CN201138116Y - System for preparing food-grade carbon-dioxide by using power station smoke gas - Google Patents
System for preparing food-grade carbon-dioxide by using power station smoke gas Download PDFInfo
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- CN201138116Y CN201138116Y CNU2007200885829U CN200720088582U CN201138116Y CN 201138116 Y CN201138116 Y CN 201138116Y CN U2007200885829 U CNU2007200885829 U CN U2007200885829U CN 200720088582 U CN200720088582 U CN 200720088582U CN 201138116 Y CN201138116 Y CN 201138116Y
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 142
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 71
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 70
- 239000007788 liquid Substances 0.000 claims abstract description 52
- 238000010521 absorption reaction Methods 0.000 claims abstract description 30
- 238000009833 condensation Methods 0.000 claims abstract description 7
- 230000005494 condensation Effects 0.000 claims abstract description 7
- 239000003546 flue gas Substances 0.000 claims description 44
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 42
- 239000007789 gas Substances 0.000 claims description 29
- 230000002745 absorbent Effects 0.000 claims description 22
- 239000002250 absorbent Substances 0.000 claims description 22
- 239000007921 spray Substances 0.000 claims description 17
- 230000008676 import Effects 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 238000013459 approach Methods 0.000 claims description 5
- 238000005507 spraying Methods 0.000 claims description 5
- 238000010992 reflux Methods 0.000 claims description 4
- 239000011800 void material Substances 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 16
- 230000008569 process Effects 0.000 abstract description 6
- 239000000779 smoke Substances 0.000 abstract description 5
- 235000013305 food Nutrition 0.000 abstract description 4
- 239000000203 mixture Substances 0.000 abstract description 3
- 238000001816 cooling Methods 0.000 abstract description 2
- 230000001172 regenerating effect Effects 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 46
- 238000012856 packing Methods 0.000 description 8
- 241000196324 Embryophyta Species 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 239000012535 impurity Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 239000011261 inert gas Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- ZZVUWRFHKOJYTH-UHFFFAOYSA-N diphenhydramine Chemical compound C=1C=CC=CC=1C(OCCN(C)C)C1=CC=CC=C1 ZZVUWRFHKOJYTH-UHFFFAOYSA-N 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000000053 physical method Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 1
- 241000282326 Felis catus Species 0.000 description 1
- 241000208125 Nicotiana Species 0.000 description 1
- 235000002637 Nicotiana tabacum Nutrition 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 150000002169 ethanolamines Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000003317 industrial substance Substances 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
- 239000000463 material Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical class OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The utility model discloses a system which uses the smoke of the power plant to prepare the food-level carbon dioxide. The system is mainly composed of a carbon dioxide absorption tower, a stripping tower, a regenerating tower, a cooling tower, a gas-liquid separator, a dryer, a compressor and a condenser, which are connected with pipelines through a pump. The system can completely adapt to the characteristics of the power plant that the flow rate of the smoke at the tail part of the boiler is large, the composition of the smoke is complicate, and the condensation of the carbon dioxide is low, thereby not only effectively improving the removing rate of the carbon dioxide, but also producing the liquid carbon dioxide with high purity; moreover, the process flow procedure is simple, the system structure is simplified, and the investment and operation cost is low.
Description
Technical field
The utility model relates to the technology that the coal-fired power station boiler tail flue gas is fully utilized, and refers to a kind of system that utilizes generating plant flue gas to produce food-grade carbon-dioxide particularly.
Background technology
The atmosphere greenhouse effects are one of human main environmental problems that faced.Carbon dioxide is main greenhouse gases, and thermal power plant is the concentrated emission source of carbon dioxide, and its CO2 emissions account for 30% of carbon dioxide total release that mankind's activity causes.The amount of carbon dioxide that the thermal power plant of a 600MW per hour discharges can reach 500 tons.Therefore, in order to reduce Atmospheric Carbon Dioxide content, primary is to reduce the station boiler tail flue gas to the airborne release carbon dioxide.Say from another point of view, carbon dioxide has purposes widely as a kind of industrial chemicals, can be used for food fresh keeping, expanded pipe tobacco, produce methyl alcohol, urea, degradation plastic etc., and present stage has mostly wasted with the carbon dioxide that the station boiler tail flue gas discharges.
