CN217661593U - Device for purifying and recovering carbon dioxide by low-temperature rectification - Google Patents
Device for purifying and recovering carbon dioxide by low-temperature rectification Download PDFInfo
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- CN217661593U CN217661593U CN202221520729.8U CN202221520729U CN217661593U CN 217661593 U CN217661593 U CN 217661593U CN 202221520729 U CN202221520729 U CN 202221520729U CN 217661593 U CN217661593 U CN 217661593U
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Abstract
The utility model provides a low temperature rectification purification retrieves carbon dioxide device directly utilizes the feed gas as the refrigerant, provides cold volume through adopting carbon dioxide self high pressure throttle, does not need other devices to provide cold volume, and the energy consumption is low, and process flow is simple reliable. The compressor is connected with the cooler, and the cooler is connected with the desulfurization unit; the desulfurization unit is connected with the adsorber, and the adsorber is connected with the main heat exchanger; the reboiler is connected with the rectifying tower; the main heat exchanger is connected with the reboiler, the reboiler is connected with the subcooler, and the subcooler is connected with the first gas-liquid separator; the first gas-liquid separator is connected with the rectifying tower and the subcooler, the subcooler is connected with the main heat exchanger, the main heat exchanger is connected with the electric heater, and the electric heater is connected with the adsorber; the top of the rectifying tower is connected with a subcooler, and the subcooler is connected with a second gas-liquid separator; and the second gas-liquid separator is connected with the rectifying tower and the subcooler, and the subcooler is connected with the main heat exchanger.
Description
Technical Field
The utility model relates to a low temperature rectification purification retrieves carbon dioxide device is applicable to the carbon dioxide recovery of chemical plant emission waste gas and recycles.
Background
The combustion of natural gas, coke, heavy oil and other fuels, the production of synthetic ammonia and glycol, and the production process of petrochemical industry need to discharge a large amount of carbon dioxide. The emission of a large amount of carbon dioxide has an influence on the environment, so that the greenhouse effect is formed, and the global temperature is raised. The green low-carbon transformation of the major petrochemical industry has the value of collecting, recycling and reusing the waste gas containing a large amount of carbon dioxide directly discharged into the atmosphere in the carbon neutralization background.
Carbon dioxide Capture is the primary link for implementing Carbon Capture, sequestration and Utilization (CCUS) in the industries of electric power, steel, cement, chemical industry and the like, and plays a key role in energy conservation, emission reduction and greenhouse effect control. The carbon dioxide capture modes mainly include three types: pre-combustion capture (Pre-combustion), oxy-fuel combustion (Oxy-combustion), and Post-combustion capture (Post-combustion). At present, the post-combustion trapping technology in the industry mainly adopts a chemical absorption method, a physical absorption method and a membrane separation method. The chemical absorption method is the most common technology for separating carbon dioxide from flue gas after combustion at present, and takes alcohol amine, compound amine and the like as adsorbents, and the carbon dioxide is recycled by utilizing the absorption capacity of the adsorbents to the carbon dioxide under different pressure and temperature.
The low-temperature rectification method is to utilize the difference of the boiling points of all the components of the raw material gas and realize the separation of the raw material gas through a rectification tower, and the process has the advantages of low energy consumption, low operation cost and high separation efficiency, and is suitable for large-scale industrial production. At present, if the technology is adopted to purify carbon dioxide, devices such as a water chilling unit, an ammonia refrigeration system and the like are required to provide extra cold energy, the energy consumption is increased, and the process flow is relatively complex.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the above-mentioned not enough that exists among the prior art, and provide a carbon dioxide device is retrieved in cryogenic rectification purification that structural design is reasonable, directly utilize the feed gas as the refrigerant, provide cold volume through adopting carbon dioxide self high pressure throttle, do not need other devices to provide cold volume, the energy consumption is low, and process flow is simple reliable.
