CN102442667A - Catching and refining device of carbon dioxide gas - Google Patents
Catching and refining device of carbon dioxide gas Download PDFInfo
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- CN102442667A CN102442667A CN2011102966925A CN201110296692A CN102442667A CN 102442667 A CN102442667 A CN 102442667A CN 2011102966925 A CN2011102966925 A CN 2011102966925A CN 201110296692 A CN201110296692 A CN 201110296692A CN 102442667 A CN102442667 A CN 102442667A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 79
- 238000007670 refining Methods 0.000 title claims abstract description 16
- 239000001569 carbon dioxide Substances 0.000 title abstract description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 title abstract description 24
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 43
- 235000011089 carbon dioxide Nutrition 0.000 claims abstract description 31
- 238000000746 purification Methods 0.000 claims abstract description 24
- 238000005057 refrigeration Methods 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 239000007787 solid Substances 0.000 claims abstract description 6
- 238000003860 storage Methods 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 63
- 238000010521 absorption reaction Methods 0.000 claims description 30
- 239000000047 product Substances 0.000 claims description 24
- 229930195733 hydrocarbon Natural products 0.000 claims description 21
- 150000002430 hydrocarbons Chemical class 0.000 claims description 21
- 241000196324 Embryophyta Species 0.000 claims description 15
- 238000004821 distillation Methods 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 4
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims description 4
- 235000015320 potassium carbonate Nutrition 0.000 claims description 4
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 3
- 239000010962 carbon steel Substances 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 239000012263 liquid product Substances 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 235000013305 food Nutrition 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 49
- 238000004519 manufacturing process Methods 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 238000006477 desulfuration reaction Methods 0.000 description 7
- 230000023556 desulfurization Effects 0.000 description 7
- 235000003599 food sweetener Nutrition 0.000 description 6
- 239000003765 sweetening agent Substances 0.000 description 6
- 238000006555 catalytic reaction Methods 0.000 description 5
- 239000012535 impurity Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 4
- 230000008859 change Effects 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 235000013334 alcoholic beverage Nutrition 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 235000013405 beer Nutrition 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 235000013361 beverage Nutrition 0.000 description 1
- 229910052796 boron Inorganic materials 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
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- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 235000012055 fruits and vegetables Nutrition 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 238000005058 metal casting Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
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Abstract
The invention discloses a catching and refining device of a carbon dioxide gas, which is composed of a blower, a compressor, an enrichment system, a desulphurization system, a de-hydrocarbon system, a purification system, a refrigeration system, a rectification system and a product system. The front end of the enrichment system is connected with the blower while the rear end thereof is connected with the desulphurization system; the rear end of the desulphurization system is connected with the de-hydrocarbon system; the rear end of the de-hydrocarbon system is connected with the purification system; the rear end of the purification system is connected with the refrigeration system; the rear end of the refrigeration system is connected with the rectification system; and the rear end of the rectification system is connected with the product system. Raw gas containing carbon dioxide is led to the enrichment system through the blower, then pressurized by the compressor and then enters into a desulphurizer and a de-hydrocarbon device for desulphurization and de-hydrocarbon; the purified carbon dioxide then enters in the refrigeration system; then the purified carbon dioxide after being liquefied enters into the rectification system and sent to a food-level carbon dioxide storage tank for storage. The liquid carbon dioxide products can be en-trucked or bottled for sale and also can be further made into solid dry ice through a dry ice machine.
Description
Technical field
Dioxide gas of the present invention is caught and refining plant relates to chemical production equipment, the manufacturing equipment of specifically a kind of food-class liquid CO 2 and dry ice.