Traditional carbon dioxide improvement or extracting method have multiple, roughly can be divided into physical method and chemical method two big classes.Physical method mainly comprises solvent absorption, adsorption method of separation, film permeation method and low temperature distillation method etc.Chemical method mainly refers to chemical absorption method, its principle is to make carbon dioxide and chemical solvent generation chemical reaction and be absorbed, the chemical solvent that absorbing carbon dioxide reaches balance becomes rich solution, rich solution enters regenerator and heats the gas that splits the carbon dioxide off, and separates the purpose that reclaims carbon dioxide thereby reach.More common chemical solvent is the aqueous solution of ethanolamines, industrial common employing alkanolamine solution removes and reclaims carbon dioxide in absorption tower and regenerator, filling-material structure is adopted on the absorption tower, though this method has effective contact area of bigger alkanolamine solution and carbon dioxide, but the impurity component in the reactant causes the packing layer in the absorption tower to stop up easily, causes the absorption tower can't operate as normal.Simultaneously, because the complex structure of packing layer makes equipment operation and maintenance relatively more difficult.This method only is suitable for the occasion that exhaust gas components is simple, flue gas flow is little, and the processing of station boiler tail flue gas also has very big gap in reality.
The particularity of station boiler tail flue gas is that its carbon dioxide content is on the low side, impurity composition is on the high side and flue gas flow is huge.Various types of after testing station boiler tail flue gas, its CO
2Concentration is about 10～15%, and other component has N
2, O
2, SO
2, H
2S, NO, CO and dust etc.Power plant with a 600MW is an example, the about 2000000Nm of its boiler tail flue gas discharge capacity
3/ h.When adopting above-mentioned alkanolamine solution to remove carbon dioxide in conventional fillers formula absorption tower, can cause the absorption tower bulky, construction, operation and overhaul of the equipments difficulty are difficult to reach and effectively remove carbon dioxide in the flue gas and with the purpose of its recycling.
Summary of the invention
The purpose of this utility model is exactly that a kind of system that utilizes generating plant flue gas to produce food-grade carbon-dioxide will be provided.Adopt this system can adapt to the characteristics that station boiler tail flue gas flow is huge, composition is complicated, gas concentration lwevel is low fully, both can effectively improve the removal efficiency of carbon dioxide in the flue gas, can produce highly purified liquid carbon dioxide again, and its technological process is simple, system architecture simplification, investment and operating cost are cheap.
For achieving the above object, the generating plant flue gas that utilizes that the utility model is designed is produced the system of food-grade carbon-dioxide, comprises the carbon dioxide absorption tower, stripping tower, regenerator, cooler, gas-liquid separator, drier, compressor and the condenser that link to each other by pipeline.Described carbon dioxide absorption tower is packless void tower structure, be disposed with absorbent spray equipment and demister from bottom to top between its underpart gas approach and the top exhanst gas outlet, its bottom alkanolamine solution outlet links to each other with the upper inlet of stripping tower by delivery pump, the lower part outlet of stripping tower links to each other with the upper liquid import of regenerator by the rich solution pump, the lower liquid outlet of regenerator links to each other with the absorbent spray equipment by lean pump, the outlet of the upper gas of regenerator links to each other with the import of gas-liquid separator by cooler, the gas vent of gas-liquid separator successively with drier, compressor, condenser and liquid carbon dioxide accumulator tank polyphone.Thus, in removing flue gas in the carbon dioxide, be that the equipment of one carries out removal of impurities, regeneration, dehydration, drying, compression and condensation etc. to it and handles continuously by combinations thereof, until the liquid carbon dioxide that obtains food-grade.
