CN115790078B - CO (carbon monoxide) 2 Liquefying process and cold box - Google Patents
CO (carbon monoxide) 2 Liquefying process and cold box Download PDFInfo
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- CN115790078B CN115790078B CN202211505772.1A CN202211505772A CN115790078B CN 115790078 B CN115790078 B CN 115790078B CN 202211505772 A CN202211505772 A CN 202211505772A CN 115790078 B CN115790078 B CN 115790078B
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Abstract
The invention belongs to CO 2 The invention provides a CO in the technical field of recycling 2 Liquefaction process and cold box. The cold box comprises a compression device, a purification device, a drying device, a cryogenic separation device and CO which are connected in sequence 2 Refrigeration cycle system wherein CO 2 The refrigeration cycle system comprises a compressor, a Freon refrigerator, a reboiler and a heat exchanger which are connected in sequence. CO using the cold box 2 Liquefaction is carried out, comprising the following steps: the raw material gas sequentially passes through a compression device, a purification device, a drying device and a cryogenic separation device to obtain liquid CO 2 The method comprises the steps of carrying out a first treatment on the surface of the CO not liquefied 2 Input CO 2 In the refrigeration cycle, refrigeration capacity is provided for the cryogenic separation plant. The cold box can liquefy CO 2 The gas with the volume content of 30-80 percent has low energy consumption and can improve CO 2 Is a recovery rate of (2).
Description
Technical Field
The present invention relates to CO 2 The technical field of recycling, in particular to a CO 2 Liquefaction process and cold box.
Background
At present, with the rapid development of economy, CO 2 As well as the total emissions, so that carbon dioxide emissions reduction has become a common worldwide focus, how to convert CO 2 Recycling becomes a hot spot of research. Liquid CO is prepared through reasonable process flow 2 The product can recycle CO 2 Tail gas realizes CO 2 And emission reduction.
However, most of domestic CO 2 The recycling process is needleFor CO with the content of more than 80 to 90 percent 2 Recovering and aiming at about 30 to 80 percent of CO 2 The recovery process is less, however, the content of CO is about 30 to 80 percent 2 Tail gas is common, so that low-energy-consumption CO with proper concentration is designed 2 The recovery process is of vital importance.
Therefore, how to provide a method for effectively recycling and utilizing CO with the content of 30-80 percent 2 The processing of gases is a problem that needs to be addressed by those skilled in the art.
Disclosure of Invention
In view of this, the present invention provides a CO 2 The liquefying process and the cold box aim at solving the problem that the prior CO with the volume concentration of 30-80 percent 2 The recovery process has the technical problems of high energy consumption, low recovery rate and the like.
In order to achieve the above purpose, the invention adopts the following technical scheme:
the invention provides a cold box, which comprises a compression device, a purification device, a drying device, a cryogenic separation device and CO which are connected in sequence 2 A refrigeration cycle system.
Further, the CO 2 The refrigeration cycle system comprises a compressor, a Freon refrigerator, a reboiler and a heat exchanger which are connected in sequence.
The invention provides a CO 2 The liquefaction process adopts the cold box, and comprises the following steps:
the raw material gas sequentially passes through a compression device, a purification device, a drying device and a cryogenic separation device to obtain liquid CO 2 The method comprises the steps of carrying out a first treatment on the surface of the CO not liquefied 2 Input CO 2 In the refrigeration cycle system, cold energy is provided for the cryogenic separation device, and the rest gas enters the tail gas expansion device.
Further, the feed gas contains 30 to 80% by volume of CO 2 。
Further, the pressure of the raw material gas in the compression device is 2.0-3.6 MPa.
Further, in the purification device, the sulfur content in the raw material gas is less than or equal to 1ppm.
Further, the dew point temperature of the raw material gas in the drying device is < -40 ℃.
Further, the temperature of the raw material gas in the cryogenic separation device is-45 to-35 ℃.
Further, the CO 2 In the refrigeration cycle system, CO that is not liquefied 2 The pressure in the compressor is 2.0-3.6 MPa, and the temperature in the Freon refrigerator is-20 to-15 ℃.
Compared with the prior art, the invention has the following beneficial effects:
for CO 2 The gas with the volume content of 30-80 percent adopts the cold box provided by the invention, wherein CO 2 The refrigeration cycle system can effectively separate liquid CO 2 And improve CO 2 Is a recovery rate of (2); the tail gas expansion device utilizes the pressure energy of the raw material gas to expand and refrigerate, thereby reducing CO 2 The power consumption of the separation liquefaction process is further realized, and the CO is recycled 2 Tail gas realizes CO 2 The purpose of emission reduction.