The utility model provides a technical scheme that above-mentioned problem adopted is: a device for purifying and recovering carbon dioxide by cryogenic rectification is characterized in that: the system comprises a compression unit, a desulfurization unit, a drying unit and a cryogenic rectification unit; the compression unit comprises a compressor and a cooler; the drying unit comprises an adsorber and an electric heater; the low-temperature rectification unit comprises a main heat exchanger, a subcooler, a reboiler, a rectification tower, a first throttling valve, a second throttling valve, a first gas-liquid separator, a second gas-liquid separator and a pressure-reducing and temperature-reducing device; the main heat exchanger is provided with a first cold runner, a second cold runner, a third cold runner and a hot runner; the subcooler is provided with a first cold runner, a second cold runner, a third cold runner, a first hot runner and a second hot runner; the inlet of the compressor is used for feeding raw material gas, the outlet of the compressor is connected with the inlet of the cooler, and the outlet of the cooler is connected with the desulfurization unit; the desulfurization unit is connected with the inlet of the adsorber, and the outlet of the adsorber is connected with the hot runner inlet of the main heat exchanger; the reboiler is connected with the rectifying tower; the hot runner outlet of the main heat exchanger is connected with the inlet of the reboiler, the outlet of the reboiler is connected with the second hot runner inlet of the subcooler, and the second hot runner outlet of the subcooler is connected with the inlet of the first gas-liquid separator through the first throttling valve; the liquid outlet of the first gas-liquid separator is connected with the reflux inlet of the rectifying tower, the gas outlet of the first gas-liquid separator is connected with the second cold runner inlet of the subcooler, the second cold runner outlet of the subcooler is connected with the second cold runner inlet of the main heat exchanger, the second cold runner outlet of the main heat exchanger is connected with the inlet of the electric heater, and the outlet of the electric heater is connected with the regeneration gas inlet of the adsorber; a gas outlet at the top of the rectifying tower is connected with a first hot runner inlet of the subcooler, and a first hot runner outlet of the subcooler is connected with an inlet of the second gas-liquid separator; the liquid outlet of the second gas-liquid separator is connected with the reflux liquid inlet of the rectifying tower; a gas outlet of the second gas-liquid separator is connected with a third cold runner inlet of the subcooler through a pressure-reducing and temperature-reducing device, and a third cold runner outlet of the subcooler is connected with a third cold runner inlet of the main heat exchanger; the liquid outlet of the rectifying tower is connected with the first cold runner inlet of the subcooler through a second throttling valve, the first cold runner outlet of the subcooler is connected with the first cold runner inlet of the main heat exchanger, and the first cold runner outlet of the main heat exchanger is connected with a carbon dioxide product pipe network.
The desulfurization unit of the utility model is a desulfurization bed.
Main heat exchanger and subcooler be plate-fin heat exchanger.
The cooler of the utility model is a water cooler.
The adsorbers of the utility model are two and are arranged in parallel.
The third cold runner exit linkage of main heat exchanger vacate.
Step-down heat sink include No. three choke valves and expander, no. three choke valves and expander are parallelly connected.
A vapour and liquid separator and No. two vapour and liquid separator all be located the top of rectifying column.
The rectifying tower is a plate-type rectifying tower or a filler rectifying tower.
Reboiler and rectifying column as an organic whole, the reboiler integration sets up the bottom at the rectifying column.
Compared with the prior art, the utility model, have following advantage and effect:
1. the utility model discloses a required cold volume of low temperature comes from the carbon dioxide and compresses the back throttle, need not extra refrigerant or refrigerating plant and provides the required cold volume of rectification, has reduced the configuration of refrigerant storage tank in refrigeration cycle, has reduced extra refrigeration cycle device, and complete equipment only has 1 compressor, makes whole flow simpler, the operation is reliable.
2. The utility model discloses a rectifying column carries out carbon dioxide purification, compares with the chemisorption method, has higher carbon dioxide rate of recovery, 93% carbon dioxide in the recoverable feed gas, and the unit energy consumption is low.