Further, also be provided with below the absorbent spray equipment and impel the equally distributed porous plate of flue gas, the ratio of the hole area of porous plate and plate area is 30～40%.Simultaneously, 3～5 spraying layers of absorbent spray equipment preferred design.Like this, flue gas upwards by behind the porous plate, evenly is full of whole carbon dioxide absorption tower cavity on the one hand, has effectively eliminated flue gas stream dead angle, helps fully contacting with the alkanolamine solution absorbent; Alkanolamine solution is under the effect of the overlapping injection of a plurality of spraying layers on the other hand, can form to intersect fine and close absorbent droplet, makes carbon dioxide in the flue gas have the contact area of maximum with it, can fully fully chemical reaction take place and is absorbed.
Further, on the transfer pipeline of rich solution pump and lean pump, also be provided with poor rich liquid heat exchanger, the lower part outlet of stripping tower links to each other with the upper liquid import of regenerator by rich solution pump, poor rich liquid heat exchanger, and the lower liquid outlet of regenerator links to each other with the absorbent spray equipment by poor rich liquid heat exchanger, lean pump.Like this, can make full use of from regenerator the waste heat of isolated lean solution, give the rich solution preheating that enters regenerator, with the lean solution cooling, realize the benign cycle of heat exchange simultaneously, save heat resource.
Further, the condensation water of gas-liquid separator outlet links to each other with liquid return hole on the carbon dioxide absorption tower by reflux pump.Like this, the condensation water of separating can be turned back in the carbon dioxide absorption tower again and circulate, reduce the process water amount, reduce production costs.
The utility model compared with prior art has following outstanding effect:
One, adopt the carbon dioxide absorption tower of void tower structure, by the carbon dioxide in the mode smoke treatment of the uninterrupted circulated sprinkling of alkanolamine solution absorbent, can make alkanolamine solution and carbon dioxide in the confined space of no any obstacle, produce strong gas-liquid conversed turbulent flow, can significantly increase the contact area of hydramine droplet and carbon dioxide, can avoid again because of the clogging that packing layer produces is set, thereby can effectively overcome the inherent shortcoming of existing filler absorption pattern, its carbon dioxide eliminating efficient can reach more than 95%, and it is low to be particularly suitable for handling gas concentration lwevel, the coal-fired power station boiler tail flue gas that flue gas flow is big.
They are two years old, by various pumps and pipeline equipment such as carbon dioxide absorption tower, stripping tower, regenerator, gas-liquid separator, cooler, drier, compressor and condenser organically are combined into a complete process system, both simplify technological process and system architecture, significantly reduced investment, the operation and maintenance cost of equipment again.
Its three, utilize the station boiler tail flue gas to turn waste into wealth, when effectively reducing the carbon dioxide greenhouse gas discharging, obtain liquid carbon dioxide, its product purity can reach more than 99.9%, meets the international food grade standard fully.Both helped the comprehensive regulation of air environmental pollution, helped the benign development of recycling economy again, can realize the innoxious and recycling of station boiler tail flue gas, be particularly suitable for the national conditions of China based on coal fired power generation.
Description of drawings
Accompanying drawing is a kind of structural principle schematic diagram that utilizes the system that generating plant flue gas produces food-grade carbon-dioxide.
The specific embodiment
Below at station boiler unit institute discharged flue gas, in conjunction with the accompanying drawings the utility model is described in further detail:
Utilize generating plant flue gas to produce the system of food-grade carbon-dioxide shown in the figure, mainly form by carbon dioxide absorption tower 2, stripping tower 18, regenerator 16, cooler 15, gas-liquid separator 14, drier 13, compressor 12 and the condenser 11 etc. that link to each other by pipeline.Carbon dioxide absorption tower 2 is packless void tower structure, be provided with booster fan 1 before the gas approach of its underpart, be disposed with porous plate 3, absorbent spray equipment 22 and demister 21 between its underpart gas approach and the top exhanst gas outlet from bottom to top, the ratio of the hole area of porous plate 3 and plate area is 30～40%, the dead angle that can remove smoke evenly distributes flue gas in carbon dioxide absorption tower 2.Absorbent spray equipment 22 is provided with 3～5 spraying layers, fully contacts with carbon dioxide in the flue gas to guarantee the alkanolamine solution absorbent.Demister 21 can be selected the combination demister for use, is made of upper and lower layer demist filter screen and the cleaning spraying mechanism 19 between upper and lower layer demist filter screen, to remove the absorbent drop in the flue gas fully.