Background technology
Carbonic acid gas is a kind of very valuable carbon resource at present, can be widely used in multiple field.Industries such as chemosynthesis industry, mechanical protection welding, metal casting processing, agricultural fertilizer, fruit and vegetable using are fresh-keeping, beer beverage can, oil production, fire-fighting fire extinguishing, medical and health all need carbonic acid gas.And the gas source of China's carbonic acid gas is very abundant: the hydrogen manufacturing of Organic Chemical Plant, terepthaloyl moietie production; The conversion gas of inorganic chemical industry factory, Ammonia Production; The grain fermentation brews alcoholic beverages, and ores such as calcium, magnesium decompose, and boron ore powder carbon is separated; Associated gas, stack gas of coal combustion or heavy oil or the like all contains a certain amount of carbonic acid gas.Carbon dioxide content in these virgin gass is different, and from 10%-90%, wherein ingredient is also different, contains plurality of impurities.New food-grade carbon-dioxide national standard 10621-2006 has strict demand to 22 indexs.Original manufacturing carbonic acid gas method is fairly simple, most of just rejects to a certain impurity composition wherein, and the product of producing is impure many; Not pure especially; Especially for the carbon dioxide product of food service industry, require relatively strictness, manufacture relatively difficulty.To existing problem in the above-mentioned prior art, a kind of novel dioxide gas of research and design is caught and refining plant, and existing problem is very necessary in the prior art thereby overcome.
Summary of the invention
In view of existing problem in the above-mentioned prior art, the objective of the invention is a kind of novel dioxide gas of research and design and catch and refining plant, thereby it is fairly simple to solve original manufacturing carbonic acid gas method; Most of just reject to a certain impurity composition wherein; The product of producing is impure many, is not pure especially, especially for the carbon dioxide product of food service industry; Require relatively strictlyer, manufacture relatively problems such as difficulty.
Dioxide gas of the present invention is caught and refining plant, is made up of gas blower, compressor, enrichment system, desulphurization system, de-hydrocarbon system, purification system, refrigeration system, distillation system and product systems.The front end of described enrichment system connects gas blower; The enrichment system rear end connects desulphurization system; The desulphurization system rear end connects de-hydrocarbon system, the de-hydrocarbon system rear end connects purification system, purification system rear end connection refrigeration system, refrigeration system rear end connection distillation system, and the distillation system rear end connects product systems.Described enrichment system comprises water wash column, tank, water pump, lean pump, rich solution pump, absorption tower, separator, regenerator column, skimmer, thermal source.The unstripped gas of being sent here by gas blower gets into water wash column, is provided with tank below the water wash column, and tank connects water pump; Water pump is sent the water in the tank into water wash column; The outlet of water wash column upper end is connected to the bottom on absorption tower, and the outlet of upper end, absorption tower is connected to separator, and the outlet of separator is connected to the top on absorption tower; The outlet at bottom on absorption tower is connected to the top of regenerator column through the rich solution pump; Regenerator column top outlet is connected to skimmer, the outlet at bottom of skimmer be connected with the regenerator column outlet at bottom and through lean pump be connected to top, absorption tower after the outlet at bottom of separator is connected, the top exit of skimmer is connected to the inlet of compressor.Thermal source is to be the regenerator column heating.Described desulphurization system comprises first water trap, first devulcanizer, second devulcanizer.The outlet of compressor is connected to first water trap, and the first water trap top exit is connected to first devulcanizer and second devulcanizer inlet, and first devulcanizer and second devulcanizer export the output that links together.Described de-hydrocarbon system comprises interchanger, well heater, takes off the hydrocarbon device.The gas of being come in by desulphurization system gets into the top of interchanger; The bottom of interchanger is connected to the bottom of well heater; The top outlet of well heater is connected to takes off hydrocarbon device top inlet, takes off hydrocarbon device outlet at bottom and is connected to the interchanger upper entrance, the output of interchanger lower part outlet.Described purification system comprises water cooler, second water trap, first cleaner, second cleaner.The gas of being come in by de-hydrocarbon system gets into second water trap behind water cooler, the second water trap top exit is connected to first cleaner and second cleaner top inlet, the output that links together of first cleaner and the second cleaner outlet at bottom.Described refrigeration system comprises condensing surface, refrigerator.By gas output after condenser condenses liquefaction that purification system is come in, refrigerator provides refrigeration to condensing surface.Described distillation system comprises rectifying tower.Described product systems comprise liquid product storage tank and the solid, dry ice maker that is connected.
