CN102895843A - System for recycling waste heat produced by methyl-diethanolamine (MDEA) decarburization process by using ultra high temperature heat pump - Google Patents
System for recycling waste heat produced by methyl-diethanolamine (MDEA) decarburization process by using ultra high temperature heat pump Download PDFInfo
- Publication number
- CN102895843A CN102895843A CN2012103617644A CN201210361764A CN102895843A CN 102895843 A CN102895843 A CN 102895843A CN 2012103617644 A CN2012103617644 A CN 2012103617644A CN 201210361764 A CN201210361764 A CN 201210361764A CN 102895843 A CN102895843 A CN 102895843A
- Authority
- CN
- China
- Prior art keywords
- solution
- mdea
- heat
- high temperature
- heat pump
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a system for recycling waste heat produced by a methyl-diethanolamine (MDEA) decarburization process by using an ultra high temperature heat pump. The system mainly comprises two procedures of MDEA decarburization and ultra high temperature heat pump working media. In the system, an evaporator of an ultra high temperature heat pump unit replaces original cooling water to decrease the temperature of a barren solution of the decarburization process to a required temperature, and the cooled barren solution absorbs CO2 of process gases; and a condenser of the ultra high temperature heat pump unit replaces original high temperature vapor. According to the system for recycling the waste heat produced by the MDEA decarburization process by using the ultra high temperature heat pump, by means of an ultra high temperature heat pump technology, technical bottlenecks of temperature limitation of original high temperature heat pumps are broken through, and recycling ranges of low temperature waste heat are greatly expanded. The ultra high temperature blending working media are used, and the waste heat produced by the MDEA decarburization process is utilized so that energy qualities are improved to meet requirements of high temperature heat required when an MDEA decarburization solution is regenerated. By means of the system, energy utilization ratios of the process are improved, and good energy-saving and economical effects are achieved.
Description
Technical field
The invention belongs to heat pump and decarburization chemical process technical field, specially refer to the superhigh temperature heat pump with technology and the device of MDEA decarbonization process in conjunction with utilization.
Background technology
The synthetic ammonia power consumption accounts for 40% of chemical industry total amount, is one of China's chemical industry five large high energy-consuming industries.In Ammonia Production, the decarbonization process energy consumption is approximately 10%～15% of total energy consumption.So it is very large that decarbonization process can save energy the space.Activation MDEA decarburization is the external BASF exploitation seventies and industrialization technology.This decarbonization process technology has that degree of purification is high, few, the regeneration CO of desulfurization and decarburization, nitrogen hydrogen loss amount simultaneously
2The advantages such as gas purity is high, solvent loss is few, difficult degraded.But the MDEA decarbonization process belongs to high energy consumption technique in numerous decarbonization process, and when comparing with techniques such as PSA, PC, steam consumption, power consumption etc. all is in a disadvantageous position.Under the overall background of energy-saving and emission-reduction, the energy consumption problem of MDEA decarbonization process needs to be resolved hurrily.
The decarburization of MDEA method utilizes MDEA solution cryogenic absorption CO exactly
2, high temperature desorption CO
2Principle realize.Under the condition of low temperature, the CO in the activation MDEA solution absorption process gas
2, absorb CO
2MDEA solution be called rich solution.Under the condition of high temperature, CO
2Parse from MDEA solution, solution is regenerated simultaneously, discharges CO
2MDEA solution be called lean solution.For realizing required environmental condition, adopt cooling water the high temperature rich solution to be down to the temperature (being down to 50 ℃～65 ℃ about 80 ℃) of demand in the conventional process flow, the MDEA solution after the cooling removes the CO of absorption technique gas
2, adopt high-temperature steam heating MDEA solution (rising to about 105 ℃ about 75 ℃), make its regeneration.In former technological process, cooling tower to air, not only needs to configure corresponding equipment with the dissipation of heat in the cooling water, also needs to consume the high-quality runnings that can realize equipment such as electric energy, and the waste heat of this part does not utilize, and also needs on the contrary to consume a large amount of energy; In addition, in the process of MDEA regeneration of waste liquor, need consume again a large amount of primary energy and produce steam for heating MDEA solution.This just means in the MDEA decarbonization process flow process and has not only consumed a large amount of energy, and its waste heat is rationally effectively utilized.
