CN202902749U - Carbon dioxide in flue gas purification system - Google Patents
Carbon dioxide in flue gas purification system Download PDFInfo
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- CN202902749U CN202902749U CN 201220206246 CN201220206246U CN202902749U CN 202902749 U CN202902749 U CN 202902749U CN 201220206246 CN201220206246 CN 201220206246 CN 201220206246 U CN201220206246 U CN 201220206246U CN 202902749 U CN202902749 U CN 202902749U
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Abstract
A carbon dioxide in flue gas purification system is used for separating and purifying carbon dioxide from flue gas with the carbon dioxide. The carbon dioxide in flue gas purification system comprises a flue gas compression device, an air cooling device, a heat-exchanging device and a gas-liquid separation device. The flue gas compression device is used for compressing the flue gas into high-pressure flue gas. The air cooling device is used for cooling the air into lower-temperature air. The heat-exchanging device is communicated with the flue gas compression device and the air cooling device. The heat-exchanging device is used for heat exchanging between the high-pressure flue gas and the low-temperature air to form high-pressure low-temperature flue gas, so that partial carbon dioxide in the high-pressure low-temperature flue gas is liquefied. The gas-liquid separation device is used for separating the liquefied carbon dioxide from the high-pressure low-temperature flue gas. The carbon dioxide in flue gas purification system is simple.
Description
Technical field
The utility model relates to a kind of carbon dioxide in flue gas purification system.
Background technology
Coal also has irreplaceable status as the basic energy resource of China within the quite a long time.Containing a large amount of carbon dioxide in the coal steam-electric plant smoke that utilizes coal to generate electricity pollutes the environment.
When existing carbon dioxide in flue gas is purified, usually flue gas is at first carried out the solution adsorption and enrichment after, solution is carried out the heating evaporation carbon dioxide, and the carbon dioxide of collecting liquefaction reuses.Yet, need to carry out preliminary treatment preventing other dusts and contaminating impurity solution in the flue gas to flue gas when flue gas is carried out the solution adsorption and enrichment, thereby so that CO 2 purification system is comparatively complicated, be unfavorable for the popularization of carbon trapping technique.
The utility model content
Based on this, be necessary to provide a kind of carbon dioxide in flue gas purification system of comparatively simple liquid carbon dioxide.
A kind of carbon dioxide in flue gas purification system is for separating of the carbon dioxide in, the flue gas contain carbon dioxide of purifying, and described carbon dioxide in flue gas purification system comprises:
The flue gas compression set is used for the flue gas pressurization is formed the high pressure flue gas;
Air refrigerating devie is used for the air cooling is formed Cryogenic air;
Heat-exchange device, be communicated with described flue gas compression set and described air refrigerating devie, described heat-exchange device is used for described high pressure flue gas and described Cryogenic air are carried out heat exchange formation high pressure low temperature flue gas, so that part co 2 liquefaction in the described high pressure low temperature flue gas;
Gas-liquid separation device is for separating of the carbon dioxide that liquefies in the described high pressure low temperature flue gas.
Therein among embodiment, described carbon dioxide in flue gas purification system also comprises the flue gas desulfur device that is communicated with described flue gas compression set, and described flue gas desulfur device is used for removing the sulfur dioxide of described flue gas before described flue gas pressurization forms the high pressure flue gas.
Among embodiment, described flue gas desulphurization system comprises therein:
The low temperature plasma device, the oxidizing sulfur dioxide that is used for flue gas is sulfur trioxide, described low temperature plasma device;
The alkali lye contact chamber is communicated with described low temperature plasma device, and described alkali lye contact chamber is used for the sulfur trioxide of described flue gas and alkaline reaction generation are contained SO
4 2-Solution;
Wherein, the alkali lye contact chamber is communicated with the flue gas compression set, makes the flue gas of removing sulfur trioxide through described alkali lye contact chamber be delivered to described flue gas compression set compression and forms the high pressure flue gas.