Used absorption liquid is for showing the absorption agent of alkalescence, like salt of wormwood or varies in absorption tower of the present invention and the regenerator column.
The mode of connection of first devulcanizer and second devulcanizer is that SP is connected in the desulphurization system of the present invention, and first devulcanizer and second devulcanizer inlet is connected, export and be connected, and outlet and enter the mouth between also link together.When desulfurizer moves first, can drive first devulcanizer earlier, connect with second devulcanizer when treating first devulcanizer outlet sulphur content near index; Second devulcanizer outlet sulphur content near index before, should reserve certain hour and stop first devulcanizer and change sweetening agent, change back first devulcanizer as new second devulcanizer; Second devulcanizer is as new first devulcanizer; Recycle, both can guarantee the quality of desulfurization product gas, can guarantee the Sulfur capacity of sweetening agent again; Sweetening agent is changed and can under the condition of not stopping, be carried out, thus the operation of safeguards system steady and continuous.This mode had both guaranteed desulfurization precision, guaranteed continuous production again, can be flexible and changeable as the case may be.
Dry ice machine of the present invention is through the ingress of pipe connection to compressor.Reclaim being discharged into carbon dioxide in air, deliver to compressor and further handle, improved the recovery of carbonic acid gas.
First cleaner of the present invention and the second cleaner material are that carbon steel adds stainless steel lining.
Equipment entrance of the present invention all is equipped with valve with outlet.
Take off the mode of connection of hydrocarbon device and interchanger, well heater in the de-hydrocarbon system of the present invention, take off hydrocarbon reaction and carry out at 300～350 ℃, electric heater starts when beginning; This reaction is for thermopositive reaction, if hydro carbons is more in the virgin gas, exothermic heat of reaction can ensure that catalysis takes off the hydrocarbon device and normally move; Need not to start electric heater, de-hydrocarbon system does not have power consumption, and energy consumption is low; Purify CH in the virgin gas through the catalysis de-hydrocarbon system
4, ethane, propane, benzene etc. all is converted into CO
2And H
2O is reaching the purification target simultaneously, newly-generated CO
2And the reduction of rectification and purification emptying amount, not only significantly improve product purity, can also increase liquid CO
2Output, alleviate the processing load of follow-up workshop section simultaneously.
Dioxide gas seizure of the present invention and refining plant working process are following: virgin gas is introduced water wash column dedusting cooling through gas blower, further gets into the absorption tower, and wherein a part of carbonic acid gas is by solvent absorbing; Tail gas such as nitrogen enter atmosphere by cat head, the rich solution behind the absorbing carbon dioxide by tower at the bottom of through being pumped into regenerator column, from rich solution, separate the sucking-off carbonic acid gas through heating; Not carbonated lean solution is gone out by the regenerator column underflow; With being pumped into the absorption tower, dioxide gas separates and removes liquid after overcooling; This moment, the content of carbonic acid gas was about 90%, sent into compressor boost to 2.2～3.2Mpa.Dioxide gas after the supercharging gets into devulcanizer after dividing water, through the method desulfurization of adsorption catalysis oxidation, makes total sulfur in the virgin gas less than 0.1ppm, and sulfurous gas is less than 1.0ppm.Gas converting heat after gas after the desulfurization gets into interchanger and takes off hydrocarbon; Take off the hydrocarbon device and take off hydrocarbon reaction through getting into after the heater heats to 300 ℃ again, hydrocarbons such as methane, ethane, ethene, benzene and hydrogen all are converted into carbonic acid gas and water through oxidizing fire, carbonic acid gas after the purification and the virgin gas heat exchange after the desulfurization; Get into cleaner after dividing water through the water cooler cooling then; Further remove impurity such as water, get into condensing surface again and utilize the cold of refrigerator generation to be cooled to-10 ℃～-20 ℃ liquefaction, the liquefaction back gets in the rectifying tower; Cat head is isolated non-condensable gasess such as oxygen, nitrogen; Carbon dioxide purity reaches more than 99.99% at the bottom of the tower, reaches the state food grade standard, is depressured to 2.2Mpa through throttling; Deliver in the food-grade carbon-dioxide basin and store; The liquid carbon dioxide product can be sold through entrucking or bottling, also can further produce solid-state dry ice through the dry ice machine, and the gaseous carbon dioxide that produces when producing dry ice is connected to sneak in the virgin gas before the compressor through pipeline and recycles.