How the waste heat in the MDEA decarbonization process flow process is adequately and reasonably utilized, promoting can the matter quality, and the high-quality heat energy of generation is back to use in the MDEA decarbonization process flow process again, is one of the mode that should actively seek of MDEA decarbonization process.So not only greatly reduce the energy consumption of MDEA decarburization, but and environmental contamination reduction and thermal pollution.Heat pump techniques is realized one of effective technology means of this purpose just.Heat pump techniques is converted into high potential with the waste heat of MDEA decarbonization process, the MDEA solution in the high potential thermal regeneration process of generation, and cost is only for consuming the high-grade energy (electric energy, mechanical energy etc.) of small amount.So both can replace the equipment such as cooling tower of former technique, take full advantage of waste heat in the technique, can replace original steam again, reduce the consumption of the fossil fuels such as coal, indirectly improve the energy utilization rate of industrial flow.In general, the heat production temperature of high temperature heat pump is more than 65 ℃, and but below 100 ℃, but the high temperature of demand is 105 ℃ in the MDEA regeneration of waste liquor process of this technique, and therefore traditional high temperature heat pump is difficult to satisfy this process requirements.
Summary of the invention
In order to solve problems of the prior art, the invention provides a kind of system that adopts the superhigh temperature heat pump to recycle MDEA decarbonization process waste heat, the low grade residual heat that solves in the MDEA decarbonization process flow process can't utilize, and need consume again a large amount of primary energy and produce the wasting of resources problem that steam is used for heating MDEA solution.
Technical scheme of the present invention is as follows:
A kind of system that adopts the superhigh temperature heat pump to recycle MDEA decarbonization process waste heat mainly is coupled to form by MDEA decarburization and two flow processs of superhigh temperature heat pump fluid:
(1) MDEA decarburization flow process
MDEA decarburization flow process comprises the circulatory system that regenerator, condenser, evaporimeter, lean pump, absorption tower, flash column, solution heat exchanger are interconnected and form successively; The lean solution of regenerating in regenerator (about 105 ℃) enters solution heat exchanger, emit the part heat, lean solution after the cooling (about 80 ℃) enters evaporimeter again, emit heat, temperature is down to 50 ℃～65 ℃ lean solution enters the absorption tower after lean pump pressurization top, the CO in the lean solution absorption technique gas in the absorption tower
2, absorb CO
2MDEA solution become rich solution; Enter the top of flash column after the rich solution decompression of absorption tower bottom, liquid from top to bottom with steam and the CO of regenerator
2The gaseous mixture counter current contacting absorbs steam and CO
2The heat of gaseous mixture, behind packing layer, the CO of part in the rich solution
2Parse, rich solution becomes semi lean solution; The semi lean solution that goes out flash column is divided into two parts, wherein delivers to the middle part on absorption tower after most of semi lean solution pressurization, enters solution heat exchanger, the heat of recovery section lean solution after the pressurization of another part semi lean solution; Semi lean solution after the intensification enters the top of regenerator, through same steam and the CO from bottom to top of packing layer
2Gaseous mixture enters into condenser together, absorbs heat in condenser, and the temperature of semi lean solution rises to about 105 ℃ by about 75 ℃, and the semi lean solution after the intensification returns regenerator, parses the CO in the solution
2, become lean solution, recycle;
(2) superhigh temperature heat pump fluid flow process
Superhigh temperature heat pump fluid flow process mainly comprises compressor, expansion valve, condenser, evaporimeter and superhigh temperature heat pump fluid; The high-temperature gas cold-producing medium expands and the reduction pressure and temperature through expansion valve, the cold-producing medium of low-temp low-pressure enters evaporimeter, absorb the waste heat of lean solution and gasify, the low pressure refrigerant of gasification enters compressor and compresses, the cold-producing medium of exhaust outlet of compressor becomes high-temperature high-pressure state, and the cold-producing medium of HTHP enters the condenser condenses heat release and liquefies the MDEA decarbonizing solution in the condensation heat thermal regeneration process, make it reach technological requirement, the cold-producing medium of liquefaction enters expansion valve circular flow again.
Described high temperature refrigerant is mix refrigerant BY-4.The commodity northeast part of China by name 4# cold-producing medium, producer is cold-producing medium factory of University Of Tianjin.