Among embodiment, described flue gas desulphurization system comprises calcium source contact chamber therein, and described calcium source contact chamber is communicated with described alkali lye contact chamber by pipeline, and described calcium source contact chamber is used for the described SO that contains
4 2-Solution and calcium source reaction generate calcium sulfate and reclaim alkali lye, the calcium source of accommodating in the contact chamber of described calcium source is calcium oxide, calcium hydroxide or aqua calcis.
Among embodiment, described carbon dioxide in flue gas purification system also comprises the molecular sieve that is communicated with described flue gas compression set therein, and described molecular sieve is used for improving the concentration of described carbon dioxide in flue gas.
Therein among embodiment, described flue gas compression set comprises compressor, cooler, oil water separator, drier and the accurate filter that is communicated with successively, described compressor is used for the compression flue gas, described cooler is for reducing the temperature of the flue gas of described compressor output, described oil water separator is used for removing the profit through the flue gas of described cooler cooling, described drier is used for the flue gas that purifies through described oil water separator is dehydrated, and described accurate filter is used for removing the dust of the flue gas after dehydrating through described drier.
Among embodiment, described carbon dioxide in flue gas purification system also comprises the flue gas pre-cooler that is communicated with described flue gas compression set therein, and described flue gas is met device for cooling and comprised air-introduced machine and the cooler that is communicated with air-introduced machine.
Therein among embodiment, described carbon dioxide in flue gas purification system also comprises the air cleaning unit that is communicated with described air refrigerating devie, described air cleaning unit comprises air compressor, oil water separator, drier and the accurate filter that is communicated with successively, described oil water separator is used for removing the airborne profit through described air compressor compression, described drier is used for the air that purifies through described oil water separator is dehydrated, and described accurate filter is used for removing the airborne dust after dehydrating through described drier.
Therein among embodiment, described carbon dioxide in flue gas purification system also comprises the air precooler that is communicated with described air refrigerating devie, described air precooler comprises cooler and the heat exchanger that is communicated with described cooler, described cooler is used for carrying out pre-cooled to air, described heat exchanger is communicated with described gas-liquid separation device, and described heat exchanger is used for separating the tail gas of removing carbon dioxide with the described gas-liquid separation device of described process through the air of described cooler cooling and carries out heat exchange.
Among embodiment, it is 1.5MPa ~ 2.5MPa that described heat-exchange device is used for described high pressure flue gas and described Cryogenic air are carried out heat exchange formation air pressure therein, and temperature is-25 ℃～-35 ℃ high pressure low temperature flue gas.。
Above-mentioned carbon dioxide in flue gas purification system, the flue gas compression set pressurizes to flue gas and forms the high pressure flue gas, air refrigerating devie forms Cryogenic air with the air cooling, high pressure flue gas and Cryogenic air are carried out heat exchange by heat-exchange device, make the high pressure flue gas become the high pressure low temperature flue gas, under the condition of high pressure low temperature, partial CO 2 liquefaction in the flue gas generates liquid carbon dioxide, co 2 liquefaction in the flue gas is separated with other gases and impurity in the flue gas, gas-liquid separation device is with the carbon dioxide separation of liquefaction, thereby this carbon dioxide in flue gas purification system is comparatively simple.
Description of drawings
Fig. 1 is the structural representation of the carbon dioxide in flue gas purification system of an embodiment;
Fig. 2 is the structural representation of flue gas desulfur device among Fig. 1.
The specific embodiment
For the ease of understanding the utility model, the below is described more fully the utility model with reference to relevant drawings.Provided first-selected embodiment of the present utility model in the accompanying drawing.But the utility model can be realized with many different forms, be not limited to embodiment described herein.On the contrary, providing the purpose of these embodiment is to make to disclosure of the present utility model more thoroughly comprehensively.
Need to prove that when element is called as " being fixedly arranged on " another element, can directly can there be element placed in the middle in it on another element or also.When an element is considered to " connection " another element, it can be to be directly connected to another element or may to have simultaneously centering elements.Term as used herein " vertical ", " level ", " left side ", " right side " and similar statement are just for illustrative purposes.
