CN102706102A - System and method for purifying carbon dioxide in flue gas - Google Patents
System and method for purifying carbon dioxide in flue gas Download PDFInfo
- Publication number
- CN102706102A CN102706102A CN2012101421259A CN201210142125A CN102706102A CN 102706102 A CN102706102 A CN 102706102A CN 2012101421259 A CN2012101421259 A CN 2012101421259A CN 201210142125 A CN201210142125 A CN 201210142125A CN 102706102 A CN102706102 A CN 102706102A
- Authority
- CN
- China
- Prior art keywords
- flue gas
- air
- carbon dioxide
- high pressure
- low temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Treating Waste Gases (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The invention relates to a system for purifying carbon dioxide in flue gas, which is used for separating and purifying carbon dioxide in carbon-dioxide-containing flue gas. The system comprises a flue gas compressor, an air refrigerator, a heat exchanger and a gas-liquid separator, wherein the flue gas compressor is used for compressing the flue gas to form high-pressure flue gas; the air refrigerator is used for cooling air to form low-temperature air; the heat exchanger is communicated with the flue gas compressor and the air refrigerator; the heat exchanger is used for exchanging heat between the high-pressure flue gas and the low-temperature air to form high-pressure low-temperature flue gas, so that the part of carbon dioxide in the high-pressure low-temperature flue gas is liquefied; and the gas-liquid separator is used for separating the liquefied carbon dioxide in the high-pressure low-temperature flue gas. The system for purifying carbon dioxide in flue gas is simple. The invention also provides a method for purifying carbon dioxide in flue gas.
Description
Technical field
The present invention relates in a kind of flue gas carbon dioxide method of purification in the CO 2 purification system and flue gas.
Background technology
Coal also has irreplaceable status as the basic energy resource of China in 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.
After the carbon dioxide purifying technique at first carries out the solution adsorption and enrichment to flue gas usually in the existing flue gas, solution is carried out the heating evaporation carbon dioxide, and the carbon dioxide of collection liquefaction reuses.Yet, need 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 make the carbon dioxide purifying technique comparatively complicated, be unfavorable for the popularization of carbon trapping technique.
Summary of the invention
Based on this, be necessary to provide in a kind of comparatively simple flue gas carbon dioxide method of purification in the CO 2 purification system and flue gas.
CO 2 purification system in a kind of flue gas, the carbon dioxide of the flue gas that contains carbon dioxide of being used for separating, purifying, CO 2 purification system comprises in the said flue gas:
The flue gas compression set is used for the flue gas pressurization is formed the high pressure flue gas;
The air cooling device is used for the air cooling is formed Cryogenic air;
Heat-exchange device; Be communicated with said flue gas compression set and said air cooling device; Said heat-exchange device is used for said high pressure flue gas and said Cryogenic air are carried out heat exchange formation high pressure low temperature flue gas, so that part co 2 liquefaction in the said high pressure low temperature flue gas;
Gas-liquid separation device is used for separating the carbon dioxide that said high pressure low temperature flue gas liquefies.
Therein among embodiment; CO 2 purification system also comprises the flue gas desulfur device that is communicated with said flue gas compression set in the said flue gas, and said flue gas desulfur device is used for before said flue gas pressurization forms the high pressure flue gas, removing said sulfur in smoke.
Carbon dioxide method of purification in a kind of flue gas may further comprise the steps:
The compression flue gas forms the high pressure flue gas;
Said high pressure flue gas and Cryogenic air are carried out heat exchange formation high pressure low temperature flue gas, so that part co 2 liquefaction in the said high pressure low temperature flue gas, the air pressure of wherein said high pressure low temperature flue gas is 1.5MPa ~ 2.5MPa, and temperature is-25 ℃～-35 ℃;
Tail gas after separating the carbon dioxide of the liquefaction in the said high pressure low temperature flue gas and removing the carbon dioxide of liquefaction.
Among embodiment, said flue gas carries out desulfurization to flue gas earlier before compression handles to remove sulfur in smoke therein.
Among embodiment, remove sulfur in smoke and may further comprise the steps therein:
Flue gas is carried out low temperature plasma excite oxidation, make sulfur in smoke be oxidized to sulfur trioxide;
To pass through flue gas and alkaline reaction that low temperature plasma excites oxidation, and said sulfur trioxide in smoke gas and alkaline reaction solution reaction generated contain SO
4 2-Solution, said alkali lye is sodium hydroxide solution or potassium hydroxide solution.
Among embodiment, said flue gas uses molecular sieve to improve gas concentration lwevel in the flue gas before compression earlier therein.
