CN217220919U - CO 2 And N 2 Composite trapping and purifying system - Google Patents
CO 2 And N 2 Composite trapping and purifying system Download PDFInfo
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- CN217220919U CN217220919U CN202220965240.5U CN202220965240U CN217220919U CN 217220919 U CN217220919 U CN 217220919U CN 202220965240 U CN202220965240 U CN 202220965240U CN 217220919 U CN217220919 U CN 217220919U
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- 239000002131 composite material Substances 0.000 title claims description 16
- 238000010521 absorption reaction Methods 0.000 claims abstract description 36
- 238000001179 sorption measurement Methods 0.000 claims abstract description 27
- 238000000746 purification Methods 0.000 claims abstract description 17
- 230000005684 electric field Effects 0.000 claims abstract description 16
- 239000000428 dust Substances 0.000 claims abstract description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000005261 decarburization Methods 0.000 claims abstract description 10
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract 3
- 230000008929 regeneration Effects 0.000 claims description 59
- 238000011069 regeneration method Methods 0.000 claims description 59
- 239000007788 liquid Substances 0.000 claims description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 239000000498 cooling water Substances 0.000 claims description 10
- 238000005262 decarbonization Methods 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 84
- 239000003546 flue gas Substances 0.000 abstract description 11
- 238000000034 method Methods 0.000 abstract description 8
- 239000000126 substance Substances 0.000 abstract description 4
- 239000000243 solution Substances 0.000 description 16
- 230000000694 effects Effects 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 238000004134 energy conservation Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000006073 displacement reaction Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 239000000443 aerosol Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 239000012855 volatile organic compound Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000007791 dehumidification Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The utility model discloses a CO 2 And N 2 A combined capture and purification system comprising CO 2 Trapping the purified fraction and N 2 Trapping the purified part; n is a radical of 2 The trapping and purifying part comprises an electric field dust removing device, a decarburization gas compressor and N 2 Adsorption column and N 2 The compressor comprises an electric field dust removal device arranged at the top in the absorption tower and comprising high-frequency positive and negative electrode plates arranged at intervals, the decarburization gas compressor is connected with the output end of the decarburization gas at the top end of the absorption tower, and the output end of the decarburization gas compressor is connected with the N electrode plates 2 Adsorption column connection, N 2 N of adsorption tower 2 Output terminal and N 2 Input connection of compressor, N 2 Evacuation of the tail gas output of the adsorption column, N 2 Compressor output and N 2 The conveying pipelines are connected. The utility model adopts the chemical absorption method to capture CO 2 While N can be realized 2 The trapping and purification of the flue gas are particularly suitable for treating the mixed flue gas discharged by a coal-fired power plant.
Description
Technical Field
The utility model relates to a CO 2 A capture and purification system, in particular to CO 2 And N 2 A composite capturing and purifying system, which belongs to CO 2 The technical field of trapping.
Background
CCS(Carbon Capture&Storage, carbon capture and sequestration) technology to capture and recover CO 2 The chemical absorption method mainly adopts the selection of alkaline amine-based absorbentSelectively mixing with CO in flue gas 2 Chemical reaction to realize CO 2 Separated from other gases and regenerated by means of the reverse reaction of this reaction, releasing high-purity CO 2 The enrichment is carried out, and the flue gas has good adaptability, high capture efficiency and relatively mature technology, thereby being the most suitable for capturing CO on a large scale 2 One of the potential technical routes.
The main components of the flue gas of the coal-fired power plant except CO 2 In addition, it also includes N 2 、SO 2 、NO 2 Water vapor, and the like. Gas injection is commonly used in oil recovery to enhance oil recovery, while N 2 The compression coefficient is high, the expansibility is large, the volume coefficient is large, the seepage displacement is facilitated, and more oil gas can be displaced by injecting gas with the same volume, so that N 2 The method is widely applied to the aspect of oil exploitation. However, conventional CCS technology typically captures only recovered CO 2 Capture and recovery of CO 2 The post-decarbonation gas is usually purified and then directly discharged into the atmosphere, which results in functional singleness of the conventional CCS technology.
Disclosure of Invention
To the problems existing in the prior art, the utility model provides a CO 2 And N 2 The composite trapping and purifying system adopts a chemical absorption method to trap CO 2 While realizing N 2 Can be collected and purified, thereby realizing CO 2 And N 2 The resource application of the double waste gases is particularly suitable for treating mixed flue gas discharged by a coal-fired power plant.