Unless otherwise defined, the employed all technology of this paper are identical with the implication that belongs to the common understanding of those skilled in the art of the present utility model with scientific terminology.Employed term is not intended to be restriction the utility model just in order to describe the purpose of specific embodiment in specification of the present utility model herein.Term as used herein " and/or " comprise one or more relevant Listed Items arbitrarily with all combinations.
See also Fig. 1, the carbon dioxide in flue gas purification system 100 of one embodiment is for separating of the carbon dioxide in, the flue gas contain carbon dioxide of purifying, and carbon dioxide in flue gas purification system 100 comprises flue gas pre-cooler 10, flue gas desulfur device 20, molecular sieve 30, flow controller 35, flue gas compression set 40, air cleaning unit 50, air precooler 60, air refrigerating devie 70, heat-exchange device 80, air emptier 85, gas-liquid separation device 90 and carbon dioxide collecting device 95.
Flue gas pre-cooler 10 comprises air-introduced machine 12 and the cooler 14 that is communicated with air-introduced machine 12.The temperature of the flue gas of power plant emission is generally and is higher than normal temperature, is approximately 130 ℃, and flue gas is delivered to air-introduced machine 12, carries out elementary cooling through being delivered to 14 pairs of flue gases of cooler after air-introduced machine 12 pressurizations, and the temperature of flue gas is reduced near normal temperature.
See also Fig. 2, flue gas desulfur device 20 comprises low temperature plasma device 22, alkali lye contact chamber 24, calcium source contact chamber 25, retracting device 26 and calcium sulfate gathering-device 27.
The oxidizing sulfur dioxide that low temperature plasma device 22 is used for flue gas is sulfur trioxide.Low temperature plasma device 22 is communicated with cooler 14, enters low temperature plasma device 22 through cooler 14 elementary cooled flue gases.
Contain a large amount of high energy electrons, ion, excited state ion in the plasma of low temperature plasma device 22 by Pulsed Discharge and have the very free radical of strong oxidizing property, wherein the average energy of active ion is higher than the bond energy of gas molecule.Active ion and sulfur dioxide bump, and opening the gas molecule key generates some nitrogen-atoms molecule and solia particles on the one hand, excites on the other hand airborne oxygen, water vapour, form ozone, O
-With hydroxyl free from the base etc. extremely strong oxidant.Sulfur dioxide in these oxidants and the flue gas occurs a series of take active ion or free radical as the electrochemical reaction of the complexity of collective, finally makes Sulphur Dioxide become sulfur trioxide.
Alkali lye contact chamber 24 is used for and will contains SO through the sulfur trioxide of low-temperature plasma device oxidation generation and the alkaline reaction generation of alkali lye contact chamber interior 120
4 2-Solution.
Alkali lye is NaOH (NaOH) solution or potassium hydroxide (KOH) solution.Preferably, the mass concentration of alkali lye is 7% ~ 15%.
Sulfur trioxide and alkaline reaction generate contains SO
4 2-Solution be sodium sulphate (Na
2SO
4) solution or potassium sulfate (K
2SO
4) solution.Concrete reaction equation is as follows:
2ROH+SO
3→R
2SO
4+H
2O
Wherein, R is K or Na.
In the present embodiment, alkali lye contact chamber 24 is communicated with low temperature plasma device 22 by pipeline.Contain in the alkali lye contact chamber 24 for the alkali lye of sulfur trioxide reaction.Specifically in the present embodiment, be provided with micro-spray device in the alkali lye contact chamber 24, micro-spray device is atomized into small drop with alkali lye, and to the flue gas spray alkali lye that passes in the alkali lye contact chamber 24, contains SO so that the abundant haptoreaction of the alkali lye of flue gas and atomizing generates
4 2-Solution.It is pointed out that micro-spray device can omit, also can directly pass into flue gas in the alkali lye this moment, and sulfur trioxide and alkali lye in the flue gas are reacted.
Calcium source contact chamber 25 is used for the SO that contains with 24 generations of alkali lye contact chamber
4 2-Solution and calcium source reaction be converted into calcium sulfate and reclaim alkali lye.
The calcium source is calcium oxide, calcium hydroxide or aqua calcis.Preferably, the mass concentration of aqua calcis is 5% ~ 13%.