Therein among embodiment, after the compression flue gas forms the high pressure flue gas, carry out cooling off successively before the heat exchange with said Cryogenic air, water-oil separating and dehydrate processing.
Therein among embodiment, said flue gas is carrying out water-oil separating and is dehydrating the back, carries out carrying out secondary filter to remove the dust in the flue gas before the heat exchange with said Cryogenic air.
Among embodiment, said Cryogenic air is prepared by following steps therein: air is compressed successively, water-oil separating, dehydrates and secondary filter forms and purifies air to remove airborne steam and minute impurities; Cool off said purifying air to form Cryogenic air.
Among embodiment, said Cryogenic air is prepared by following steps therein: air is compressed successively, water-oil separating, dehydrates and secondary filter forms and purifies air to remove airborne steam and minute impurities; Cool off said purifying air to form Cryogenic air.
Carbon dioxide method of purification in CO 2 purification system and the flue gas in the above-mentioned flue gas; Make through the 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; Partial CO 2 liquefaction in the flue gas generates liquid carbon dioxide; At air pressure is 1.5MPa ~ 2.5MPa, and temperature is that other gases can not liquefy in the flue gas under-25 ℃～-35 ℃ the condition; Thereby the co 2 liquefaction in the flue gas is separated with other gases and impurity in the flue gas, and purification system and purifying technique are all comparatively simple.
Description of drawings
Fig. 1 is the structural representation of CO 2 purification system in the flue gas 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 present invention, will more comprehensively describe the present invention with reference to relevant drawings below.Provided first-selected embodiment of the present invention in the accompanying drawing.But the present invention can realize with many different forms, be not limited to embodiment described herein.On the contrary, the purpose of these embodiment being provided is to make to disclosure of the present invention more thoroughly comprehensively.
Need to prove, when element is called as " being fixedly arranged on " another element, it can be directly on another element or also can have element placed in the middle.When an element is considered to " connection " another element, it can be to be directly connected to another element or possibly to have element placed in the middle simultaneously.Term as used herein " vertical ", " level ", " left side ", " right side " and similar statement are just for illustrative purposes.
Only if definition is arranged in addition, the employed all technology of this paper are identical with the implication that belongs to those skilled in the art's common sense of the present invention with scientific terminology.Among this paper in specification of the present invention employed term be not intended to be restriction the present invention just in order to describe the purpose of concrete embodiment.Term as used herein " and/or " comprise one or more relevant Listed Items arbitrarily with all combinations.
See also Fig. 1; CO 2 purification system 100 carbon dioxide of the flue gas that contains carbon dioxide that is used for separating, purifies in the flue gas of one embodiment, CO 2 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 cooling device 70, heat-exchange device 80, air emptier 85, gas-liquid separation device 90 and carbon dioxide collecting device 95 in the flue gas.
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, contact chamber, calcium source 25, retracting device 26 and calcium sulfate gathering-device 27.
Low temperature plasma device 22 is used for sulfur in smoke is oxidized to sulfur trioxide.Low temperature plasma device 22 is communicated with cooler 14, gets into low temperature plasma device 22 through cooler 14 elementary cooled smoke.
Contain a large amount of high energy electrons, ion, excitation state ion in the plasma of low temperature plasma device 22 through 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 open the gas molecule key on the one hand and generate some nitrogen-atoms molecule and solia particles, excite airborne oxygen, water vapour on the other hand, form ozone, O-and hydroxyl free from extremely strong oxidants such as bases.It is the electrochemical reaction of the complicacy of collective with active ion or free radical that these oxidants and sulfur in smoke take place a series of, finally makes Sulphur Dioxide become sulfur trioxide.
Alkali lye contact chamber 24 is used for 120 alkaline reaction generation in the sulfur trioxide that generates through the low-temperature plasma device oxidation and the alkali lye contact chamber is contained 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%.
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 following:
2ROH+SO
3→R
2SO
4+H
2O
Wherein, R is K or Na.
In this embodiment, alkali lye contact chamber 24 is communicated with low temperature plasma device 22 through pipeline.Contain the alkali lye that is used for the sulfur trioxide reaction in the alkali lye contact chamber 24.Specifically in this 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 the spray of the flue gas in feeding alkali lye contact chamber 24 alkali lye, makes the abundant haptoreaction generation of alkali lye of flue gas and atomizing contain SO
4 2-Solution.It is pointed out that micro-spray device can omit, also can directly feed flue gas in the alkali lye this moment, and sulfur trioxide in smoke gas and alkali lye are reacted.