3. The utility model discloses a two-stage vapour and liquid separator can further improve the carbon dioxide rate of recovery.
4. The utility model discloses utilize the waste gas of separation feed gas as the regeneration gas of drying unit, need not additionally provide regeneration gas such as nitrogen gas.
5. The utility model discloses a rectifying column can adopt plate tower or packed column, and the rectification separation is effectual, and operation elasticity is big, can carry out the variable operating mode operation according to the feed gas condition.
6. The utility model discloses a reboiler can with the rectifying column synthesis arrange, low temperature rectification equipment is less in the cold box, and the cold box is arranged compactly, is favorable to designing into the sled piece, can obviously save the equipment investment and practice thrift and take up an area of.
7. The utility model discloses the choke valve is chooseed for use to the device, reduces the investment and convenient operation.
Therefore, the utility model has the advantages of the flow is simple, area is little, the investment economizes to the device energy consumption is low, and suitable for wide range, easily be suitable for, the carbon dioxide recovery that the carbon dioxide concentration that is particularly useful for chemical plant exhaust gas is between 60% ~ 90% is recycled.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
Detailed Description
The present invention will be described in further detail by way of examples with reference to the accompanying drawings, which are illustrative of the present invention and are not intended to limit the present invention.
The embodiment of the utility model provides a include four units of compression unit, desulfurization unit, drying unit and cryogenic rectification unit.
The compression unit comprises a compressor 1 and a cooler 2. The desulfurization unit is a desulfurization bed 3 filled with a desulfurizing agent. The drying unit comprises an adsorber 4 and an electric heater 5. The low-temperature rectification unit is arranged in the cold box 16 and comprises a main heat exchanger 6, a subcooler 7, a rectifying tower 8, a reboiler 9, a first throttling valve 10, a first gas-liquid separator 11, a second gas-liquid separator 12, a pressure-reducing and temperature-reducing device and a second throttling valve 15.
The main heat exchanger 6 has a first cold runner, a second cold runner, a third cold runner, and a hot runner. The subcooler 7 has a first cold runner, a second cold runner, a third cold runner, a first hot runner, and a second hot runner. The main heat exchanger 6 and the subcooler 7 are both vacuum brazing plate-fin heat exchangers.
The inlet of the compressor 1 is used for feeding the raw material gas 101, and the outlet is connected with the inlet of the cooler 2. The outlet of the cooler 2 is connected with the inlet of the desulfurization bed 3. The cooler 2 is a water cooler.
The outlet of the desulfurizing bed 3 is connected with the inlet of the adsorber 4, and the outlet of the adsorber 4 is connected with the hot runner inlet of the main heat exchanger 6. Two adsorbers 4 are arranged in parallel, the two adsorbers 4 are used alternately in pairs, one of which is in operation and the other of which is regenerated. The adsorber 4 can select a vertical axial flow bed layer, a horizontal or vertical radial flow bed layer according to the working pressure and the flow of the feed gas. Regeneration of the adsorber 4 is generally carried out in four steps, the first step: reducing the pressure; the second step: heating; the third step: cooling by blowing; the fourth step: after the four steps of pressure boosting and regeneration are finished, the adsorber can be put into operation, and after about 3 minutes of parallel operation, the switching process is finished.
The rectifying tower can be a plate rectifying tower or a filler rectifying tower, and the reboiler is a vacuum brazing type plate-fin heat exchanger. The reboiler 9 can be selectively integrated with the rectifying tower 8, and the reboiler 9 is integrally arranged at the bottom of the rectifying tower 8; the reboiler also can be selected as a shell-and-tube heat exchanger, is independently arranged outside the rectifying tower 8 and is connected with the rectifying tower 8 through a pipeline. The hot runner outlet of the main heat exchanger 6 is connected with the inlet of a reboiler 9, the outlet of the reboiler 9 is connected with the second hot runner inlet of the subcooler 7, and the second hot runner outlet of the subcooler 7 is connected with the inlet of a first gas-liquid separator 11 through a first throttling valve 10.