The alkanolamine solution outlet of carbon dioxide absorption tower 2 bottoms links to each other with the upper inlet of stripping tower 18 by delivery pump 4, the bottom of stripping tower 18 is provided with inert gas conveying device 17, the lower part outlet of stripping tower 18 links to each other with the upper liquid import of regenerator 16 by rich solution pump 6, poor rich liquid heat exchanger 7, the lower liquid outlet of regenerator 16 links to each other with absorbent spray equipment 22 by poor rich liquid heat exchanger 7, lean pump 5, the import department of absorbent spray equipment 22 also is provided with alkanolamine solution device for supplying 20, and the boiling device 8 in the regenerator 16 is arranged on tower bottom.The upper gas outlet of regenerator 16 links to each other with the import of centrifugal gas-liquid separator 14 by cooler 15, the outlet of the condensation water of gas-liquid separator 14 links to each other with liquid return hole on the carbon dioxide absorption tower 2 by reflux pump 9, the gas vent of gas-liquid separator 14 links to each other with the import of drier 13, the outlet of drier 13 links to each other with the import of compressor 12, the outlet of compressor 12 links to each other with the import of condenser 11, and the outlet of condenser 11 links to each other with liquid carbon dioxide accumulator tank 10.Above each several part equipment is the chemical field common equipment, and its concrete structure repeats no more.
It is as follows that the utility model utilizes generating plant flue gas to produce the course of work of system of food-grade carbon-dioxide:
After conventional dedusting of process of station boiler tail flue gas and desulfurization were handled, from the gas approach input tower of carbon dioxide absorption tower 2 bottoms, it was up to pass through porous plate 3 by booster fan 1.Meanwhile, alkanolamine solution ejection downwards from absorbent spray equipment 22.Alkanolamine solution is that 5～10% monoethanolamine, mass percent concentration 20～30% methyl diethanolamines and water are formed by mass percent concentration, the temperature that keeps flue gas in 35～50 ℃ scope, pressure in the scope of 2500～3000Pa, and set spray CO in hydramine and the flue gas
2The mol ratio of gas is 1.1～1.3.CO in the flue gas
2Gas produces reverse the contact with the alkanolamine solution droplet, sufficient chemical reaction takes place and is absorbed by alkanolamine solution.
Removed CO by the alkanolamine solution suction
2Flue gas continue upwards to flow, remove the absorbent droplet through the demister 21 that is arranged in carbon dioxide absorption tower 2 tops after, cleaning flue gases directly enters atmosphere.And absorption CO
2The alkanolamine solution rich solution that reaches balance falls into carbon dioxide absorption tower 2 bottoms, imports from stripping tower 18 upper inlet by delivery pump 4.Stripping tower 18 is a packed tower, is furnished with nozzle and packing layer in the tower, and the alkanolamine solution rich solution is sprayed onto on the packing layer of stripping tower 18.Meanwhile, from the bottom inert gas conveying device 17 of stripping tower 18, introduce inert gas (nitrogen or other similar gas), with the abundant counter current contacting of alkanolamine solution rich solution on the packing layer, to remove the O in the alkanolamine solution rich solution
2, NO
x, impurity such as CO.