The advantage of this device is to carbonic acid gas different material source, carries out the multiple systems path combination, produces liquid and solid-state food grade carbon-dioxide product, and is flexible and changeable, production efficiency is high, quality product is high.
This device fore portion capturing carbon dioxide adopts chemical process, and use shows the solution of alkalescence, absorbs earlier like materials such as salt of wormwood, thanomins and afterwards meets heat release, has improved the gas concentration lwevel in the virgin gas, and is simple and practical.Two devulcanizer series/parallel operations are partly adopted in desulfurization, when desulfurizer moves first, can drive first devulcanizer earlier; Connect with second devulcanizer when treating first devulcanizer outlet sulphur content near index, second devulcanizer export sulphur content near index before, should reserve certain hour and stop first devulcanizer; Change sweetening agent, change back first devulcanizer as new second devulcanizer, second devulcanizer is as new first devulcanizer; Recycle, both can guarantee the quality of desulfurization product gas, can guarantee the Sulfur capacity of sweetening agent again; Sweetening agent is changed and can under the condition of not stopping, be carried out, thus the operation of safeguards system steady and continuous; Take off hydrocarbon reaction and carry out at 300～350 ℃, electric heater starts when beginning, and this reaction is for thermopositive reaction, if hydro carbons is more in the virgin gas; Exothermic heat of reaction can ensure that catalysis takes off the hydrocarbon device and normally move, and need not to start electric heater, and de-hydrocarbon system does not have power consumption; Energy consumption is low, purifies methane, ethane, ethene, benzene in the virgin gas through the catalysis de-hydrocarbon system; Hydrogen etc. all are converted into carbonic acid gas and water, when reaching the purification target, and the reduction of newly-generated carbonic acid gas and rectification and purification emptying amount; Not only significantly improve product purity, can also increase the output of Liquid carbon dioxide, alleviate the processing load of follow-up workshop section simultaneously.When producing dry ice, before the gaseous carbon dioxide of generation turns back to compressor, improved the production efficiency of dry ice greatly.
The present invention is directed to carbonic acid gas different material source, and the high purity of liquid and solid carbon dioxide product, a whole set of carbon dioxide capture purification techniques is provided, the carbon dioxide recovery in the various different industrial gaseous wastees is utilized again.According to the difference of impurity composition in the virgin gas and content, and the difference of product requirement, the integral part in the native system is adjusted, to the different system of different source of the gas combinations, produce specification product.The present invention has multiple systems path combination, flexible and changeable, advanced technology, energy consumption is low, production efficiency is high, cover multiple gases source, characteristics such as quality product height.
Description of drawings
The present invention has a width of cloth accompanying drawing,
Fig. 1 is that dioxide gas is caught and the refining plant structural representation.
Among the figure: 1; Gas blower 2; Water wash column 3; Tank 4; Water pump 5; Lean pump 6; Rich solution pump 7; Absorption tower 8; Separator 9; Regenerator column 10; Skimmer 11; Thermal source 12; Compressor 13; First water trap 14; First devulcanizer 15; Second devulcanizer 16; Interchanger 17; Well heater 18; Take off hydrocarbon device 19; Water cooler 20; Second water trap 21; First cleaner 22; Second cleaner 23; Condensing surface 24; Refrigerator 25; Rectifying tower 26; Storage tank 27; The solid, dry ice maker.