In this system, the evaporimeter of superhigh temperature source pump replaces original cooling water, the lean solution temperature of decarbonization process is dropped to require temperature, and the lean solution after the cooling is removed the CO of absorption technique gas
2The condenser of superhigh temperature source pump replaces original high-temperature steam, satisfies MDEA regeneration of waste liquor process to the demand of high-quality heat.
The invention has the beneficial effects as follows: the present invention proposes a kind of system and device that adopts the superhigh temperature heat pump to recycle MDEA decarbonization process waste heat, the lift technique of UTILIZATION OF VESIDUAL HEAT IN and energy grade is organically combined with the MDEA decarbonization process.In this system and device, not only the low temperature exhaust heat that produces in the MDEA decarbonization process is reclaimed, and promoted the energy matter quality of waste heat by the superhigh temperature heat pump, the high-grade heat of generation satisfies the heat demand of MDEA regeneration of waste liquor in the technique.In this process, the superhigh temperature heat pump has higher Energy Efficiency Ratio (more than 3.5).Generally speaking, not only reduced the application of cooling water in the traditional handicraft, also reduce waste heat and be discharged into the thermal pollution that produces in the atmosphere, in addition, the high warm of generation again can be for the MDEA regeneration of waste liquor, reduce the use of high-temperature steam in the former technique, thereby reduced the consumption of the fossil fuels such as coal that produce steam and cause and the discharging of a large amount of pernicious gases.This system has not only improved the energy utilization rate of technological process, and well energy-conservation, economic effect is also arranged.
The superhigh temperature heat pump techniques that the present invention adopts has been broken through the technical bottleneck of original high temperature heat pump temperature limiting, has expanded greatly the recycling scope of low temperature exhaust heat.Adopt the superhigh temperature mixed working fluid, the waste heat that utilizes MDEA decarbonization process process to produce promotes energy matter quality, and needs is high warm when regenerating to satisfy the MDEA decarbonizing solution.
Description of drawings
Fig. 1 is that the present invention adopts the superhigh temperature heat pump to recycle the process chart of the system of MDEA decarbonization process waste heat;
Wherein 1---the absorption tower; 2---flash column; 3---solution heat exchanger; 4---regenerator; 5---condenser; 6---compressor; 7---expansion valve; 8---evaporimeter; 9---lean pump.
The specific embodiment
The system that the superhigh temperature heat pump is recycled MDEA decarbonization process waste heat carries out instance analysis with the MDEA decarbonization process that device is used for Gansu enterprise, and coupling system flow chart 1 is explained.
The lean solution (105 ℃) of regenerating in the regenerator 4 in this example enters solution heat exchanger 3, emits the part heat, and temperature is reduced to 80 ℃.80 ℃ lean solution enters evaporimeter 8, and the temperature of lean solution drops to 60 ℃ in the evaporimeter 8, and then lean solution is got back to lean pump 9 imports, squeezes into the CO in the 1 absorption technique gas of absorption tower
2, lean solution becomes rich solution.Rich solution enters steam and the CO of flash column 2 and regenerator 4
2The gaseous mixture counter current contacting absorbs heat, and the rich solution by flash column 2 parses part CO
2, rich solution becomes semi lean solution.Semi lean solution is divided into two parts, delivers to the middle part on absorption tower 1 after most of semi lean solution pressurization; Enter solution heat exchanger 3 after the pressurization of another part semi lean solution, absorb heat, the semi lean solution after the intensification enters regenerator 4 tops, and same steam and CO2 gaseous mixture from bottom to top enters into condenser 5 together.Semi lean solution enters absorption condensation heat in the condenser 5, and temperature rises to 105 ℃ by 75 ℃.Then, the semi lean solution after the intensification returns regenerator 4, parses the CO in the solution
2, become lean solution, recycle.This example adopts the superhigh temperature source pump with the exhaust-heat absorption of lean solution, has reduced the quantity of circulating water of cooling water in the former scheme, reduces operating cost and the cost of equipment of cooling water; The high warm MDEA decarbonizing solution in order to thermal regeneration that the unit condenser end produces has replaced the heating of high-temperature steam in the former scheme.