To achieve the above object, the present CO 2 And N 2 The composite capture and purification system comprises CO 2 Trapping the purified fraction and N 2 Collecting the purified part;
CO 2 the trapping and purifying part comprises an absorption tower and a regeneration tower, a dry bed is arranged at the inner top of the absorption tower, a rich liquid discharge port at the bottom of the absorption tower is connected with a rich liquid input end at the top of the regeneration tower through a rich liquid pump and a pipeline, a regenerated gas discharge port at the top of the regeneration tower is connected with a regenerated gas input end of a regenerated gas separator, and CO at the top of the regenerated gas separator 2 Discharge port and CO 2 The bottom end of the regeneration tower is connected by a conveying pipelineThe barren solution discharge port is connected with a barren solution return port of the absorption tower below the dry bed through a barren solution pump;
N 2 the collecting and purifying part comprises an electric field dust removing device, a decarburization gas compressor and N 2 Adsorption column and N 2 The compressor, the electric field dust collector of the positive negative pole plate of high frequency including the interval setting sets up top in the absorption tower, and electric field dust collector is located the top of dry bed, and the input of decarbonization gas compressor passes through the pipeline and is connected with the decarbonization gas output on absorption tower top, and the output of decarbonization gas compressor passes through the pipeline and is connected with N 2 Input end connection of adsorption tower, N 2 N of adsorption tower 2 The output end is connected with N through a pipeline 2 Input connection of compressor, N 2 Evacuation of the tail gas output of the adsorption column, N 2 The output end of the compressor is connected with the N through a pipeline 2 The conveying pipelines are connected.
As a further improvement of the present invention, N 2 The adsorption tower comprises a plurality of adsorption towers which are arranged in parallel.
As a further improvement of the present invention, CO 2 The capturing and purifying part also comprises a lean-rich liquid heat exchanger and a reboiler, the pump-out end of a rich liquid pump is connected with the rich liquid input end at the top of the regeneration tower through the lean-rich liquid heat exchanger, a lean liquid circulation port at the bottom of the regeneration tower is connected with the reboiler through a circulation pipeline, the pump-out end of the lean liquid pump is connected with the input end of a heat exchange calandria of the lean-rich liquid heat exchanger through a pipeline, and the output end of the heat exchange calandria of the lean-rich liquid heat exchanger is connected with a lean liquid return port of the absorption tower below the dry bed through a lean liquid cooler.
As a further improvement of the utility model, the heat source of the reboiler is high temperature steam.
As a further improvement of the present invention, CO 2 The trapping and purifying part also comprises a regenerated gas compressor, a regenerated gas heat exchanger and a regenerated gas cooler, the input end of the regenerated gas compressor is connected with a regenerated gas discharge port at the top end of the regeneration tower through a pipeline, the output end of the regenerated gas compressor is connected with the input end of the regenerated gas cooler through the regenerated gas heat exchanger, and the output end of the regenerated gas cooler is connected with the regenerated gas of the regenerated gas separatorThe input ends are connected.
As a further improvement of the utility model, the regenerated gas heat exchanger is a circulating water cooling cooler which cools through circulating cooling water.
As the utility model discloses a further improvement scheme, the recirculated cooling water's of regeneration gas heat exchanger input and generating set bearing seal heater comdenstion water discharge end are connected, recirculated cooling water's output is connected with generating set low pressure feed water heater's input.
As a further improvement scheme of the utility model, the leakage fluid dram of regeneration gas separator bottom passes through the liquid return pump and is connected with the liquid return port at regenerator column top.
Compared with the prior art, the CO 2 And N 2 The composite capturing and purifying system captures CO by adopting a chemical absorption method 2 Meanwhile, the pressure swing adsorption process is utilized to separate the decarbonized flue gas discharged from the top of the absorption tower so as to realize N 2 To thereby effect CO purification 2 And N 2 Resource utilization of double waste gases; the absorption tower absorbs CO by utilizing a high-frequency electric field channel formed by an electric field dust removal device which is arranged at the top in the absorption tower and comprises high-frequency positive and negative electrode plates arranged at intervals 2 Deeply removing impurities and liquid drops from the decarbonized flue gas, and collecting small liquid and aerosol in the flue gas to reduce the loss of a solvent and the generation of VOCs; the large-temperature-difference heat exchange between the regenerated gas and the condensate water of the power plant is carried out after the regenerated gas is pressurized, so that the waste heat of the regenerated gas is fully recycled, the regeneration energy consumption and the cooling water consumption of the regenerated gas can be greatly reduced, the investment and the operation cost are saved, and the device is particularly suitable for treating the mixed flue gas discharged by the coal-fired power plant.