Concrete, calcium oxide with contain SO
4 2-Solution in steeping in water for reconstitution give birth to reaction, generate calcium hydroxide (Ca (OH)
2).Therefore the calcium source with contain SO
4 2-The recovery alkali lye that generates of solution reaction be sodium hydroxide solution or potassium hydroxide solution.Concrete reaction equation is as follows:
R
2SO
4+Ca(OH)
2→Ca
2SO
4+2ROH
Wherein, R is K or Na, calcium sulfate (Ca
2SO
4) being slightly soluble in water, multiple reversal afterwards calcium sulfate exists with precipitation form.
In the present embodiment, calcium source contact chamber 25 is communicated with alkali lye contact chamber 24 by pipeline.
Specifically in the present embodiment, be provided with reaction tank in the calcium source contact chamber 25, the calcium source is contained in the reaction tank, can be with the SO that contains of alkali lye contact chamber 24 interior generations during use
4 2-Solution pass in the reaction tank by pipeline, reacting with calcium source in the reaction tank generates calcium sulfate precipitation and reclaims alkali lye.In other embodiments, the adding of the calcium source in the contact chamber of calcium source can be contained SO
4 2-Solution in react.
Calcium sulfate gathering-device 27 is used for collecting the calcium sulfate of calcium source contact chamber 25 interior generations.The calcium sulfate that calcium sulfate gathering-device 27 is collected can be used for the production of industrial gypsum.
Flue gas compression set 40 comprises compressor 41, cooler 42, oil water separator 43, drier 44, accurate filter 45.
Cooler 42 is communicated with compressor 41.Cooler 42 is for reducing the temperature of the flue gas of compressor 41 outputs.
Drier 44 is communicated with oil water separator 43.Drier 44 is used for the flue gas that purifies through oil water separator 43 is dehydrated.
Drier 53 is communicated with oil water separator 52.Drier 53 is used for the air that purifies through oil water separator 52 is dehydrated.
Heat-exchange device 80 is communicated with the accurate filter 45 of air refrigerating devie 70 and flue gas compression set 40 simultaneously.Cryogenic air through air refrigerating devie 70 preparations is carried out heat exchange with the high pressure flue gas for preparing through compression set 40 at heat-exchange device 80, and making the high pressure flue gas become air pressure is 1.5MPa ~ 2.5MPa, and temperature is-25 ℃ ~-35 ℃ high pressure low temperature flue gas.Under the condition of high pressure low temperature, the partial CO 2 liquefaction in the flue gas generates liquid carbon dioxide.
Air emptier 85 is communicated with heat-exchange device 80.Carry out in heat-exchange device 80 that air after the heat exchange enters in the air emptier 85 and emptying through air venting device 85.
Gas-liquid separation device 90 is communicated with heat-exchange device 80 simultaneously and the heat exchanger 62 of air precooler 60 is communicated with.The flue gas that contains liquid carbon dioxide that carries out in heat-exchange device 80 after the heat exchange enters gas-liquid separation device 90, to isolate liquid carbon dioxide and to remove the tail gas of the carbon dioxide of liquefaction.Tail gas is delivered to the heat exchanger 62 of air precooler 60 as low-temperature receiver owing to temperature is lower, and carry out heat exchange through the pre-cooled air of subcooler 61.Because the carbon dioxide in the flue gas can not liquefy fully, so still contains the carbon dioxide of higher concentration in the tail gas.The compressor 41 that again enters flue gas compression set 40 through the tail gas after heat exchanger 62 heat exchange re-starts the separation of carbon dioxide.
Carbon dioxide collecting device 95 is used for collecting the liquid carbon dioxide that separates through gas-liquid separation device 90.Carbon dioxide collecting device 95 liquid towards carbon dioxide carry out canned.