The cold-producing medium BY-4 of HTHP enters condenser 5, semi lean solution in the cold-producing medium liquefaction condensation heat release heating MDEA decarbonization process in the condenser 5, then cold-producing medium BY-4 enters expansion valve 7, the temperature and pressure of cold-producing medium all reduces in expansion valve 7, the cold-producing medium BY-4 of low-temp low-pressure enters evaporimeter 8, absorbs the heat of lean solution in the MDEA decarbonization process and gasifies; The low pressure refrigerant of gasification enters compressor 6 and compresses, and the high-pressure refrigerant after the compression enters condenser circular flow.
The COP of this programme moderate and high temperature heat is conservative, and value is 3.5, MDEA decarbonizing solution flow 170m
3/ h, specific heat capacity 1.29kcal/ (kg ℃).Can be calculated: the waste heat 4491.3kW of lean solution, intensification calorific requirement 3725.17kW during the regeneration of MDEA decarbonizing solution, pressing full up foot calculates for technique intensification heat 3725.17kW demand, need set up the source pump of 1064KW, heat pump need absorb waste heat 2660kW, can absorb from the lean solution cooling heat of about half.Annual economic benefit can reach more than 100 ten thousand yuan, in addition, also has good environmental benefit and energy-saving effect.Through conversion, can save more than 2200 ton in mark coal every year, CO
2More than 4900 ton of CER, SO
2More than 150 ton of CER, NO
xCER is more than 70 ton.
In general, the waste heat total amount of lean solution cooling is more, as long as go out the absorption portion waste heat from lean solution, just can satisfy the required heat of technique intensification.So unabsorbed lean solution waste heat still needs to adopt cooling water to cool off, but the water yield of cooling water but is far smaller than the cooling water water yield in the former technique, thereby has reduced the power consumption of cooling water circulation and reduced the costs of equipment such as cooling tower.In addition, can also utilize the superhigh temperature heat pump that the waste heat of lean solution is all utilized, a high warm part that produces is used for the heat demand of MDEA regeneration of waste liquor, rich high-quality heat also can be used for heating, domestic hot-water or other technological process etc., can save discharging and the thermal pollution of a large amount of pernicious gases of a large amount of high-quality energy, reduction primary energy burning generation.
Although by reference to the accompanying drawings the present invention has been carried out foregoing description; but the present invention is not limited to the above-mentioned specific embodiment; the above-mentioned specific embodiment only is schematic; rather than restrictive; those of ordinary skill in the art is under enlightenment of the present invention; in the situation that do not break away from aim of the present invention and claim institute protection domain, can also make a lot of distortion, these all belong to the row of protection of the present invention.
Claims (2)
1. a system that adopts the superhigh temperature heat pump to recycle MDEA decarbonization process waste heat is characterized in that, mainly is coupled to form by MDEA decarburization and two flow processs of superhigh temperature heat pump fluid:
(1) MDEA decarburization flow process
MDEA decarburization flow process comprises the circulatory system that regenerator, condenser, evaporimeter, lean pump, absorption tower, flash column, solution heat exchanger are interconnected and form successively; The lean solution of regenerating in regenerator enters solution heat exchanger, emits the part heat, and the lean solution after the cooling enters evaporimeter again, emits heat, then enters the top on absorption tower after the lean pump pressurization, the CO in the lean solution absorption technique gas in the absorption tower
2, absorb CO
2MDEA solution become rich solution; Enter the top of flash column after the rich solution decompression of absorption tower bottom, liquid from top to bottom with steam and the CO of regenerator
2The gaseous mixture counter current contacting absorbs steam and CO
2The heat of gaseous mixture, behind packing layer, the CO of part in the rich solution
2Parse, rich solution becomes semi lean solution; The semi lean solution that goes out flash column is divided into two parts, wherein delivers to the middle part on absorption tower after most of semi lean solution pressurization, enters solution heat exchanger, the heat of recovery section lean solution after the pressurization of another part semi lean solution; Semi lean solution after the intensification enters the top of regenerator, through same steam and the CO from bottom to top of packing layer
2Gaseous mixture enters into condenser together, absorbs heat in condenser, and the temperature of semi lean solution raises, and the semi lean solution after the intensification returns regenerator, parses the CO in the solution
2, become lean solution, recycle;
(2) superhigh temperature heat pump fluid flow process
Superhigh temperature heat pump fluid flow process mainly comprises compressor, expansion valve, condenser, evaporimeter and superhigh temperature heat pump fluid; The high-temperature gas cold-producing medium expands and the reduction pressure and temperature through expansion valve, the cold-producing medium of low-temp low-pressure enters evaporimeter, absorb the waste heat of lean solution and gasify, the low pressure refrigerant of gasification enters compressor and compresses, the cold-producing medium of exhaust outlet of compressor becomes high-temperature high-pressure state, and the cold-producing medium of HTHP enters the condenser condenses heat release and liquefies the MDEA decarbonizing solution in the condensation heat thermal regeneration process, make it reach technological requirement, the cold-producing medium of liquefaction enters expansion valve circular flow again.