Drawings
Fig. 1 is a process flow diagram of the present invention.
In the figure: 1. absorption tower, 2, rich liquor pump, 3, lean and rich liquor heat exchanger, 4, regeneration tower, 5, lean liquor pump, 6, lean liquor cooler, 7, regeneration gas compressor, 8, regeneration gas heat exchanger, 9, regeneration gas cooler, 10, regeneration gas separator, 11, reboiler, 12, electric field dust removal device, 13, decarbonization gas compressor, 14, N 2 Adsorption column, 15, N 2 A compressor.
Detailed Description
The present invention will be further explained with reference to the accompanying drawings.
This CO 2 And N 2 The composite capture and purification system comprises CO 2 Trapping the purified fraction and N 2 The purified fraction is captured.
As shown in FIG. 1, CO 2 The trapping purification part comprises an absorption tower 1 and a regeneration tower 4, a dry bed is arranged at the inner top of the absorption tower 1, a rich liquid discharge port at the bottom of the absorption tower 1 is connected with a rich liquid input end at the top of the regeneration tower 4 through a rich liquid pump 2 and a pipeline, a regenerated gas discharge port at the top of the regeneration tower 4 is connected with a regenerated gas input end of a regenerated gas separator 10, and CO at the top of the regenerated gas separator 10 2 Discharge port and CO 2 The delivery pipe is connected, and the barren liquor discharging opening at the bottom end of the regeneration tower 4 is connected with a barren liquor return opening of the absorption tower 1 below the dry bed through a barren liquor pump 5.
N 2 The trapping and purifying part comprises an electric field dust removing device 12, a decarburization gas compressor 13 and N 2 Adsorption column 14 and N 2 A compressor 15, an electric field dust removing device 12 including high-frequency positive and negative electrode plates arranged at intervals is arranged at the top in the absorption tower 1, the electric field dust removing device 12 is positioned above the dry bed, the input end of the decarburization gas compressor 13 is connected with the output end of the decarburization gas at the top end of the absorption tower 1 through a pipeline, and the output end of the decarburization gas compressor 13 is connected with the N electrode plates through a pipeline 2 Input of the adsorption tower 14, N 2 N of adsorption column 14 2 The output end is connected with N through a pipeline 2 Input connection of compressor 15, N 2 Evacuation of the Tail gas output of the adsorption column 14, N 2 The output end of the compressor 15 is connected with N through a pipeline 2 The conveying pipelines are connected.
To achieve better N 2 Trapping effect, as a further improvement of the present invention, N 2 The adsorption tower 14 includes a plurality of adsorption towers arranged in parallel.
In order to realize energy conservation and consumption reduction and better CO 2 The trapping effect, as a further improvement of the present invention, is CO 2 The capture purification part also comprises a lean rich liquor heat exchanger 3 andthe reboiler 11, the pump-out end of the rich liquor pump 2 is connected with the rich liquor input end at the top of the regeneration tower 4 through the lean-rich liquor heat exchanger 3, the lean liquor circulation port at the bottom of the regeneration tower 4 is connected with the reboiler 11 through a circulation pipeline, the pump-out end of the lean liquor pump 5 is connected with the heat exchange calandria input end of the lean-rich liquor heat exchanger 3 through a pipeline, and the heat exchange calandria output end of the lean-rich liquor heat exchanger 3 is connected with the lean liquor return port of the absorption tower 1 below the dry bed through the lean liquor cooler 6.
In order to realize energy conservation and consumption reduction and better CO 2 The trapping effect, as a further improvement of the present invention, is CO 2 The trapping and purifying part also comprises a regenerated gas compressor 7, a regenerated gas heat exchanger 8 and a regenerated gas cooler 9, wherein the input end of the regenerated gas compressor 7 is connected with a regenerated gas discharge port at the top end of the regeneration tower 4 through a pipeline, the output end of the regenerated gas compressor 7 is connected with the input end of the regenerated gas cooler 9 through the regenerated gas heat exchanger 8, the regenerated gas heat exchanger 8 can adopt a circulating cooling water cooling mode, in order to further realize resource reutilization, energy conservation and consumption reduction, the input end of the circulating cooling water can be connected with the condensate water discharge end of a shaft seal heater of the generator set, the output end of the circulating cooling water can be connected with the input end of a low-pressure heater of the generator set, and the output end of the regenerated gas cooler 9 is connected with the regenerated gas input end of the regenerated gas separator 10.