In the above-mentioned carbon dioxide in flue gas purification system 100,40 pairs of flue gases of flue gas compression set pressurize and form the high pressure flue gas, air refrigerating devie 70 forms Cryogenic air with the air cooling, high pressure flue gas and Cryogenic air are carried out heat exchange by heat-exchange device 80, make the high pressure flue gas become the high pressure low temperature flue gas, adopt high pressure, the low temperature mode makes the partial CO 2 liquefaction in the flue gas generate liquid carbon dioxide, be 1.5MPa ~ 2.5MPa at air pressure, temperature is under-25 ℃～-35 ℃ the condition, other gases can not liquefy in the flue gas, thereby the co 2 liquefaction in the flue gas separates with other gases and impurity in the flue gas, and is comparatively simple; And the cryogenic gas that other do not liquefy can be used for cold recovery the precooling of the air of air refrigerating devie 70 in heat exchanger 67, thereby realizes the comprehensive utilization of energy.
Be appreciated that, when the temperature of carrying out the flue gas that carbon dioxide purifies during near normal temperature, flue gas pre-cooler 10 can omit, when sulfur dioxide in flue gas content is low, flue gas desulfur device 20 can omit, molecular sieve 30 can omit, and directly be delivered to flue gas flue gas compression set 40 and be collapsed into the high pressure flue gas and get final product this moment; When oil gas, steam and dust were less in the flue gas, cooler 42, oil water separator 43, drier 44 and accurate filter 45 can omit, and directly the flue gas that compresses were delivered to heat-exchange device 80 and got final product; Same, when oil gas, steam and dust were less in the air, air cleaning unit 50 can omit, and directly be delivered to air air precooler 60 and get final product this moment; Air precooler 60 can omit, and directly be delivered to air air refrigerating devie 70 and get final product this moment.
Please consult simultaneously Fig. 1 to Fig. 2, the carbon dioxide in flue gas method of purification of an embodiment may further comprise the steps for separating of the carbon dioxide in, the flue gas contain carbon dioxide of purifying:
Step S101, flue gas is carried out pre-cooled processing.
The temperature of fume emission out the time probably is 130 ℃.Flue gas is carried out pre-cooled processing to be comprised flue gas is carried out precharge and to carrying out pre-cooled through the flue gas of precharge.
Air pressure with flue gas when flue gas is carried out precharge increases to 0.15MPa ~ 0.5MPa.In the present embodiment, use air-introduced machine 12 to carry out precharge.
Flue gas is carried out flue gas being precooled to normal temperature when pre-cooled.In the present embodiment, use 14 pairs of flue gases of cooler to carry out pre-cooled.
Step S102, flue gas is carried out desulfurization process.
Flue gas is carried out the desulfurization processing be may further comprise the steps:
Flue gas is carried out low temperature plasma excite oxidation, making the oxidizing sulfur dioxide in the flue gas is sulfur trioxide;
To excite through low temperature plasma flue gas and the alkaline reaction of oxidation, and make sulfur trioxide and the generation of alkaline reaction solution reaction in the described flue gas contain SO
4 2-Solution.
Alkali lye is NaOH (NaOH) solution or potassium hydroxide (KOH) solution.Preferably, the mass concentration of alkali lye is 7% ~ 15%.
Further, can SO will be contained
4 2-Solution and calcium source reaction, regather and contain SO
4 2-Solution and the calcium sulfate that generates of calcium source reaction and reclaim alkali lye, and the recovery alkali lye that will collect is used for and the process low temperature plasma excites the smoke reaction of oxidation.
In the present embodiment, use 20 pairs of flue gases of flue gas desulfur device to carry out desulfurization and process.
Step S103, use molecular sieve improve the concentration of the carbon dioxide in the flue gas.
Enter molecular sieve 30 through the flue gas after the desulfurization processing, the volumn concentration of carbon dioxide in flue gas is increased to more than 50%.
Step S104, compression flue gas form the high pressure flue gas.
Preferably, the air pressure of high pressure flue gas is 1.5MPa ~ 2.5MPa.
In the present embodiment, use 41 pairs of flue gases of processing through molecular sieve of compressor to compress, make the air pressure of flue gas increase to 1.5MPa ~ 2.5MPa.
Further, 35 controls of use traffic controller are delivered to the flow of the flue gas of compressor 41.
