CN115790078A - CO (carbon monoxide) 2 Liquefaction process and cold box - Google Patents
CO (carbon monoxide) 2 Liquefaction process and cold box Download PDFInfo
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- CN115790078A CN115790078A CN202211505772.1A CN202211505772A CN115790078A CN 115790078 A CN115790078 A CN 115790078A CN 202211505772 A CN202211505772 A CN 202211505772A CN 115790078 A CN115790078 A CN 115790078A
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Abstract
The invention belongs to CO 2 The invention belongs to the technical field of recycling and provides CO 2 A liquefaction process and a 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 in which CO 2 The refrigerating cycle system comprises a compressor, a Freon refrigerating machine, a reboiler and a heat exchanger which are connected in sequence. Using the cold box to treat CO 2 Carrying out liquefaction comprising the steps of: the raw material gas passes through a compression device, a purification device, a drying device and a cryogenic separation device in sequence to obtain liquid CO 2 (ii) a CO not being liquefied 2 Input of CO 2 In the refrigeration cycle system, the refrigeration capacity is provided for the cryogenic separation device. The cold box can liquefy CO 2 The gas with the volume content of 30-80 percent not only has low energy consumption, but also can improve CO 2 The recovery rate of (1).
Description
Technical Field
The invention relates to CO 2 Technology for recyclingThe technical field, in particular to CO 2 A liquefaction process and a cold box.
Background
At present, with the rapid development of economy, CO 2 The total amount of emissions is also increasing, so that carbon dioxide emission reduction has become a focus of common attention all over the world, and therefore, how to reduce CO 2 The recycling becomes a hot point of research. Liquid CO is prepared by reasonable process flow 2 Product, CO can be recycled 2 Tail gas, to CO 2 And (5) emission reduction.
However, most of the CO is currently available in China 2 The recycling process aims at the content of CO of more than 80 to 90 percent 2 The CO content of the carbon dioxide is recovered, and the carbon dioxide is about 30 to 80 percent 2 The recovery process is few, however, the content of CO is about 30 to 80 percent 2 Tail gas is relatively common, so that the CO with low energy consumption and suitable for the 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 has become an urgent problem to be solved by those skilled in the art.
Disclosure of Invention
In view of the above, the present invention provides a CO 2 A liquefaction process and a cold box, aiming at solving the problem of the prior art aiming at 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 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, said CO 2 The refrigerating cycle system comprises a compressor, a Freon refrigerating machine, a reboiler and a heat exchanger which are connected in sequence.
The invention provides CO 2 The liquefaction process adopts the cold box, and comprises the following steps:
the raw material gas is sequentially compressedThe device, the purification device, the drying device and the cryogenic separation device can obtain liquid CO 2 (ii) a CO not being liquefied 2 Input of 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 raw material gas contains 30-80% of CO by volume fraction 2 。
Furthermore, the pressure of the feed gas in the compression device is 2.0-3.6 MPa.
Furthermore, 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 feed gas in the drying unit is < -40 ℃.
Further, the temperature of the feed gas in the cryogenic separation device is-45 to-35 ℃.
Further, said CO 2 CO not liquefied in a refrigeration cycle 2 The pressure in the compressor is 2.0-3.6 MPa, and the temperature in the Freon refrigerator is-20 to-15 ℃.
According to the technical scheme, 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, and CO in the gas 2 The refrigeration cycle system can effectively separate liquid CO 2 And increase CO 2 Recovery rate of (a); 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 and liquefaction process is reduced, and the CO is recycled 2 Tail gas, to CO 2 And (4) the purpose of emission reduction.
Drawings
FIG. 1 shows the use of the cold box pair CO provided by the present invention 2 Flow chart for carrying out 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 inventionIn (2), the CO 2 The refrigerating cycle system comprises a compressor, a Freon refrigerating machine, a reboiler and a heat exchanger which are connected in sequence.
The invention provides CO 2 The liquefaction process adopts the cold box, and comprises the following steps:
the raw material gas passes through a compression device, a purification device, a drying device and a cryogenic separation device in sequence to obtain liquid CO 2 (ii) a CO not being liquefied 2 Input of 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 invention, the raw material gas contains 30-80% of CO by volume fraction 2 Preferably 40 to 70%, and 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 feed gas in the purification apparatus is not more than 1ppm, preferably not more than 0.8ppm, and more preferably not more than 0.5ppm.