2. described employing superhigh temperature heat pump is recycled the system of MDEA decarbonization process waste heat according to claim 1, it is characterized in that, described high temperature refrigerant is mix refrigerant BY-4.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210361764.4A CN102895843B (en) | 2012-09-24 | 2012-09-24 | System for recycling waste heat produced by methyl-diethanolamine (MDEA) decarburization process by using ultra high temperature heat pump |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210361764.4A CN102895843B (en) | 2012-09-24 | 2012-09-24 | System for recycling waste heat produced by methyl-diethanolamine (MDEA) decarburization process by using ultra high temperature heat pump |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102895843A true CN102895843A (en) | 2013-01-30 |
| CN102895843B CN102895843B (en) | 2015-02-25 |
Family
ID=47568511
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210361764.4A Expired - Fee Related CN102895843B (en) | 2012-09-24 | 2012-09-24 | System for recycling waste heat produced by methyl-diethanolamine (MDEA) decarburization process by using ultra high temperature heat pump |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102895843B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103977683A (en) * | 2014-04-30 | 2014-08-13 | 天津大学 | Method and device for reducing regeneration energy consumption of decarburization absorption liquid |
| CN104006568A (en) * | 2014-05-06 | 2014-08-27 | 江苏华昌化工股份有限公司 | New method for applying lithium bromide refrigerating device in nitrogenous fertilizer production |
| CN104974115A (en) * | 2014-04-02 | 2015-10-14 | 中国石油化工股份有限公司 | System and method for removing light components out of EO-enriched absorption water by EO/EG device |
| CN109027994A (en) * | 2018-07-18 | 2018-12-18 | 华北电力大学 | Utilize residual heat from boiler fume, decarburization waste heat and absorption heat pump coal generating system |
| CN115920601A (en) * | 2022-11-14 | 2023-04-07 | 河南中烟工业有限责任公司 | Moisture removing device for back-burning flue gas of boiler |
| CN117771892A (en) * | 2024-02-27 | 2024-03-29 | 安徽普泛能源技术有限公司 | System and coupling machine for thermally-driven carbon capture pressure boosting and refrigeration deep coupling |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101612512A (en) * | 2008-06-25 | 2009-12-30 | 苏庆泉 | Carbon dioxide separating system and separation method |
| CN101854988A (en) * | 2007-11-09 | 2010-10-06 | 环球油品有限责任公司 | Separator with multi-stage heat pump compressor and intermediate reboiler |
| WO2011069264A1 (en) * | 2009-12-09 | 2011-06-16 | University Of Regina | Alcohol-based gas stripping process |
| JP2012167918A (en) * | 2011-02-17 | 2012-09-06 | Babcock Hitachi Kk | Coal-fired boiler system including carbon dioxide recovery system |
-
2012
- 2012-09-24 CN CN201210361764.4A patent/CN102895843B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101854988A (en) * | 2007-11-09 | 2010-10-06 | 环球油品有限责任公司 | Separator with multi-stage heat pump compressor and intermediate reboiler |
| CN101612512A (en) * | 2008-06-25 | 2009-12-30 | 苏庆泉 | Carbon dioxide separating system and separation method |
| WO2011069264A1 (en) * | 2009-12-09 | 2011-06-16 | University Of Regina | Alcohol-based gas stripping process |
| JP2012167918A (en) * | 2011-02-17 | 2012-09-06 | Babcock Hitachi Kk | Coal-fired boiler system including carbon dioxide recovery system |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104974115A (en) * | 2014-04-02 | 2015-10-14 | 中国石油化工股份有限公司 | System and method for removing light components out of EO-enriched absorption water by EO/EG device |
| CN104974115B (en) * | 2014-04-02 | 2017-01-25 | 中国石油化工股份有限公司 | System and method for removing light components out of EO-enriched absorption water by EO/EG device |
| CN103977683A (en) * | 2014-04-30 | 2014-08-13 | 天津大学 | Method and device for reducing regeneration energy consumption of decarburization absorption liquid |