Drawings
FIG. 1 shows the cold box pair CO provided by the invention 2 A flow chart for performing liquefaction.
Detailed Description
The invention provides a cold box, which comprises a compression device, a purification device, a drying device, a cryogenic separation device and CO which are connected in sequence 2 A refrigeration cycle system.
In the present invention, the CO 2 The refrigeration cycle system comprises a compressor, a Freon refrigerator, a reboiler and a heat exchanger which are connected in sequence.
The invention provides a CO 2 The liquefaction process adopts the cold box, and comprises the following steps:
the raw material gas sequentially passes through a compression device, a purification device, a drying device and a cryogenic separation device to obtain liquid CO 2 The method comprises the steps of carrying out a first treatment on the surface of the CO not liquefied 2 Input CO 2 In the refrigeration cycle system, cold energy is provided for the cryogenic separation device, and the rest gas enters the tail gas expansion device.
In the present invention, the raw material gas contains 30 to 80% by volume of CO 2 Preferably 40 to 70%, more preferably 50 to 60%.
In the present invention, the pressure of the raw material gas in the compression device is 2.0 to 3.6MPa, preferably 2.2 to 3.5MPa, and more preferably 2.5 to 3.0MPa.
In the present invention, the sulfur content in the raw material gas in the purification apparatus is 1ppm or less, preferably 0.8ppm or less, and more preferably 0.5ppm or less.
In the present invention, the dew point temperature of the raw material gas in the drying apparatus is < -40 ℃, preferably < -50 ℃, and more preferably-60 ℃ or-65 ℃.
In the present invention, the temperature of the raw material gas in the cryogenic separation plant is-45 to-35 ℃, preferably-42 to-37 ℃, and more preferably-40 to-38 ℃.
In the present invention, the CO 2 In the refrigeration cycle system, CO that is not liquefied 2 The pressure in the compressor is 2.0 to 3.6MPa, preferably 2.2 to 3.5MPa, more preferably 2.5 to 3.0MPa, and the temperature in the Freon refrigerator is-20 to-15 ℃, preferably-18 ℃.
In the invention, the cryogenic separation plant comprises a rectifying tower and liquid CO 2 After purification in a rectifying column, liquid CO 2 Further purifying to 99.5-99.9% in reboiler at-15-12 deg.c, preferably-14 deg.c.
In the present invention, liquid CO in reboiler 2 Entering a heat exchanger to be supercooled to minus 20 to minus 25 ℃ and then being sent out; preferably at-21 to-24℃and more preferably at-23 ℃.
In the present invention, CO is removed in the rectifying column 2 The other gases are rewuped to the temperature of minus 10 ℃ to 0 ℃ by a heat exchanger and then enter a tail gas expansion device, the tail gas expansion device can utilize the raw material gas pressure in a compressor to carry out expansion refrigeration, cold energy is provided for a cryogenic separation device, then the gas is rewuped to the normal temperature and then is exhausted, and the rewuped temperature by the heat exchanger is preferably minus 5 ℃.
In the present invention, the exhaust gas expansion device includes any one of a turbine expander, a gas bearing expander, an oil bearing expander, a screw expander, and a pressure reducing valve.
In the present invention, the pressure of the gas in the tail gas expansion device is 0.2 to 1.0MPa, preferably 0.4 to 0.8MPa, and more preferably 0.6MPa.
In the present invention, the CO 2 The working principle of the refrigeration cycle system is as follows: CO not liquefied 2 Input CO 2 In the refrigeration cycle system, the refrigerant is compressed and cooled by a compressor, and then condensed and liquefied by a Freon refrigerator, and liquefied CO 2 The reboiler of the rectifying tower is used as a heat source for further cooling, then throttling and cooling are carried out, the heat exchanger is returned to provide cold energy for the compressed raw material gas, and the raw material gas returns to the inlet of the compressor after being rewarmed to normal temperature, so that the refrigeration cycle is completed.
The following description of the technical solutions in the embodiments of the present invention will be clear and complete, and it is obvious that the described embodiments are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
Example 1
The CO with the volume concentration of 30 to 80 percent 2 The raw material gas is introduced into a compression device to be compressed to 3.0MPa; delivering the mixture to a purifying device to desulfurize the mixture to less than 1 ppm; then the mixture is conveyed to a drying device for dehydration, so that the dew point is less than-40 ℃; delivering the dried raw gas to a cryogenic separation plant, cooling to-40deg.C, condensing to liquid CO 2 Delivering the mixture to a rectifying tower for rectifying and purifying the liquid CO 2 Enters a reboiler (-14 ℃) to be further purified to 99.9%, and then liquid CO in the reboiler 2 And the mixture enters a heat exchanger to be supercooled to minus 25 ℃ and is sent out.