Step S105, to flue gas cool off successively, water-oil separating and dehydrate processing.
Flue gas cools off rear temperature and is reduced to 35 ℃ ~ 55 ℃.In the present embodiment, the high pressure flue gas that compression forms through compressor 41 at first enters the temperature that cooler 42 cools off to reduce the flue gas of compressor 41 outputs.
Use oil water separator 43 to remove profit in the flue gas, purifying smoke through the flue gas of subcooler 42 cooling.In the present embodiment, oil water separator 43 is cyclone separator.
The flue gas of removing profit through water-oil separating uses drier 44 to dehydrate to remove steam in the flue gas.
Step S106, flue gas is carried out secondary filter remove impurity in the flue gas
In the present embodiment, use 45 pairs of flue gases of accurate filter to filter.
Step S107, air is compressed successively, water-oil separating, dehydrates and secondary filter is processed to form and purified air.
In the present embodiment, use air cleaning unit 50 to purify air, be specially, use air compressor 51 compressed air, making the air pressure of the air after the compression is 0.6MPa ~ 1.2MPa; 51 compression rear section impurity liquefaction are profit to air through air compressor, use the airborne profit that separates through after air compressor 51 compressions; Use drier 53 further to remove airborne steam; Use accurate filter 54 is removed airborne dust and the particle through drying and dehydrating.
Preferably, oil water separator 52 is cyclone separator.
Step S108, carry out purifying air pre-cooled.
In the present embodiment, use cooler 61 will be precooled to through purifying air normal temperature.
Step S109, cool off to form Cryogenic air to purifying air.
The temperature of Cryogenic air is-40 ℃～-60 ℃.
In the present embodiment, use air refrigerating devie 70 air to be cooled to-40 ℃～-60 ℃.Preferably, air refrigerating devie 70 is air wave refrigerating device.
The air pressure of Cryogenic air is 0.6MPa ~ 1.2MPa, is preferably 0.8MPa.
Step S110, will carry out heat exchange through the flue gas of secondary filter and Cryogenic air and form the high pressure low temperature flue gas, so that part co 2 liquefaction in the high pressure low temperature flue gas, the air pressure of high pressure low temperature flue gas is 1.5MPa ~ 2.5MPa, and temperature is-25 ℃～-35 ℃.
In the present embodiment, carry out heat exchange through flue gas and the Cryogenic air of secondary filter by heat-exchange device 80, make the high pressure flue gas become the high pressure low temperature flue gas.Be 1.5MPa ~ 2.5MPa at air pressure, temperature is that the partial CO 2 liquefaction in the flue gas generates liquid carbon dioxide under-25 ℃～-35 ℃ the condition.
Cryogenic air becomes normal temperature air through after the heat exchange, can discharge, and in the present embodiment, normal temperature air is emptying by air emptier 85.
Step S110, separate the carbon dioxide of the liquefaction in the described high pressure low temperature flue gas and remove the tail gas of the carbon dioxide of liquefaction.
The flue gas that contains liquid carbon dioxide that carries out forming after the heat exchange in heat-exchange device 80 enters gas-liquid separation device 90, to isolate liquid carbon dioxide and to remove the tail gas of the carbon dioxide of liquefaction.
The carbon dioxide of step S111, collection liquefaction.
In the present embodiment, use carbon dioxide collecting device 95 collection liquid carbon dioxides and liquid towards carbon dioxide to carry out can.
Step S112, the air that tail gas and process is pre-cooled carry out heat exchange.
Temperature through the tail gas after separating is lower, can be used as low-temperature receiver to again carrying out pre-cooled through pre-cooled air.In the present embodiment, the air pre-cooled through the tail gas after separating and process passes through heat exchanger 62 heat exchange.
Step S113, will re-start separating-purifying through the tail gas of heat exchange.
Because the carbon dioxide in the flue gas can not liquefy fully, so still contains the carbon dioxide of higher concentration in the tail gas.In this city embodiment, the compressor 41 that again enters flue gas compression set 40 through the tail gas after heat exchanger 62 heat exchange re-starts the separation of carbon dioxide.