The liquid outlet at the bottom of the first gas-liquid separator 11 is connected with the reflux inlet at the top of the rectifying tower 9, the gas outlet at the top of the first gas-liquid separator 11 is connected with the second cold runner inlet of the subcooler 7, the second cold runner outlet of the subcooler 7 is connected with the second cold runner inlet of the main heat exchanger 6, the second cold runner outlet of the main heat exchanger 6 is connected with the inlet of the electric heater 5, and the outlet of the electric heater 5 is connected with the regeneration gas inlet of the adsorber 4. Two electric heaters 5 are selected, one electric heater is used, and the other electric heater is standby, so that the reliability of the process is improved.
And a gas outlet at the top of the rectifying tower 8 is connected with a first hot runner inlet of the subcooler 7, and a first hot runner outlet of the subcooler 7 is connected with an inlet of the second gas-liquid separator 12.
The liquid outlet at the bottom of the second gas-liquid separator 12 is connected with the reflux liquid inlet at the top of the rectifying tower 9. And a gas outlet at the top of the second gas-liquid separator 12 is connected with a third cold runner inlet of the subcooler 7 through a pressure-reducing and temperature-reducing device, and a third cold runner outlet of the subcooler 7 is connected with a third cold runner inlet of the main heat exchanger 6. The outlet of the third cold runner of the main heat exchanger 6 is connected to the vent. The pressure reduction and temperature reduction device comprises a third throttling valve 13 and an expansion machine 14, wherein the third throttling valve 13 is connected with the expansion machine 14 in parallel.
The liquid outlet at the bottom of the rectifying tower 8 is connected with the first cold runner inlet of the subcooler 7 through a second throttling valve 15, the first cold runner outlet of the subcooler 7 is connected with the first cold runner inlet of the main heat exchanger 6, and the first cold runner outlet of the main heat exchanger 6 is connected with a carbon dioxide product pipe network.
The first gas-liquid separator 11 and the second gas-liquid separator 12 are both positioned above the rectifying tower 8, and the second gas-liquid separator realizes that the separated liquid enters the rectifying tower again for rectification and separation by utilizing the height of a liquid column between the second gas-liquid separator and an inlet at the top of the rectifying tower.
A device and a method for recovering carbon dioxide by low-temperature rectification purification comprise the following steps:
1) The temperature of the raw material gas is 14 ℃, the pressure is 0.11MPa.A, and the flow rate is 76000Nm 3 The concentrations of the components in the raw material gas 21 are respectively as follows: 86.68% carbon dioxide, 10.96% N2, 1.43% H 2 O、0.48%CH 4 、0.18%C 2 H 4 、0.24%C 2 H 6 、0.03%C 3 H 8 、0.02% CO、2ppm COS、120ppm CH 3 And (5) OH. The raw material gas enters a compressor 1 for compression, is pressurized to 1.5-2.5 Mpa, then enters a cooler 2 for being cooled to normal temperature by circulating water, and then is sent into a desulfurization bed 3 for being separated from sulfur component impurities and then is sent into a drying unit.
2) In order to prevent sulfur components in the feed gas from corroding equipment and pipelines, the feed gas needs to be pretreated by an adsorption method before entering a cold box, so that sulfur in the components is removed; in order to prevent water molecules in the feed gas from freezing at low temperature and blocking a heat exchanger and a pipeline, the feed gas needs to be pretreated by an adsorption method before entering a cold box to remove water in components. When the feed gas passes through the adsorber 4 from bottom to top, H contained in the feed gas 2 O、C 2 H 2 After impurities are removed by adsorbent, the water content of purified raw material gas<1ppm。
3) The raw material gas dehydrated by the drying unit is sent to a main heat exchanger 6, is cooled to-10 ℃ by the return gas and then enters a reboiler 9 of the rectifying tower 8, and is cooled to-28 ℃ by liquid carbon dioxide at the bottom of the rectifying tower as a heat source of the rectifying tower 8 in the reboiler 9; the feed gas is further cooled to-55 ℃ to-60 ℃ by the return gas in the subcooler 7, is depressurized and cooled by a first throttle valve 10, is sent to a first gas-liquid separator 11, and is subjected to gas-liquid two-phase separation in the first gas-liquid separator 11.