CO not liquefied 2 Input CO 2 In the refrigeration cycle system, the refrigerant is compressed to 3.0MPa by a compressor, then cooled to-18 ℃ by a Freon refrigerator, and CO 2 The liquid is completely condensed and sent to a reboiler at the bottom of the rectifying tower to provide heat for the rectifying tower, and CO 2 Further reducing the temperature to-20 ℃ and then sending the mixture to a heat exchanger for deep heatingThe cold separating device provides cold energy, and returns to the inlet of the compressor after being rewarmed to normal temperature, thus completing the refrigeration cycle.
CO removal in rectifying column 2 The other gases are rewuped to minus 5 ℃ by a heat exchanger and then enter a pressure reducing valve in a tail gas expansion device to be decompressed to 0.8MPa, the raw material gas pressure in a compressor is utilized for expansion refrigeration, the refrigeration capacity is provided for a cryogenic separation device, and then the cryogenic separation device is rewuped to normal temperature and then is emptied.
Example CO 2 The recovery rate of (2) was 86%.
Example 2
The CO with the volume concentration of 30 to 80 percent 2 The raw material gas is introduced into a compression device to be compressed to 2.8MPa; delivering the mixture to a purifying device to desulfurize the mixture to less than 1 ppm; then the mixture is conveyed to a drying device for dehydration, so that the dew point is less than-40 ℃; delivering the dried raw gas to a cryogenic separation plant, cooling to-37deg.C, condensing to liquid CO 2 Delivering the mixture to a rectifying tower for rectifying and purifying the liquid CO 2 Further purifying to 99.9% in reboiler (-15 deg.C), and then liquid CO in reboiler 2 And the mixture enters a heat exchanger to be supercooled to-22 ℃ and is sent out.
CO not liquefied 2 Input CO 2 In the refrigeration cycle system, the refrigerant is compressed to 2.5MPa by a compressor, then cooled to-17 ℃ by a Freon refrigerator, and CO 2 The liquid is completely condensed and sent to a reboiler at the bottom of the rectifying tower to provide heat for the rectifying tower, and CO 2 The temperature of the refrigerant is further reduced to-22 ℃, then the refrigerant is sent to a heat exchanger to provide cold for the cryogenic separation device, and the refrigerant returns to the inlet of the compressor after being rewarmed to normal temperature, thus completing the refrigeration cycle.
CO removal in rectifying column 2 The other gases are reheated to the temperature of minus 8 ℃ by a heat exchanger and then enter a turbine expander in the tail gas expansion device to be expanded to 0.6MPa, the raw material gas pressure in the compressor is utilized to carry out expansion refrigeration, the cryogenic separation device is provided with cold energy, and then the cryogenic separation device is reheated to normal temperature and then is emptied.
Example CO 2 The recovery rate of (2) was 82%.
Example 3
The CO with the volume concentration of 30 to 80 percent 2 Raw materialsIntroducing the gas into a compression device to compress to 3.5MPa; delivering the mixture to a purifying device to desulfurize the mixture to less than 1 ppm; then the mixture is conveyed to a drying device for dehydration, so that the dew point is less than-40 ℃; delivering the dried raw gas to a cryogenic separation plant, cooling to-42 ℃, condensing into liquid CO 2 Delivering the mixture to a rectifying tower for rectifying and purifying the liquid CO 2 Enters a reboiler (-12 ℃) to be further purified to 99.9%, and then liquid CO in the reboiler 2 And the mixture enters a heat exchanger to be supercooled to-20 ℃ and is sent out.
CO not liquefied 2 Input CO 2 In the refrigeration cycle system, the refrigerant is compressed to 3.4MPa by a compressor, then cooled to-15 ℃ by a Freon refrigerator, and CO 2 The liquid is completely condensed and sent to a reboiler at the bottom of the rectifying tower to provide heat for the rectifying tower, and CO 2 The temperature of the refrigerant is further reduced to-23 ℃, and then the refrigerant is sent to a heat exchanger to provide cold for the cryogenic separation device, and the refrigerant returns to the inlet of the compressor after being rewarmed to normal temperature, thus completing the refrigeration cycle.
CO removal in rectifying column 2 The other gases are reheated to minus 6 ℃ by a heat exchanger and then enter a gas bearing expander in the tail gas expansion device to be expanded to 0.5MPa, the raw material gas pressure in the compressor is utilized to carry out expansion refrigeration, the cryogenic separation device is provided with cold energy, and then the cryogenic separation device is reheated to normal temperature and then is emptied.