Embodiment
For example shown in the accompanying drawing, dioxide gas is caught and refining plant is made up of gas blower 1, compressor 12, enrichment system, desulphurization system, de-hydrocarbon system, purification system, refrigeration system, distillation system and product systems in practical implementation of the present invention.The front end of described enrichment system connects gas blower 1; The enrichment system rear end connects desulphurization system; The desulphurization system rear end connects de-hydrocarbon system, the de-hydrocarbon system rear end connects purification system, purification system rear end connection refrigeration system, refrigeration system rear end connection distillation system, and the distillation system rear end connects product systems.Described enrichment system comprises water wash column 2, tank 3, water pump 4, lean pump 5, rich solution pump 6, absorption tower 7, separator 8, regenerator column 9, skimmer 10, thermal source 11.The unstripped gas of being sent here by gas blower 1 gets into water wash column 2; Be provided with tank 3 below the water wash column 2; Tank 3 connects water pump 4, and water pump 4 is sent the water of 3 li of tanks into water wash column 2, and the outlet of water wash column 2 upper ends is connected to the bottom on absorption tower 7; The outlet of 7 upper ends, absorption tower is connected to separator 8; The outlet of separator 8 is connected to the top on absorption tower 7, and the outlet at bottom on absorption tower 7 is connected to the top of regenerator column 9 through rich solution pump 6, and regenerator column 9 top exits are connected to skimmer 10; The outlet at bottom of skimmer 10 be connected with regenerator column 9 outlet at bottoms and through lean pump 5 be connected to 7 tops, absorption tower after the outlet at bottom of separator 8 is connected, the top exit of skimmer 10 is connected to the inlet of compressor 12.Thermal source 11 is to be regenerator column 9 heating.Described desulphurization system comprises first water trap 13, first devulcanizer 14, second devulcanizer 15; The outlet of compressor 12 is connected to first water trap, 13, the first water traps, 13 top exits and is connected to first devulcanizer 14 and second devulcanizer, 15 inlets, and first devulcanizer 14 and second devulcanizer 15 export the output that links together.Described de-hydrocarbon system comprises interchanger 16, well heater 17, takes off hydrocarbon device 18.The gas of being come in by desulphurization system gets into the top of interchanger 16; The bottom of interchanger 16 is connected to the bottom of well heater 17; The top outlet of well heater 17 is connected to takes off hydrocarbon device 18 tops inlet, takes off hydrocarbon device 18 outlet at bottoms and is connected to interchanger 16 upper entrances, the output of interchanger 16 lower part outlets.Described purification system comprises water cooler 19, second water trap 20, first cleaner 21, second cleaner 22.The gas of being come in by de-hydrocarbon system gets into second water trap 20 behind water cooler 19; Second water trap, 20 top exits are connected to first cleaner 21 and second cleaner, 22 tops inlet, the output that links together of first cleaner 21 and second cleaner, 22 outlet at bottoms; Described refrigeration system comprises condensing surface 23, refrigerator 24.Gas by purification system is come in is exported behind condensing surface 23 condensation liquefactions, and refrigerator 24 provides refrigeration for condensing surface 23.Described distillation system comprises rectifying tower 25; Described product systems comprise liquid product storage tank 26 and the solid, dry ice maker 27 that is connected.
The mode of connection of first devulcanizer 14 and second devulcanizer 15 is that SP is connected in the desulphurization system of the present invention, and first devulcanizer 14 is connected with second devulcanizer 15 inlet, export and be connected, and outlet and enter the mouth between also link together.
Dry ice machine of the present invention (27) is through the ingress of pipe connection to compressor (12).
First cleaner of the present invention (21) is that carbon steel adds stainless steel lining with second cleaner (22) material.
Equipment entrance of the present invention all is equipped with valve with outlet.