4) The liquid carbon dioxide condensed at the bottom of the first gas-liquid separator 11 is sent to the top of the rectifying tower 9 to be rectified as reflux liquid, rectification and purification are carried out, the liquid carbon dioxide refined through purification is obtained at the bottom of the rectifying tower 8, the gas coming out of the top of the first gas-liquid separator 11 is reheated by the cooler 7 and the main heat exchanger 6 and then serves as the regeneration gas of the adsorber 4, the regeneration gas is heated to 180 ℃ through the electric heater 5 in the heating stage and then enters the adsorber 4, the regeneration gas directly enters the adsorber 4 in the cold blowing stage, and the gas is emptied from the high position after coming out of the adsorber 4.
5) And the crude gas obtained from the top of the rectifying tower 8 is cooled by the cooler 7 and then enters the second gas-liquid separator 12 for gas-liquid two-phase separation, and the liquid at the bottom of the second gas-liquid separator 12 enters the rectifying tower 8 from the top to participate in rectification. And the gas separated from the top of the second gas-liquid separator 12 is depressurized and cooled by a third throttling valve 13 or an expansion machine 14 to be used as cold fluid, and is discharged after cold energy is recovered in the subcooler 7 and the main heat exchanger 8.
6) And the carbon dioxide liquid with the purity of 99.91 percent obtained from the bottom of the rectifying tower 8 is depressurized to 0.35MPa.A through a second throttling valve 15, reheated by a cooler 7 and a main heat exchanger 6 and then sent to a carbon dioxide product pipe network.
In this embodiment, the purity of the final carbon dioxide product obtained by cryogenic rectification is 99.91% and the flow rate is 61600Nm 3 The carbon dioxide gaseous product with the pressure of 0.35MPa.A and the carbon dioxide recovery rate of the whole device reach 93 percent. The required cold energy comes from compression throttling refrigeration of the feed gas. The main power consumption equipment of the whole set of device is a carbon dioxide compressor and an electric heater, the power consumption of the device is 10958Kw, and the unit energy consumption for preparing carbon dioxide gaseous products is 0.09 Kw/kg.
Certain exemplary embodiments of the present invention have been described above by way of illustration only, and it will be apparent to those of ordinary skill in the art that the described embodiments may be modified in various different ways without departing from the spirit and scope of the present invention. Accordingly, the drawings and description are illustrative in nature and should not be construed as limiting the scope of the invention.
