5％、C5H128.6 percent, and the balance of hydrogen-rich gas and inevitable impurity gas.
Furthermore, a plate-fin heat exchanger is arranged in the liquefaction cold box and arranged on the circulating pipeline.
Further, the temperature of the refrigerant before entering the MRC mixed refrigerant compressor was 30 ℃.
Furthermore, the heat exchange temperature of the bottom in the liquefaction cold box is-162 to-167 ℃.
Furthermore, the liquefaction cold box is provided with an inlet end and an outlet end, and the inlet end is connected with methane gas.
Further, the temperature of the methane gas entering the liquefaction cold box is 40 ℃.
Further, the pressure of the mixed refrigerant compressor for pressurizing the refrigerant is 3.0 MPaG.
Further, the refrigerant is subjected to stepped refrigeration in the liquefaction cold box, and the stepped refrigeration comprises top precooling, middle liquefaction and bottom supercooling.
The invention optimizes the refrigerant proportion and reduces the heavy refrigerant propane (C)3H8) Isopentane (C)5H12) Ethylene (C)2H4) Proportioning and increasing light refrigerant methane (CH)4) Nitrogen (N)2) Ratio of occupation. The nitrogen mainly has the function of providing cold energy at the bottom of the cold box, and the vaporization quantity is enough to support the pressure of the MRC mixed refrigerant compressor; the main function of the methane is to provide cold in the middle of the cold box and a small amount of cold at the bottom. The nitrogen comes from a public pipe network, the methane can be produced by itself, and the methane and the nitrogen have no purchase cost. Based on the effect analysis of the heavy refrigerant and the light refrigerant in the cold box, the refrigerant ratio adjusting direction is determined, the ratio of nitrogen to methane is improved by 1-3%, the ratio of ethylene to propane to isopentane is reduced by 1-3%, and the adjusted current refrigerant ratio is (N) 2 12.12％、CH4 43.18％、C2H421.7％、C3H8 12.5％、C5H128.6%), the cold area of the plate-fin heat exchanger is moved upwards during heat exchange, and the running cost of the compressor is reduced.
The invention has the beneficial effects that:
(1) the invention improves the light cryogen methane (CH) in the refrigerant4) Nitrogen (N)2) Proportioning, stabilizing the bottom temperature of the plate-fin heat exchanger of the cold box, reducing methane components in high nitrogen and hydrogen and effectively increasing the yield of LNG;
(2) the invention reduces the propane (C) of the heavy refrigerant in the refrigerant3H8) Isopentane (C)5H12) Ethylene (C)2H4) Proportioning and adding light refrigerant methane (CH)4) Nitrogen (N)2) Proportioning, and reducing the operation cost of the MRC mixed refrigerant compressor;
(3) the invention optimizes the proportion of heavy refrigerant in the refrigerant, and the bottom countercurrent temperature zone is transferred to the upper part, thereby effectively reducing the temperature of the upper plate fin of the cold box, reducing the running cost of the MRC mixed refrigerant compressor and improving the running performance of the compressor;
(4) the invention adopts the boiling point of the mixed refrigerant to carry out step cooling, effectively carries out heat exchange on methane gas and ensures the liquefaction quality of LNG.
Drawings
In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present invention, the drawings used in the description of the embodiments or prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained based on these drawings without creative efforts.
FIG. 1 is a refrigerant cooling flow diagram of an embodiment of the present invention.
In the figure: 1-an inlet separator, 2-an MRC mixed refrigerant compressor, 3-a circulating pipeline, 4-a liquefaction cold box and 5-a denitrogenation tower.
Detailed Description
In order to make those skilled in the art better understand the technical solutions of the present invention, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, shall fall within the protection scope of the present invention.
Example 1
The cryogenic method for preparing LNG (liquefied natural gas) from coke oven gas comprises the following steps that as shown in figure 1, the temperature of a refrigerant is 30 ℃, after the refrigerant is pressurized in an MRC mixed refrigerant compressor 2, the pressurizing pressure of the MRC mixed refrigerant compressor 2 is 3.0MPaG, the pressurized refrigerant enters a liquefaction cold box 4 through a circulating pipeline 3 for heat exchange, a plate-fin heat exchanger is arranged in the liquefaction cold box 4 and arranged on the circulating pipeline 3, the liquefaction cold box 4 is provided with an inlet end and an outlet end, the inlet end is connected with methane gas for refrigerating and liquefying the methane gas, the temperature of the methane gas entering the liquefaction cold box 4 is 40 ℃, the temperature of the refrigerant is throttled and cooled in the liquefaction cold box 4 after the methane gas enters the liquefaction cold box 4 and is pressurized by the MRC mixed refrigerant compressor 2, the bottom temperature of the liquefaction cold box 4 is stabilized at-162 ℃ to-167 ℃, and the methane gas is throttled and cooled in the liquefaction cold box 4 The liquefied refrigerant is discharged from the outlet end, the refrigerant after heat exchange sequentially enters the denitrogenation tower 5 and the inlet separator 1, and finally enters the MRC mixed refrigerant compressor 2 through the circulating pipeline 3 to be pressurized again, wherein the refrigerant is a mixed refrigerant which comprises the following components in proportion: n is a radical of hydrogen2 12.12％、CH4 43.18％、C2H4 21.7％、C3H8 12.5％、C5H12 8.6％。
The mixed refrigerant is optimized in proportion, the propane and the isopentane have different boiling points, the propane and the isopentane participate in the refrigeration and precooling action of the upper part of the liquefied cold box 4, the methane and the ethylene participate in the liquefaction and refrigeration action of the middle part of the liquefied cold box 4, and the nitrogen participates in the supercooling and refrigeration action of the lower part of the liquefied cold box 4 to carry out stepped cooling, so that the methane gas is effectively subjected to heat exchange, and the liquefied quality of LNG is ensured.