Claims (6)
1. a dioxide gas is caught and refining plant, is made up of gas blower (1), compressor (12), enrichment system, desulphurization system, de-hydrocarbon system, purification system, refrigeration system, distillation system and product systems; The front end that it is characterized in that described enrichment system connects gas blower (1); The enrichment system rear end connects desulphurization system; The desulphurization system rear end connects de-hydrocarbon system, the de-hydrocarbon system rear end connects purification system, purification system rear end connection refrigeration system, refrigeration system rear end connection distillation system, and the distillation system rear end connects product systems; Described enrichment system comprises water wash column (2), tank (3), water pump (4), lean pump (5), rich solution pump (6), absorption tower (7), separator (8), regenerator column (9), skimmer (10), thermal source (11); The unstripped gas of being sent here by gas blower (1) gets into water wash column (2); Be provided with tank (3) below the water wash column (2); Tank (3) connects water pump (4), and water pump (4) is sent the water of tank (3) lining into water wash column (2), and the outlet of water wash column (2) upper end is connected to the bottom of absorption tower (7); The outlet of upper end, absorption tower (7) is connected to separator (8); The outlet of separator (8) is connected to the top of absorption tower (7), and the outlet at bottom of absorption tower (7) is connected to the top of regenerator column (9) through rich solution pump (6), and regenerator column (9) top exit is connected to skimmer (10); The outlet at bottom of skimmer (10) be connected with regenerator column (9) outlet at bottom and through lean pump (5) be connected to top, absorption tower (7) after the outlet at bottom of separator (8) is connected, the top exit of skimmer (10) is connected to the inlet of compressor (12); Thermal source (11) is to be regenerator column (9) heating; Described desulphurization system comprises first water trap (13), first devulcanizer (14), second devulcanizer (15); The outlet of compressor (12) is connected to first water trap (13), and first water trap (13) top exit is connected to first devulcanizer (14) and second devulcanizer (15) inlet, and first devulcanizer (14) and second devulcanizer (15) export the output that links together; Described de-hydrocarbon system comprises interchanger (16), well heater (17), takes off hydrocarbon device (18); The gas of being come in by desulphurization system gets into the top of interchanger (16); The bottom of interchanger (16) is connected to the bottom of well heater (17); The top outlet of well heater (17) is connected to takes off hydrocarbon device (18) top inlet; Take off hydrocarbon device (18) outlet at bottom and be connected to interchanger (16) upper entrance, the output of interchanger (16) lower part outlet; Described purification system comprises water cooler (19), second water trap (20), first cleaner (21), second cleaner (22); The gas of being come in by de-hydrocarbon system gets into second water trap (20) behind water cooler (19); Second water trap (20) top exit is connected to first cleaner (21) and second cleaner (22) top inlet, the output that links together of first cleaner (21) and second cleaner (22) outlet at bottom; Described refrigeration system comprises condensing surface (23), refrigerator (24); Gas by purification system is come in is exported behind condensing surface (23) condensation liquefaction, and refrigerator (24) provides refrigeration for condensing surface (23); Described distillation system comprises rectifying tower (25); Described product systems comprise liquid product storage tank (26) and the solid, dry ice maker (27) that is connected.
2. dioxide gas according to claim 1 is caught and refining plant, it is characterized in that the used absorption liquid in described absorption tower (7) and regenerator column (9) lining is for showing the absorption agent of alkalescence, like salt of wormwood or varies.
3. dioxide gas according to claim 1 is caught and refining plant; It is characterized in that the mode of connection of first devulcanizer (14) and second devulcanizer (15) is that SP is connected in the described desulphurization system; First devulcanizer (14) and second devulcanizer (15) inlet is connected, export and be connected, and outlet and enter the mouth between also link together.
4. dioxide gas according to claim 1 is caught and refining plant, it is characterized in that described dry ice machine (27) is through the ingress of pipe connection to compressor (12).
5. dioxide gas according to claim 1 is caught and refining plant, it is characterized in that described first cleaner (21) and second cleaner (22) material are that carbon steel adds stainless steel lining.