Carry O
2, NO
x, impurity such as CO inert gas directly discharge from the cat head of stripping tower 18.And pure alkanolamine solution rich solution sinks to the lower part outlet place of stripping tower 18, is transported in the poor rich liquid heat exchanger 7 CO that removed that is flowed out from the outlet of regenerator 16 lower liquid by rich solution pump 6
2The alkanolamine solution lean solution be heated to 95～100 ℃, send into the tower from the upper liquid import of regenerator 16 again.Regenerator 16 is a packed tower also, is furnished with nozzle and packing layer in the tower, and pure alkanolamine solution rich solution is sprayed onto on the packing layer of regenerator 16, and the steam gas that is risen is carried, and is heated to 100～115 ℃ through boiling device 8 at the bottom of the tower, parses the CO of high concentration
2Gas makes the alkanolamine solution rich solution be reduced into simultaneously and has removed CO
2The alkanolamine solution lean solution.
The alkanolamine solution lean solution is drawn from the outlet of the lower liquid of regenerator 16, after poor rich liquid heat exchanger 7 heat exchange, by lean pump 5 be transported to continue in the absorbent spray equipment 22 recycling.Temperature greatly about about 90 ℃, pressure is about regeneration gas---the high concentration CO of 0.02Mpa
2Gas is flowed out by the upper gas outlet of regenerator 16 in company with a large amount of water vapour, enters in the cooler 15, and after recirculated water heat exchange in the cooler 15, air-flow is cooled to 35～45 ℃, and water vapour is wherein freeze-outed.
The regeneration gas of handling through subcooler 15 is from the import input of gas-liquid separator 14, by centrifugal action with CO
2The lime set of carrying secretly in the gas is separated, and obtains purity and is higher than 99.9% CO
2Gas.Isolated lime set flow out from the outlet of the condensation water of gas-liquid separator 14, send into circulation in the carbon dioxide absorption tower 2 again by reflux pump 9.Isolated high-purity CO
2Gas is then sent into drier 13, and drying is delivered to compressor 12 after handling again, and compressed processing enters condenser 11, is condensed into liquid state, and food prepared therefrom class liquid CO 2 finished product is sent in the liquid carbon dioxide accumulator tank 10 and preserved.
Claims (5)
1, a kind of system that utilizes generating plant flue gas to produce food-grade carbon-dioxide, comprise the carbon dioxide absorption tower (2) that links to each other by pipeline, stripping tower (18), regenerator (16), cooler (15), gas-liquid separator (14), drier (13), compressor (12) and condenser (11), it is characterized in that: described carbon dioxide absorption tower (2) is packless void tower structure, be disposed with absorbent spray equipment (22) and demister (21) between its underpart gas approach and the top exhanst gas outlet from bottom to top, its bottom alkanolamine solution outlet links to each other with the upper inlet of stripping tower (18) by delivery pump (4), the lower part outlet of stripping tower (18) links to each other with the upper liquid import of regenerator (16) by rich solution pump (6), the lower liquid outlet of regenerator (16) links to each other with absorbent spray equipment (22) by lean pump (5), the outlet of the upper gas of regenerator (16) links to each other with the import of gas-liquid separator (14) by cooler (15), the gas vent of gas-liquid separator (14) successively with drier (13), compressor (12), condenser (11) and liquid carbon dioxide accumulator tank (10) polyphone.
2, the system that utilizes generating plant flue gas to produce food-grade carbon-dioxide according to claim 1, it is characterized in that: the below of said absorbent spray equipment (22) is provided with impels the equally distributed porous plate of flue gas (3), and the hole area of porous plate (3) and the ratio of plate area are 30～40%.
3, the system that utilizes generating plant flue gas to produce food-grade carbon-dioxide according to claim 1 and 2 is characterized in that: said absorbent spray equipment (22) is provided with 3～5 spraying layers.
4, the system that utilizes generating plant flue gas to produce food-grade carbon-dioxide according to claim 1 and 2, it is characterized in that: the lower part outlet of said stripping tower (18) links to each other with the upper liquid import of regenerator (16) by rich solution pump (6), poor rich liquid heat exchanger (7), and the lower liquid outlet of said regenerator (16) links to each other with absorbent spray equipment (22) by poor rich liquid heat exchanger (7), lean pump (5).