In the present invention, the dew point temperature of the raw gas in the drying apparatus is less than-40 ℃, preferably less than-50 ℃, and more preferably-60 ℃ or-65 ℃.
In the invention, the temperature of the feed gas in the cryogenic separation device is-45 to-35 ℃, preferably-42 to-37 ℃, and more preferably-40 to-38 ℃.
In the present invention, the CO is 2 CO not liquefied in the refrigerating cycle 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 device comprises a rectifying tower and liquid CO 2 After purification in a rectification column, liquid CO 2 The obtained product is further purified to 99.5 to 99.9 percent in a reboiler, and the temperature in the reboiler is-15 to-12 ℃, preferably-14 ℃.
In the present invention, reboilingLiquid CO in the vessel 2 Entering a heat exchanger for supercooling to minus 20 to minus 25 ℃ and sending out; preferably-21 to-24 ℃ and more preferably-23 ℃.
In the present invention, CO is removed in the rectifying tower 2 And the other gas is reheated to-10-0 ℃ by a heat exchanger and then enters a tail gas expansion device, the tail gas expansion device can perform expansion refrigeration by using the pressure of the raw material gas in a compressor to provide cold energy for a cryogenic separation device, then the gas is reheated to normal temperature and then is exhausted, and the temperature of the reheated gas by the heat exchanger is preferably-5 ℃.
In the present invention, the tail gas expansion device includes any one of a turbo 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 exhaust 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 is 2 The working principle of the refrigeration cycle system is as follows: CO not being liquefied 2 Input of CO 2 In the refrigeration cycle system, the CO is compressed and cooled by a compressor, condensed and liquefied by a Freon refrigerator, and liquefied CO 2 And the refrigerant enters a reboiler of the rectifying tower to be used as a heat source for further cooling, then is throttled and cooled, returns to the heat exchanger to provide cold energy for the compressed feed gas, returns to the inlet of the compressor after being reheated to normal temperature, and completes the refrigeration cycle.
The technical solutions in the embodiments of the present invention will be clearly and completely described below, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
Will contain CO with a volume concentration of between 30 and 80 percent 2 Introducing the raw material gas into a compression device to be compressed to 3.0MPa; then conveying the mixture to a purification device for desulfurization to below 1 ppm; then conveying the mixture to a drying device for dehydration to enable the dew point of the mixture to be less than-40 ℃; conveying the dried raw material gas to a cryogenic separation device for coolingTo-40 deg.C, CO condensed to liquid 2 The liquid CO is sent to a rectifying tower for rectification and purification 2 Further purifying to 99.9% in reboiler (-14 deg.C), and then liquid CO in reboiler 2 Entering a heat exchanger for supercooling to-25 ℃ and sending out.
CO not being liquefied 2 Input of CO 2 In a refrigeration cycle system, the mixture is compressed to 3.0MPa by a compressor and then cooled to-18 ℃ by a Freon refrigerator, and CO is discharged 2 Completely condensed into liquid and sent to a reboiler at the bottom of the rectifying tower to provide heat and CO for the rectifying tower 2 The temperature of the refrigerant is further reduced to minus 20 ℃, then the refrigerant is sent to a heat exchanger to provide cold energy for the cryogenic separation device, and the refrigerant returns to the inlet of the compressor after being reheated to normal temperature, thereby completing the refrigeration cycle.
CO removal in a rectification column 2 And the other gas is reheated to-5 ℃ by a heat exchanger, enters a pressure reducing valve in a tail gas expansion device, is decompressed to 0.8MPa, is expanded and refrigerated by utilizing the pressure of the raw material gas in a compressor, provides cold energy for a cryogenic separation device, is reheated to normal temperature, and is exhausted.
Example CO 2 The recovery of (D) was 86%.
Example 2
Will contain CO with a volume concentration of between 30 and 80 percent 2 Introducing the raw material gas into a compression device to be compressed to 2.8MPa; then conveying the mixture to a purification device for desulfurization to below 1 ppm; then conveying the mixture to a drying device for dehydration to enable the dew point of the mixture to be less than-40 ℃; delivering the dried raw gas to a cryogenic separation device, cooling to-37 deg.C, and condensing into liquid CO 2 The liquid CO is sent to a rectifying tower for rectification and purification 2 Further purifying to 99.9% in reboiler (-15 deg.C), and then liquid CO in reboiler 2 Entering a heat exchanger for supercooling to minus 22 ℃ and sending out.