6. dioxide gas according to claim 1 is caught and refining plant, it is characterized in that described equipment entrance all is equipped with valve with exporting.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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Cited By (10)
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| CN105712348A (en) * | 2016-01-19 | 2016-06-29 | 辽宁石油化工大学 | Carbon dioxide recovery method and carbon dioxide recovery device for achieving zero emission of liquified natural gas |
| CN106281524A (en) * | 2016-08-31 | 2017-01-04 | 胜利油田孚瑞特石油装备有限责任公司 | A kind of recoverying and utilizing method of non-combustible oil field gas |
| CN106587061A (en) * | 2017-01-10 | 2017-04-26 | 宁夏坤辉气化有限公司 | System for purifying carbon dioxide by utilizing air discharged in decarbonization |
| CN107399718A (en) * | 2017-07-25 | 2017-11-28 | 大连中鼎化学有限公司 | A kind of ultra-pure oxygen, nitrogen purification method |
| CN108423681A (en) * | 2018-02-05 | 2018-08-21 | 杭州快凯高效节能新技术有限公司 | It is a kind of to absorb the carbon trapping qi exhaustion nitre purification technique combined with rectifying |
| CN108939750A (en) * | 2018-06-25 | 2018-12-07 | 珠海恒基达鑫国际化工仓储股份有限公司 | A kind of condensate Deodor technique |
| CN111151117A (en) * | 2019-04-07 | 2020-05-15 | 魏善兆 | Process for producing and sealing carbon dioxide |
| CN114984704A (en) * | 2022-06-30 | 2022-09-02 | 重庆瑞信气体有限公司 | Method for recovering carbon dioxide from tail gas of closed lime kiln |
| CN116099333A (en) * | 2023-04-13 | 2023-05-12 | 清华四川能源互联网研究院 | Produced gas chemical method carbon capture system |
| CN119353875A (en) * | 2024-12-25 | 2025-01-24 | 上海联风气体有限公司 | Carbon dioxide refining equipment |
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| CN105712348A (en) * | 2016-01-19 | 2016-06-29 | 辽宁石油化工大学 | Carbon dioxide recovery method and carbon dioxide recovery device for achieving zero emission of liquified natural gas |
| CN106281524A (en) * | 2016-08-31 | 2017-01-04 | 胜利油田孚瑞特石油装备有限责任公司 | A kind of recoverying and utilizing method of non-combustible oil field gas |
| CN106587061A (en) * | 2017-01-10 | 2017-04-26 | 宁夏坤辉气化有限公司 | System for purifying carbon dioxide by utilizing air discharged in decarbonization |
| CN107399718A (en) * | 2017-07-25 | 2017-11-28 | 大连中鼎化学有限公司 | A kind of ultra-pure oxygen, nitrogen purification method |
| CN108423681A (en) * | 2018-02-05 | 2018-08-21 | 杭州快凯高效节能新技术有限公司 | It is a kind of to absorb the carbon trapping qi exhaustion nitre purification technique combined with rectifying |
| CN108423681B (en) * | 2018-02-05 | 2021-05-18 | 杭州快凯高效节能新技术有限公司 | Absorption and rectification combined denitration and purification process for carbon capture gas |
| CN108939750A (en) * | 2018-06-25 | 2018-12-07 | 珠海恒基达鑫国际化工仓储股份有限公司 | A kind of condensate Deodor technique |
| CN111151117A (en) * | 2019-04-07 | 2020-05-15 | 魏善兆 | Process for producing and sealing carbon dioxide |
| CN114984704A (en) * | 2022-06-30 | 2022-09-02 | 重庆瑞信气体有限公司 | Method for recovering carbon dioxide from tail gas of closed lime kiln |
| CN116099333A (en) * | 2023-04-13 | 2023-05-12 | 清华四川能源互联网研究院 | Produced gas chemical method carbon capture system |
| CN119353875A (en) * | 2024-12-25 | 2025-01-24 | 上海联风气体有限公司 | Carbon dioxide refining equipment |
| CN119353875B (en) * | 2024-12-25 | 2025-03-25 | 上海联风气体有限公司 | Carbon dioxide refining equipment |
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