5, the system that utilizes generating plant flue gas to produce food-grade carbon-dioxide according to claim 1 and 2 is characterized in that: the outlet of the condensation water of said gas-liquid separator (14) links to each other with liquid return hole on the carbon dioxide absorption tower (2) by reflux pump (9).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007200885829U CN201138116Y (en) | 2007-11-29 | 2007-11-29 | System for preparing food-grade carbon-dioxide by using power station smoke gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007200885829U CN201138116Y (en) | 2007-11-29 | 2007-11-29 | System for preparing food-grade carbon-dioxide by using power station smoke gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201138116Y true CN201138116Y (en) | 2008-10-22 |
Family
ID=40038803
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2007200885829U Expired - Lifetime CN201138116Y (en) | 2007-11-29 | 2007-11-29 | System for preparing food-grade carbon-dioxide by using power station smoke gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201138116Y (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101177267B (en) * | 2007-10-31 | 2010-10-13 | 武汉凯迪电力环保有限公司 | Method for preparing food-grade carbon-dioxide by using power station smoke gas and system thereof |
| CN102210247A (en) * | 2011-04-02 | 2011-10-12 | 武汉凯迪控股投资有限公司 | Method and equipment for providing heat and carbon dioxide for vegetables and/or algae by using flue gas of power plant |
| CN103277979A (en) * | 2013-06-08 | 2013-09-04 | 中煤科工集团重庆研究院 | Deacidifying device in low-concentration oxygen-bearing coal bed gas copious cooling rectification treatment process |
| CN104043332A (en) * | 2014-07-07 | 2014-09-17 | 银川天佳能源科技股份有限公司 | Multi-tower series-connected circulating amine solution regenerating device |
| CN104226083A (en) * | 2013-06-07 | 2014-12-24 | 合肥思力事达机电科技有限公司 | Flue gas recovered food grade carbon dioxide recycling system |
| CN105402991A (en) * | 2015-12-28 | 2016-03-16 | 苟仲武 | Method and device for condensing and recovering chemical components of exhaust gas and generating electricity by using afterheat |
-
2007
- 2007-11-29 CN CNU2007200885829U patent/CN201138116Y/en not_active Expired - Lifetime
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101177267B (en) * | 2007-10-31 | 2010-10-13 | 武汉凯迪电力环保有限公司 | Method for preparing food-grade carbon-dioxide by using power station smoke gas and system thereof |
| CN102210247A (en) * | 2011-04-02 | 2011-10-12 | 武汉凯迪控股投资有限公司 | Method and equipment for providing heat and carbon dioxide for vegetables and/or algae by using flue gas of power plant |
| WO2012136124A1 (en) * | 2011-04-02 | 2012-10-11 | 阳光凯迪新能源集团有限公司 | Method and device for providing heat and carbon dioxide to vegetables and/or algae using power station flue gas |
| CN102210247B (en) * | 2011-04-02 | 2012-10-31 | 武汉凯迪控股投资有限公司 | Method and device for providing heat and carbon dioxide to vegetables and/or algae using power plant flue gas |
| CN104226083A (en) * | 2013-06-07 | 2014-12-24 | 合肥思力事达机电科技有限公司 | Flue gas recovered food grade carbon dioxide recycling system |
| CN103277979A (en) * | 2013-06-08 | 2013-09-04 | 中煤科工集团重庆研究院 | Deacidifying device in low-concentration oxygen-bearing coal bed gas copious cooling rectification treatment process |
| CN103277979B (en) * | 2013-06-08 | 2015-06-17 | 中煤科工集团重庆研究院有限公司 | Deacidification device in cryogenic rectification treatment process of low-concentration oxygen-containing coal bed gas |
| CN104043332A (en) * | 2014-07-07 | 2014-09-17 | 银川天佳能源科技股份有限公司 | Multi-tower series-connected circulating amine solution regenerating device |
| CN105402991A (en) * | 2015-12-28 | 2016-03-16 | 苟仲武 | Method and device for condensing and recovering chemical components of exhaust gas and generating electricity by using afterheat |
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Granted publication date: 20081022 Effective date of abandoning: 20071129 |