In order to realize energy conservation and consumption reduction and better CO 2 The entrapment effect is regarded as the utility model discloses a further improvement scheme, and the leakage fluid dram accessible return liquid pump of regeneration gas separator 10 bottom is connected with the return liquid mouth at regeneration tower 4 tops.
This CO 2 And N 2 The process flow of the composite trapping and purifying system is as follows:
as shown in figure 1, flue gas subjected to desulfurization and denitrification at 40-50 ℃ enters an absorption tower 1 from bottom to top, a barren solution absorbent is sprayed from top to bottom and is in countercurrent contact with the barren solution absorbent to finish CO 2 The decarbonized gas goes upwards through an electric field channel between high-frequency positive and negative electrode plates of the electric field dust removing device 12 and then is discharged through a decarbonized gas output end at the top end of the absorption tower 1, aerosol and liquid drop particles in the gas flow are adsorbed and coalesced, and the high-efficiency impurity removal, dehumidification and smoke gas can be realizedReducing solvent loss and VOCs production.
The decarbonizing gas pressurized by the decarbonizing gas compressor 13 enters N 2 The adsorption tower 14 is used for separation and purification, and N after adsorption and purification 2 (≧ 99.9%) is composed of N 2 N in the top of the adsorption column 14 2 The output end enters N 2 The compressor 15 is pressurized and then enters N 2 Conveying to N by a conveying pipeline 2 And in the oil displacement block, exhausting the residual tail gas to the atmosphere.
Absorb CO 2 The rich solution (50-55 ℃) of the gas is discharged from the bottom of the absorption tower 1, the gas enters a lean rich solution heat exchanger 3 for heat exchange after being pressurized by a rich solution pump 2, the gas enters the upper part of a regeneration tower 4 for spray desorption after the heat exchange (the temperature of the rich solution is 90-100 ℃) and is heated and regenerated by a reboiler 11, and the heat source of the reboiler 11 can come from steam (0.3MPag, 144 ℃) in a plant area.
And discharging the regenerated barren solution (100-110 ℃) from a barren solution discharge outlet at the bottom end of the regeneration tower 4, pressurizing the barren solution by a barren solution pump 5, then entering a barren and rich solution heat exchanger 3 for heat exchange, entering a barren solution cooler 6 for cooling the barren solution (60-65 ℃) after heat exchange to 40 ℃, and then entering an absorption tower 1 for cyclic absorption.
The regeneration gas (10-20 kPag, 95-100 ℃) discharged from a regeneration gas discharge port at the top end of the regeneration tower 4 is pressurized by a regeneration gas compressor 7 (20-40 kPag, 120-140 ℃) and enters a regeneration gas heat exchanger 8 to exchange heat with condensate water (40-50 ℃) from a generator set heater, the condensate water (80-90 ℃) after recovering the heat of the regeneration gas reenters an inlet of a low-pressure heater of the generator set to be recycled, the regeneration gas (80-85 ℃) after heat exchange enters a regeneration gas cooler 9 to be cooled to 40 ℃ and then enters a regeneration gas separator 10, water separated from the bottom of the regeneration gas separator 10 can be directly discharged into an underground groove, and CO separated from the upper part of the regeneration gas separator 10 2 (≥ 95%) may be passed through CO 2 The CO enters the compressor after the pressure boost dehydration 2 Transport pipe to CO 2 And injecting the oil displacement block.