CO not being liquefied 2 Input of CO 2 In a refrigeration cycle system, the mixture is compressed to 2.5MPa by a compressor, cooled to-17 ℃ by a Freon refrigerator and then subjected to CO 2 Completely condensed into liquid and sent to a reboiler at the bottom of the rectifying tower to provide heat and CO for the rectifying tower 2 Is further reduced to-22 ℃, and then is sent to a heat exchanger to extract for a cryogenic separation deviceAnd (4) supplying cold energy, returning to the inlet of the compressor after the temperature is restored to the normal temperature, and completing the refrigeration cycle.
CO removal in a rectification column 2 And the other gas is reheated to-8 ℃ by a heat exchanger, enters a turbine expander in a tail gas expansion device to be expanded to 0.6MPa, is expanded and refrigerated by utilizing the pressure of raw material gas in a compressor, provides cold energy for a cryogenic separation device, is reheated to normal temperature and is exhausted.
Example CO 2 The recovery rate of (D) was 82%.
Example 3
Will contain CO with a volume concentration of between 30 and 80 percent 2 Introducing the raw material gas into a compression device to be compressed to 3.5MPa; then conveying the mixture to a purification device for desulfurization to below 1 ppm; then conveying the mixture to a drying device for dehydration to enable the dew point of the mixture to be less than-40 ℃; delivering the dried raw gas to a cryogenic separation device, cooling to-42 deg.C, and condensing into liquid CO 2 The liquid CO is sent to a rectifying tower for rectification and purification 2 Further purifying to 99.9% in reboiler (-12 deg.C), and then liquid CO in reboiler 2 Entering a heat exchanger for supercooling to-20 ℃ and sending out.
CO not being liquefied 2 Input of CO 2 In a refrigeration cycle system, the mixture is compressed to 3.4MPa by a compressor, cooled to-15 ℃ by a Freon refrigerator and then subjected to CO 2 Completely condensed into liquid and sent to a reboiler at the bottom of the rectifying tower to provide heat and CO for the rectifying tower 2 The temperature of the refrigerant is further reduced to-23 ℃, then the refrigerant is sent to a heat exchanger to provide cold energy for the cryogenic separation device, and the refrigerant returns to the inlet of the compressor after being reheated to normal temperature, thereby completing the refrigeration cycle.
CO removal in a rectification column 2 And the other gas is reheated to-6 ℃ by a heat exchanger, enters a gas bearing expander in the tail gas expansion device to be expanded to 0.5MPa, is expanded and refrigerated by utilizing the pressure of the raw material gas in the compressor, provides cold energy for the cryogenic separation device, is reheated to normal temperature and is exhausted.
Example CO 2 The recovery of (b) was 92%.
The embodiments in the present description are described in a progressive manner, each embodiment focuses on differences from other embodiments, and the same and similar parts among the embodiments are referred 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.
2. A cold box according to claim 1, wherein said CO 2 The refrigerating cycle system comprises a compressor, a Freon refrigerating machine, a reboiler and a heat exchanger which are connected in sequence.
3. CO (carbon monoxide) 2 Characterized in that the cold box of claim 1 or 2 is used, comprising the following steps:
the raw material gas passes through a compression device, a purification device, a drying device and a cryogenic separation device in sequence to obtain liquid CO 2 (ii) a CO not being liquefied 2 Input of 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. The liquefaction process of claim 3, wherein the feed gas comprises 30 to 80 vol.% CO 2 。
5. The liquefaction process of claim 4, wherein the pressure of the feed gas in the compression device is between 2.0 and 3.6MPa.
6. The liquefaction process of claim 4 or 5, characterized in that the sulphur content in the feed gas in the purification unit is less than or equal to 1ppm.
7. The liquefaction process of claim 6, characterized in that the dew point temperature of the feed gas in the drying means is < -40 ℃.
8. The liquefaction process of claim 3, 4 or 7, characterized in that the temperature of the feed gas in the cryogenic separation device is between-45 and-35 ℃.
9. The liquefaction process of claim 8, wherein the CO is 2 CO not liquefied in the refrigerating cycle 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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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
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| CN115790078B (en) | 2023-09-29 |
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