Example CO 2 The recovery rate of (2%) was 92%.
In the present specification, each embodiment is described in a progressive manner, and each embodiment is mainly described in a different point from other embodiments, and identical and similar parts between the embodiments are all enough to refer to each other.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (9)
1. The cold box is characterized by comprising a compression device, a purification device, a drying device, a cryogenic separation device and CO which are sequentially connected 2 A refrigeration cycle system;
liquid CO 2 And CO not liquefied 2 CO removal 2 The specific connection relation of the other gas treatment processes and the liquefying components is as follows:
the CO with the volume concentration of 30 to 80 percent 2 The raw material gas is introduced into a compression device for compression and then is conveyed to a purification device for desulfurization; then the mixture is conveyed to a drying device for dehydration; delivering the dried raw material gas to a cryogenic separation device for cooling, and condensing into liquid CO 2 Delivering the mixture to a rectifying tower for rectifying and purifying the liquid CO 2 Further purifying in reboiler, and then liquid CO in reboiler 2 Subcooling the mixture in a heat exchanger and discharging the mixture of CO which is not liquefied 2 Input CO 2 In the refrigeration cycle system, the CO is compressed by a compressor and then cooled by a Freon refrigerator 2 The liquid is completely condensed and sent to a reboiler at the bottom of the rectifying tower to provide heat for the rectifying tower, and CO 2 The temperature of the mixture is further reduced, and then the mixture is sent to a heat exchanger to provide cold energy for a cryogenic separation device, and the mixture is returned to the inlet of a compressor after being rewarmed to normal temperature, so that the refrigeration cycle is completed, and CO is removed in a rectifying tower 2 The other gases are subjected to rewarming by the heat exchanger and then enter a pressure reducing valve in the tail gas expansion device for pressure reduction, the raw material gas pressure in the compressor is utilized for expansion refrigeration, cold energy is provided for the cryogenic separation device, and then the cryogenic separation device is subjected to rewarming to normal temperature and then is emptied.
2. The cold box according to claim 1, wherein the CO 2 The refrigeration cycle system comprises a compressor, a Freon refrigerator, a reboiler and a heat exchanger which are connected in sequence.
3. CO (carbon monoxide) 2 Is characterized in that it uses the cold box according to claim 1 or 2, comprising the following steps:
sequentially adding raw material gasThe liquid CO can be obtained through a compression device, a purification device, a drying device and a cryogenic separation device 2 The method comprises the steps of carrying out a first treatment on the surface of the CO not liquefied 2 Input CO 2 In the refrigeration cycle system, cold energy is provided for the cryogenic separation device, and the rest gas enters the tail gas expansion device.
4. A liquefaction process according to claim 3, wherein the feed gas comprises 30-80% by volume of CO 2 。
5. The liquefaction process according to claim 4, wherein the pressure of the feed gas in the compression device is between 2.0 and 3.6MPa.
6. The liquefaction process according to claim 4 or 5, wherein the sulfur content of the feed gas in the purification device is less than or equal to 1ppm.
7. The liquefaction process according to claim 6, wherein the feed gas has a dew point temperature in the drying means of < -40 ℃.
8. A liquefaction process according to claim 3, wherein the temperature of the feed gas in the cryogenic separation plant is in the range-45 to-35 ℃.
9. The liquefaction process of claim 8, wherein the CO 2 In the refrigeration cycle system, CO that is not liquefied 2 The pressure in the compressor is 2.0-3.6 MPa, and the temperature in the Freon refrigerator is-20 to-15 ℃.