In the above-mentioned carbon dioxide in flue gas method of purification, make through flue gas and the Cryogenic air of pressurization and carry out heat exchange, make the high pressure flue gas become the high pressure low temperature flue gas, under the condition of high pressure low temperature, the partial CO 2 liquefaction in the flue gas generates liquid carbon dioxide, is 1.5MPa ~ 2.5MPa at air pressure, temperature is under-25 ℃～-35 ℃ the condition, other gases can not liquefy in the flue gas, thereby the co 2 liquefaction in the flue gas is separated with other gases and impurity in the flue gas, and purifying technique is comparatively simple; And the pre-cooled air of the cryogenic gas that other do not liquefy and process carries out heat exchange, with the cold recovery utilization, thus the comprehensive utilization of realization energy.
Need to prove, each step might not be according to cited carrying out smoothly in the carbon dioxide in flue gas method of purification, the step (step S101 is to step S106) that forms the high pressure flue gas such as the processing that flue gas is carried out can be carried out simultaneously with the step (step S107 is to step S109) that the processing that air is carried out forms Cryogenic air, forms the high pressure low temperature flue gas as long as make high pressure flue gas and Cryogenic air carry out heat exchange.
Be appreciated that step S101 can omit to step S103, direct execution in step S104 compressed flue gas and got final product this moment.Need not purification, sulphur removal and steam when less when impurity in the flue gas is less, step S105 and step S106 also can omit, this moment will be through the air of step S104 compression direct and Cryogenic air carry out heat exchange and get final product.Need not to purify and steam when less when impurity in the air is less, step S106 and step S107 can omit, and this moment, directly execution in step S108 got final product.Step S108 also can omit, and directly air is cooled off the formation Cryogenic air this moment and gets final product.Step S109 can omit, and also can directly buy Cryogenic air this moment, need not self-control.Step S112 and step S113 can omit.
The above embodiment has only expressed several embodiment of the present utility model, and it describes comparatively concrete and detailed, but can not therefore be interpreted as the restriction to the utility model claim.Should be pointed out that for the person of ordinary skill of the art without departing from the concept of the premise utility, can also make some distortion and improvement, these all belong to protection domain of the present utility model.Therefore, the protection domain of the utility model patent should be as the criterion with claims.
Claims (10)
1. carbon dioxide in flue gas purification system, the carbon dioxide for separating of in, the flue gas that contains carbon dioxide of purifying is characterized in that described carbon dioxide in flue gas purification system comprises:
The flue gas compression set is used for the flue gas pressurization is formed the high pressure flue gas;
Air refrigerating devie is used for the air cooling is formed Cryogenic air;
Heat-exchange device, be communicated with described flue gas compression set and described air refrigerating devie, described heat-exchange device is used for described high pressure flue gas and described Cryogenic air are carried out heat exchange formation high pressure low temperature flue gas, so that part co 2 liquefaction in the described high pressure low temperature flue gas;
Gas-liquid separation device is for separating of the carbon dioxide that liquefies in the described high pressure low temperature flue gas.
2. carbon dioxide in flue gas purification system according to claim 1, it is characterized in that, described carbon dioxide in flue gas purification system also comprises the flue gas desulfur device that is communicated with described flue gas compression set, and described flue gas desulfur device is used for removing the sulfur dioxide of described flue gas before described flue gas pressurization forms the high pressure flue gas.
3. carbon dioxide in flue gas purification system according to claim 2 is characterized in that, described flue gas desulphurization system comprises:
The low temperature plasma device, the oxidizing sulfur dioxide that is used for flue gas is sulfur trioxide;
The alkali lye contact chamber is communicated with described low temperature plasma device, and described alkali lye contact chamber is used for the sulfur trioxide of described flue gas and alkaline reaction generation are contained SO
4 2-Solution;
Wherein, the alkali lye contact chamber is communicated with the flue gas compression set, makes the flue gas of removing sulfur trioxide through described alkali lye contact chamber be delivered to described flue gas compression set compression and forms the high pressure flue gas.