| CN104006568A (en) * | 2014-05-06 | 2014-08-27 | 江苏华昌化工股份有限公司 | New method for applying lithium bromide refrigerating device in nitrogenous fertilizer production |
| CN109027994A (en) * | 2018-07-18 | 2018-12-18 | 华北电力大学 | Utilize residual heat from boiler fume, decarburization waste heat and absorption heat pump coal generating system |
| CN109027994B (en) * | 2018-07-18 | 2023-08-29 | 华北电力大学 | Coal-fired power generation system utilizing boiler flue gas waste heat, decarbonizing waste heat and absorption heat pump |
| CN115920601A (en) * | 2022-11-14 | 2023-04-07 | 河南中烟工业有限责任公司 | Moisture removing device for back-burning flue gas of boiler |
| CN117771892A (en) * | 2024-02-27 | 2024-03-29 | 安徽普泛能源技术有限公司 | System and coupling machine for thermally-driven carbon capture pressure boosting and refrigeration deep coupling |
| CN117771892B (en) * | 2024-02-27 | 2024-06-04 | 安徽普泛能源技术有限公司 | System and coupling machine for thermally-driven carbon capture pressure boosting and refrigeration deep coupling |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102895843B (en) | 2015-02-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102895843B (en) | System for recycling waste heat produced by methyl-diethanolamine (MDEA) decarburization process by using ultra high temperature heat pump | |
| US8252091B2 (en) | CO2 recovery from IGCC power plants | |
| CN112126477A (en) | Carbon dioxide capture system and method based on blast furnace slag washing water waste heat recycling | |
| CN101856579B (en) | Novel energy-saving CO2 trapping process of improved potassium carbonate | |
| CN104948246A (en) | Method for capturing carbon dioxide in mineral smelting waste gas by making use of liquefied natural gas (LNG) cold energy | |
| CN109763948A (en) | A kind of supercritical carbon dioxide solar heat power generation system and operation method | |
| CN102732349A (en) | Method for producing liquefied natural gas | |
| CN104266454A (en) | Liquefied natural gas production system with gas-supercritical carbon dioxide united power | |
| CN102413901B (en) | Apparatus and method for compressing co2, system and method for separating and recovering co2 | |
| CN108795508A (en) | A method of detaching coke-stove gas using nitrogen and helium swell refrigeration | |
| CN101813398B (en) | Multi-mode thermochemical adsorption refrigeration device based on cascade utilization of energy | |
| CN111530238A (en) | Carbon dioxide capturing and utilizing system integrated with steel mill and using method thereof | |
| CN113149012A (en) | Method for extracting carbon dioxide by using blast furnace gas | |
| CN102989264A (en) | Afterheat recovery coupling system in high-temperature heat pump technology and cuprammonia refining process | |
| CN102698566A (en) | High and medium pressure regeneration system for flue gas decarbonization | |
| CN203545947U (en) | high-purity hydrogen production system, and synthetic ammonia system | |
| CN203572091U (en) | Heating-medium-water-driving ammonia and lithium bromide integrated absorption refrigeration device | |
| CN203443264U (en) | Device for extracting methane liquid from purified garbage landfill gas | |
| CN203240840U (en) | Energy saving system integrated by conversion section waste heat recovery and rectisol process refrigeration station | |
| CN103353207B (en) | Device for purifying methane liquid from purified landfill gas | |
| CN105091401A (en) | Jet absorption refrigerating device with copious cooling effect | |
| CN104651004A (en) | Energy-saving coal-based natural gas process | |
| CN103566712B (en) | A kind of smoke carbon dioxide capture technique | |
| CN210410096U (en) | Separation system for carbon dioxide in medium-high pressure gas source | |
| CN109737691B (en) | Air separation system of iron and steel enterprise |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150225 Termination date: 20210924 |