Although the present invention has been described in detail in connection with the preferred embodiments with reference to the accompanying drawings, the present invention is not limited thereto. Various equivalent modifications or substitutions can be made on the embodiments of the present invention by those skilled in the art without departing from the spirit and scope of the present invention, and these modifications or substitutions are within the scope of the present invention/any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention.
Claims (8)
1. The cryogenic method for preparing LNG (liquefied natural gas) from coke oven gas is characterized by comprising the following steps that a refrigerant is pressurized in an MRC mixed refrigerant compressor, then enters a liquefaction cold box for heat exchange through a circulating pipeline, enters a denitrification tower and an inlet separator in sequence after heat exchange, and finally enters the MRC mixed refrigerant compressor for pressurization again through the circulating pipeline, wherein the refrigerant is a mixed refrigerant which comprises the following components in parts by weight: n is a radical of hydrogen2 12.12％、CH443.18％、C2H421.7％、C3H812.5％、C5H128.6％。
2. The cryogenic process for preparing LNG from coke oven gas as claimed in claim 1, wherein the liquefaction cooling tank is internally provided with a plate-fin heat exchanger, and the plate-fin heat exchanger is arranged on a circulating pipeline.
3. The cryogenic process for producing LNG from coke oven gas as claimed in claim 1, wherein the temperature of the refrigerant before entering the MRC mixed refrigerant compressor is 30 ℃.
4. The cryogenic method for preparing LNG from coke oven gas as claimed in claim 1, wherein the heat exchange temperature of the bottom in the liquefaction cooling tank is-162 ℃ to-167 ℃.
5. The cryogenic process for producing LNG from coke oven gas as claimed in claim 1, wherein the liquefaction cooling tank is provided with an inlet port and an outlet port, the inlet port being connected to methane gas.
6. The cryogenic process for producing LNG from coke oven gas as claimed in claim 5, wherein the temperature of the methane gas entering the liquefaction cooling tank is 40 ℃.
7. The cryogenic process for producing LNG from coke oven gas according to claim 1, wherein the pressure of the MRC mixed refrigerant compressor pressurizing the refrigerant is 3.0 MPaG.
8. The cryogenic method for preparing LNG by using coke oven gas as claimed in any one of claims 1 to 7, wherein the refrigerant is subjected to step refrigeration in a liquefaction cold box, and the step refrigeration comprises top precooling, middle liquefaction and bottom supercooling.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210290028.8A CN114576927A (en) | 2022-03-23 | 2022-03-23 | Cryogenic method for preparing LNG (liquefied Natural gas) from coke oven gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202210290028.8A CN114576927A (en) | 2022-03-23 | 2022-03-23 | Cryogenic method for preparing LNG (liquefied Natural gas) from coke oven gas |
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4901533A (en) * | 1986-03-21 | 1990-02-20 | Linde Aktiengesellschaft | Process and apparatus for the liquefaction of a natural gas stream utilizing a single mixed refrigerant |
| US20060162378A1 (en) * | 2003-03-18 | 2006-07-27 | Roberts Mark J | Integrated multiple-loop refrigeration process for gas liquefaction |
| CN102504900A (en) * | 2011-10-20 | 2012-06-20 | 辽宁哈深冷气体液化设备有限公司 | Equipment for preparing liquefied natural gas (LNG) from coke oven gas and method thereof |
| FR2993643A1 (en) * | 2012-07-17 | 2014-01-24 | Saipem Sa | NATURAL GAS LIQUEFACTION PROCESS WITH PHASE CHANGE |
| CN103697661A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of coke oven gas |
| CN103697660A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing LNG and hydrogen-rich products out of high methane gas |
| CN105698487A (en) * | 2016-03-17 | 2016-06-22 | 杨晓东 | Mixed refrigerant internal circulation method, and natural gas liquefying method and device |
-
2022
- 2022-03-23 CN CN202210290028.8A patent/CN114576927A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4901533A (en) * | 1986-03-21 | 1990-02-20 | Linde Aktiengesellschaft | Process and apparatus for the liquefaction of a natural gas stream utilizing a single mixed refrigerant |
| US20060162378A1 (en) * | 2003-03-18 | 2006-07-27 | Roberts Mark J | Integrated multiple-loop refrigeration process for gas liquefaction |
| CN102504900A (en) * | 2011-10-20 | 2012-06-20 | 辽宁哈深冷气体液化设备有限公司 | Equipment for preparing liquefied natural gas (LNG) from coke oven gas and method thereof |
| FR2993643A1 (en) * | 2012-07-17 | 2014-01-24 | Saipem Sa | NATURAL GAS LIQUEFACTION PROCESS WITH PHASE CHANGE |
| CN103697661A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing liquefied natural gas and hydrogen-rich products out of coke oven gas |
| CN103697660A (en) * | 2013-12-23 | 2014-04-02 | 中空能源设备有限公司 | Device and method for manufacturing LNG and hydrogen-rich products out of high methane gas |
| CN105698487A (en) * | 2016-03-17 | 2016-06-22 | 杨晓东 | Mixed refrigerant internal circulation method, and natural gas liquefying method and device |
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