Claims (10)
1. A device for purifying and recovering carbon dioxide by low-temperature rectification is characterized in that: the system comprises a compression unit, a desulfurization unit, a drying unit and a cryogenic rectification unit; the compression unit comprises a compressor and a cooler; the drying unit comprises an adsorber and an electric heater; the low-temperature rectification unit comprises a main heat exchanger, a subcooler, a reboiler, a rectification tower, a first throttling valve, a second throttling valve, a first gas-liquid separator, a second gas-liquid separator and a pressure-reducing and temperature-reducing device; the main heat exchanger is provided with a first cold runner, a second cold runner, a third cold runner and a hot runner; the subcooler is provided with a first cold runner, a second cold runner, a third cold runner, a first hot runner and a second hot runner; the inlet of the compressor is used for feeding raw material gas, the outlet of the compressor is connected with the inlet of the cooler, and the outlet of the cooler is connected with the desulfurization unit; the desulfurization unit is connected with the inlet of the adsorber, and the outlet of the adsorber is connected with the hot runner inlet of the main heat exchanger; the reboiler is connected with the rectifying tower; the hot runner outlet of the main heat exchanger is connected with the inlet of the reboiler, the outlet of the reboiler is connected with the second hot runner inlet of the subcooler, and the second hot runner outlet of the subcooler is connected with the inlet of the first gas-liquid separator through a first throttling valve; the liquid outlet of the first gas-liquid separator is connected with the reflux inlet of the rectifying tower, the gas outlet of the first gas-liquid separator is connected with the second cold runner inlet of the subcooler, the second cold runner outlet of the subcooler is connected with the second cold runner inlet of the main heat exchanger, the second cold runner outlet of the main heat exchanger is connected with the inlet of the electric heater, and the outlet of the electric heater is connected with the regeneration gas inlet of the adsorber; a gas outlet at the top of the rectifying tower is connected with a first hot runner inlet of the subcooler, and a first hot runner outlet of the subcooler is connected with an inlet of the second gas-liquid separator; a liquid outlet of the second gas-liquid separator is connected with a reflux inlet of the rectifying tower; a gas outlet of the second gas-liquid separator is connected with a third cold runner inlet of the subcooler through a pressure-reducing and temperature-reducing device, and a third cold runner outlet of the subcooler is connected with a third cold runner inlet of the main heat exchanger; the liquid outlet of the rectifying tower is connected with the first cold runner inlet of the subcooler through a second throttling valve, the first cold runner outlet of the subcooler is connected with the first cold runner inlet of the main heat exchanger, and the first cold runner outlet of the main heat exchanger is connected with a carbon dioxide product pipe network.
2. The apparatus for purifying and recovering carbon dioxide by cryogenic rectification according to claim 1, wherein: the desulfurization unit is a desulfurization bed.
3. The apparatus for recovering carbon dioxide by cryogenic rectification purification according to claim 1, wherein: the main heat exchanger and the subcooler are plate-fin heat exchangers.
4. The apparatus for purifying and recovering carbon dioxide by cryogenic rectification according to claim 1, wherein: the cooler is a water cooler.
5. The apparatus for recovering carbon dioxide by cryogenic rectification purification according to claim 1, wherein: the number of the adsorbers is two, and the adsorbers are arranged in parallel.
6. The apparatus for recovering carbon dioxide by cryogenic rectification purification according to claim 1, wherein: and the outlet of the third cold runner of the main heat exchanger is connected with a vent.
7. The apparatus for purifying and recovering carbon dioxide by cryogenic rectification according to claim 1, wherein: the pressure reduction and temperature reduction device comprises a third throttling valve and an expansion machine, wherein the third throttling valve is connected with the expansion machine in parallel.
8. The apparatus for recovering carbon dioxide by cryogenic rectification purification according to claim 1, wherein: the first gas-liquid separator and the second gas-liquid separator are both positioned above the rectifying tower.
9. The apparatus for recovering carbon dioxide by cryogenic rectification purification according to claim 1, wherein: the rectifying tower is a plate rectifying tower or a filler rectifying tower.
10. The apparatus for recovering carbon dioxide by cryogenic rectification purification according to claim 1, wherein: the reboiler and the rectifying tower are integrated, and the reboiler is integrally arranged at the bottom of the rectifying tower.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202221520729.8U CN217661593U (en) | 2022-06-17 | 2022-06-17 | Device for purifying and recovering carbon dioxide by low-temperature rectification |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116271924A (en) * | 2023-05-19 | 2023-06-23 | 山西新微能源科技有限公司 | Carbon dioxide separation and purification device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116271924A (en) * | 2023-05-19 | 2023-06-23 | 山西新微能源科技有限公司 | Carbon dioxide separation and purification device |
| CN116271924B (en) * | 2023-05-19 | 2023-08-29 | 山西新微能源科技有限公司 | Carbon dioxide separation and purification device |
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