Claims (8)
1. CO (carbon monoxide) 2 And N 2 The composite capture and purification system is characterized by comprising CO 2 Collecting and purifying partIs divided by N 2 Collecting the purified part;
CO 2 the trapping purification part comprises an absorption tower (1) and a regeneration tower (4), a dry bed is arranged at the inner top of the absorption tower (1), a rich liquid discharge port at the bottom of the absorption tower (1) is connected with a rich liquid input end at the top of the regeneration tower (4) through a rich liquid pump (2) and a pipeline, a regenerated gas discharge port at the top of the regeneration tower (4) is connected with a regenerated gas input end of a regenerated gas separator (10), and CO at the top of the regenerated gas separator (10) 2 Discharge port and CO 2 The delivery pipeline is connected, and a barren liquor discharge port at the bottom end of the regeneration tower (4) is connected with a barren liquor return port of the absorption tower (1) below the dry bed through a barren liquor pump (5);
N 2 the trapping and purifying part comprises an electric field dust removing device (12), a decarburization gas compressor (13) and N 2 Adsorption column (14) and N 2 Compressor (15), electric field dust collector (12) including the positive negative pole electrode plate of high frequency that the interval set up top in absorption tower (1), and electric field dust collector (12) are located the top of dry bed, and the input of decarbonization gas compressor (13) passes through the pipeline and is connected with the decarbonization gas output on absorption tower (1) top, and the output of decarbonization gas compressor (13) passes through the pipeline and N and export the pipeline and N 2 The input ends of the adsorption towers (14) are connected, N 2 N of adsorption column (14) 2 The output end is connected with N through a pipeline 2 Input connection of a compressor (15), N 2 Evacuation of the tail gas output of the adsorption column (14), N 2 The output end of the compressor (15) is connected with the N through a pipeline 2 The conveying pipelines are connected.
2. CO according to claim 1 2 And N 2 The composite capture and purification system is characterized in that N 2 The adsorption column (14) includes a plurality of adsorption columns arranged in parallel.
3. CO according to claim 1 2 And N 2 The composite capture and purification system is characterized in that CO 2 The capturing and purifying part also comprises a lean-rich liquid heat exchanger (3) and a reboiler (11), the pump-out end of the rich liquid pump (2) is connected with the rich liquid input end at the top of the regeneration tower (4) through the lean-rich liquid heat exchanger (3), and a lean liquid circulating port at the bottom of the regeneration tower (4) is connected with the lean liquid input end at the top of the regeneration tower (4) through a circulating portThe ring pipeline is connected with the reboiler (11), the pump-out end of the barren liquor pump (5) is connected with the input end of the heat exchange calandria of the barren and rich liquor heat exchanger (3) through a pipeline, and the output end of the heat exchange calandria of the barren and rich liquor heat exchanger (3) is connected with a barren liquor return port of the absorption tower (1) below the dry bed through a barren liquor cooler (6).
4. CO according to claim 3 2 And N 2 The composite capture purification system is characterized in that the heat source of the reboiler (11) is high-temperature steam.
5. CO according to claim 1 2 And N 2 The composite capture and purification system is characterized in that CO 2 The trapping and purifying part further comprises a regeneration gas compressor (7), a regeneration gas heat exchanger (8) and a regeneration gas cooler (9), the input end of the regeneration gas compressor (7) is connected with a regeneration gas discharge port at the top end of the regeneration tower (4) through a pipeline, the output end of the regeneration gas compressor (7) is connected with the input end of the regeneration gas cooler (9) through the regeneration gas heat exchanger (8), and the output end of the regeneration gas cooler (9) is connected with the regeneration gas input end of the regeneration gas separator (10).
6. CO according to claim 5 2 And N 2 The composite capture purification system is characterized in that the regeneration gas heat exchanger (8) is a circulating water cooling cooler which cools through circulating cooling water.
7. CO according to claim 6 2 And N 2 The composite capturing and purifying system is characterized in that the input end of circulating cooling water of a regenerated gas heat exchanger (8) is connected with the condensed water discharge end of a shaft seal heater of a generating set, and the output end of the circulating cooling water is connected with the input end of a low-pressure heater of the generating set.
8. CO according to claim 1 2 And N 2 The composite trapping and purifying system is characterized in that a liquid outlet at the bottom end of the regeneration gas separator (10) is connected with a liquid return port at the top of the regeneration tower (4) through a liquid return pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220965240.5U CN217220919U (en) | 2022-04-25 | 2022-04-25 | CO 2 And N 2 Composite trapping and purifying system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202220965240.5U CN217220919U (en) | 2022-04-25 | 2022-04-25 | CO 2 And N 2 Composite trapping and purifying system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116585868A (en) * | 2023-03-13 | 2023-08-15 | 中国矿业大学 | Integrated process for capturing carbon dioxide and preparing urea |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116585868A (en) * | 2023-03-13 | 2023-08-15 | 中国矿业大学 | Integrated process for capturing carbon dioxide and preparing urea |
| CN116585868B (en) * | 2023-03-13 | 2023-10-31 | 中国矿业大学 | Integrated process for capturing carbon dioxide and preparing urea |
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Granted publication date: 20220819 |