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| CN202211505772.1A CN115790078B (en) | 2022-11-29 | 2022-11-29 | CO (carbon monoxide) 2 Liquefying process and cold box |
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| CN202211505772.1A CN115790078B (en) | 2022-11-29 | 2022-11-29 | CO (carbon monoxide) 2 Liquefying process and cold box |
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| CN108870868B (en) * | 2018-09-10 | 2023-08-22 | 江苏华扬液碳有限责任公司 | Skid-mounted movable carbon dioxide oil displacement produced gas recovery system |
Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4883516A (en) * | 1987-04-07 | 1989-11-28 | The Boc Group, Inc. | Air separation |
| JP2002316809A (en) * | 2001-01-31 | 2002-10-31 | Mayekawa Mfg Co Ltd | System for preparing, storing and utilizing liquefied co2 dry ice, system for preparing, storing and utilizing liquefied co2 and hydrogen, and method and apparatus for preparing dry ice |
| CN101126041A (en) * | 2007-03-28 | 2008-02-20 | 林寿贵 | Cascade connection method for preparing liquefied natural gas |
| CN102422108A (en) * | 2009-03-09 | 2012-04-18 | 英国备选能源国际有限公司 | Separation of carbon dioxide and hydrogen |
| CN104515361A (en) * | 2013-09-30 | 2015-04-15 | 神华集团有限责任公司 | Method for producing liquid carbon dioxide |
| CN106979664A (en) * | 2017-03-06 | 2017-07-25 | 毛恒松 | Atmospheric carbon dioxide liquifying method |
| CN108870868A (en) * | 2018-09-10 | 2018-11-23 | 江苏华扬液碳有限责任公司 | A kind of skid movable carbon dioxide displacement of reservoir oil output gas recovery system |
| CN110054153A (en) * | 2019-04-18 | 2019-07-26 | 裴栋中 | A kind of device of refinery factory refinery dry gas purification hydrogen manufacturing |
| CN111238166A (en) * | 2020-03-20 | 2020-06-05 | 金昌隆博气体有限责任公司 | Refrigeration cycle system and method in carbon dioxide rectification separation process |
| CN210892361U (en) * | 2019-08-29 | 2020-06-30 | 兖矿国宏化工有限责任公司 | Device for preparing liquid carbon dioxide by utilizing surplus cold energy for refrigeration |
| CN113318470A (en) * | 2021-05-31 | 2021-08-31 | 鲁西化工集团股份有限公司氯碱化工分公司 | Fluorine direct cooling technology combined chlorine rectification purification system and method |
| CN114165987A (en) * | 2021-12-09 | 2022-03-11 | 重庆川茂化工科技有限公司 | Liquid carbon dioxide production device and production method thereof |
| CN114963691A (en) * | 2022-05-31 | 2022-08-30 | 山东石油化工学院 | Low pressure CO 2 Low-temperature gas separation method and device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009016625A2 (en) * | 2007-07-29 | 2009-02-05 | Baruchi Barry Baruch Kimchi | Method and system for the separation of a mixture containing carbon dioxide, hydrocarbon, and hydrogen |
-
2022
- 2022-11-29 CN CN202211505772.1A patent/CN115790078B/en active Active
Patent Citations (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4883516A (en) * | 1987-04-07 | 1989-11-28 | The Boc Group, Inc. | Air separation |
| JP2002316809A (en) * | 2001-01-31 | 2002-10-31 | Mayekawa Mfg Co Ltd | System for preparing, storing and utilizing liquefied co2 dry ice, system for preparing, storing and utilizing liquefied co2 and hydrogen, and method and apparatus for preparing dry ice |
| CN101126041A (en) * | 2007-03-28 | 2008-02-20 | 林寿贵 | Cascade connection method for preparing liquefied natural gas |
| CN102422108A (en) * | 2009-03-09 | 2012-04-18 | 英国备选能源国际有限公司 | Separation of carbon dioxide and hydrogen |
| CN104515361A (en) * | 2013-09-30 | 2015-04-15 | 神华集团有限责任公司 | Method for producing liquid carbon dioxide |
| CN106979664A (en) * | 2017-03-06 | 2017-07-25 | 毛恒松 | Atmospheric carbon dioxide liquifying method |
| CN108870868A (en) * | 2018-09-10 | 2018-11-23 | 江苏华扬液碳有限责任公司 | A kind of skid movable carbon dioxide displacement of reservoir oil output gas recovery system |
| CN110054153A (en) * | 2019-04-18 | 2019-07-26 | 裴栋中 | A kind of device of refinery factory refinery dry gas purification hydrogen manufacturing |
| CN210892361U (en) * | 2019-08-29 | 2020-06-30 | 兖矿国宏化工有限责任公司 | Device for preparing liquid carbon dioxide by utilizing surplus cold energy for refrigeration |
| CN111238166A (en) * | 2020-03-20 | 2020-06-05 | 金昌隆博气体有限责任公司 | Refrigeration cycle system and method in carbon dioxide rectification separation process |
| CN113318470A (en) * | 2021-05-31 | 2021-08-31 | 鲁西化工集团股份有限公司氯碱化工分公司 | Fluorine direct cooling technology combined chlorine rectification purification system and method |
| CN114165987A (en) * | 2021-12-09 | 2022-03-11 | 重庆川茂化工科技有限公司 | Liquid carbon dioxide production device and production method thereof |
| CN114963691A (en) * | 2022-05-31 | 2022-08-30 | 山东石油化工学院 | Low pressure CO 2 Low-temperature gas separation method and device |
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