4. carbon dioxide in flue gas purification system according to claim 3 is characterized in that, described flue gas desulphurization system comprises calcium source contact chamber, and described calcium source contact chamber is communicated with described alkali lye contact chamber by pipeline, and described calcium source contact chamber is used for the described SO that contains
4 2-Solution and calcium source reaction generate calcium sulfate and reclaim alkali lye, the calcium source of accommodating in the contact chamber of described calcium source is calcium oxide, calcium hydroxide or aqua calcis.
5. carbon dioxide in flue gas purification system according to claim 1, it is characterized in that, described carbon dioxide in flue gas purification system also comprises the molecular sieve that is communicated with described flue gas compression set, and described molecular sieve is used for improving the concentration of described carbon dioxide in flue gas.
6. carbon dioxide in flue gas purification system according to claim 1, it is characterized in that, described flue gas compression set comprises the compressor that is communicated with successively, cooler, oil water separator, drier and accurate filter, described compressor is used for the compression flue gas, described cooler is for reducing the temperature of the flue gas of described compressor output, described oil water separator is used for removing the profit through the flue gas of described cooler cooling, described drier is used for the flue gas that purifies through described oil water separator is dehydrated, and described accurate filter is used for removing the dust of the flue gas after dehydrating through described drier.
7. carbon dioxide in flue gas purification system according to claim 1, it is characterized in that, described carbon dioxide in flue gas purification system also comprises the flue gas pre-cooler that is communicated with described flue gas compression set, and described flue gas pre-cooler comprises air-introduced machine and the cooler that is communicated with air-introduced machine.
8. carbon dioxide in flue gas purification system according to claim 1, it is characterized in that, described carbon dioxide in flue gas purification system also comprises the air cleaning unit that is communicated with described air refrigerating devie, described air cleaning unit comprises the air compressor that is communicated with successively, oil water separator, drier and accurate filter, described oil water separator is used for removing the airborne profit through described air compressor compression, described drier is used for the air that purifies through described oil water separator is dehydrated, and described accurate filter is used for removing the airborne dust after dehydrating through described drier.
9. carbon dioxide in flue gas purification system according to claim 1, it is characterized in that, described carbon dioxide in flue gas purification system also comprises the air precooler that is communicated with described air refrigerating devie, described air precooler comprises cooler and the heat exchanger that is communicated with described cooler, described cooler is used for carrying out pre-cooled to air, described heat exchanger is communicated with described gas-liquid separation device, and described heat exchanger is used for separating the tail gas of removing carbon dioxide with the described gas-liquid separation device of process through the air of described cooler cooling and carries out heat exchange.
10. carbon dioxide in flue gas purification system according to claim 1, it is characterized in that, it is 1.5MPa～2.5MPa that described heat-exchange device is used for described high pressure flue gas and described Cryogenic air are carried out heat exchange formation air pressure, and temperature is-25 ℃～-35 ℃ high pressure low temperature flue gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220206246 CN202902749U (en) | 2012-05-09 | 2012-05-09 | Carbon dioxide in flue gas purification system |
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| CN 201220206246 CN202902749U (en) | 2012-05-09 | 2012-05-09 | Carbon dioxide in flue gas purification system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102706102A (en) * | 2012-05-09 | 2012-10-03 | 深圳市明鑫高分子技术有限公司 | System and method for purifying carbon dioxide in flue gas |
| WO2021103023A1 (en) * | 2019-11-30 | 2021-06-03 | 惠州凯美特气体有限公司 | Process method for recovering carbon dioxide by purifying chemical waste gas |
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2012
- 2012-05-09 CN CN 201220206246 patent/CN202902749U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102706102A (en) * | 2012-05-09 | 2012-10-03 | 深圳市明鑫高分子技术有限公司 | System and method for purifying carbon dioxide in flue gas |
| CN102706102B (en) * | 2012-05-09 | 2014-12-10 | 深圳市明鑫高分子技术有限公司 | System and method for purifying carbon dioxide in flue gas |
| WO2021103023A1 (en) * | 2019-11-30 | 2021-06-03 | 惠州凯美特气体有限公司 | Process method for recovering carbon dioxide by purifying chemical waste gas |
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