Contact chamber, calcium source 25 is used for the SO that contains with 24 generations of alkali lye contact chamber
4 2-Solution and calcium source reaction conversion be 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 water react, 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 following:
R
2SO
4+Ca(OH)
2→Ca
2SO
4+2ROH
Wherein, R is K or Na, calcium sulfate (Ca
2SO
4) be slightly soluble in water, repeatedly reaction back calcium sulfate exists with precipitation form.
In this embodiment, contact chamber, calcium source 25 is communicated with alkali lye contact chamber 24 through pipeline.
Specifically in this embodiment, be provided with reaction tank in the contact chamber, calcium source 25, the calcium source is contained in the reaction tank, can be with the SO that contains that produces in the alkali lye contact chamber 24 during use
4 2-Solution feed in the reaction tank through pipeline, reacting with calcium source in the reaction tank generates calcium sulfate precipitation and reclaims alkali lye.In other embodiments, can the adding of the calcium source in the contact chamber, calcium source be contained SO
4 2-Solution in react.
Calcium sulfate gathering-device 27 is used to collect the calcium sulfate that produces in the contact chamber, calcium source 25.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 used to reduce 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 cooling device 70 and flue gas compression set 40 simultaneously.Cryogenic air through 70 preparations of air cooling device 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 ℃ a 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.In heat-exchange device 80, carrying out air after the heat exchange gets in the air emptier 85 and passes through 85 emptyings of air tapping equipment.
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 in heat-exchange device 80, carries out after the heat exchange gets into 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 subcooler 61 pre-cooled air.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 gets into flue gas compression set 40 through the tail gas after heat exchanger 62 heat exchange once more carries out the separation of carbon dioxide again.
Carbon dioxide collecting device 95 is used to collect 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 CO 2 purification system 100,40 pairs of flue gases of flue gas compression set pressurize and form the high pressure flue gas in the above-mentioned flue gas, and air cooling device 70 forms Cryogenic air with the air cooling; High pressure flue gas and Cryogenic air are carried out heat exchange through heat-exchange device 80; Making the high pressure flue gas become the high pressure low temperature flue gas, adopt high pressure, low temperature mode to make the partial CO 2 liquefaction in the flue gas generate 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 separates with other gases and impurity in the flue gas, and are comparatively simple; And the cryogenic gas that other do not liquefy can be in heat exchanger 67 be used for cold recovery the precooling of the air of air cooling device 70, 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, and when sulfur dioxide in flue gas content was low, flue gas desulfur device 20 can omit; Molecular sieve 30 can omit, and directly be delivered to flue gas compression set 40 with flue gas and be collapsed into the high pressure flue gas and get final product this moment; In flue gas oil gas, steam and dust more after a little while, cooler 42, oil water separator 43, drier 44 and accurate filter 45 can omit, and directly the flue gas of compression are delivered to heat-exchange device 80 and get final product; Same, in air oil gas, steam and dust more after a little while, air cleaning unit 50 can omit, directly be delivered to air precooler 60 with air and get final product this moment; Air precooler 60 can omit, and directly be delivered to air cooling device 70 with air and get final product this moment.
Please consult Fig. 1 to Fig. 2 simultaneously, the carbon dioxide method of purification carbon dioxide of the flue gas that contains carbon dioxide that is used for separating, purifies in the flue gas of an embodiment may further comprise the steps:
Step S101, flue gas is carried out pre-cooled processing.
Temperature when fume emission comes out 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 this 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 this embodiment, use 14 pairs of flue gases of cooler to carry out pre-cooled.
Step S102, flue gas is carried out desulfurization handle.
Flue gas is carried out the desulfurization processing may further comprise the steps:
Flue gas is carried out low temperature plasma excite oxidation, make sulfur in smoke be oxidized to sulfur trioxide;
To pass through flue gas and alkaline reaction that low temperature plasma excites oxidation, and said sulfur trioxide in smoke gas and alkaline reaction solution reaction generated 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 be with containing SO
4 2-The reaction of solution and calcium source, regather and contain SO
4 2-The calcium sulfate that generates of solution and calcium source reaction and reclaim alkali lye, and the recovery alkali lye that will collect is used for exciting with the process low temperature plasma smoke reaction of oxidation.
In this embodiment, use 20 pairs of flue gases of flue gas desulfur device to carry out desulfurization and handle.
Step S103, use molecular sieve improve the concentration of carbon dioxide in the flue gas.
Flue gas after handling through desulfurization gets into molecular sieve 30, makes that the volumn concentration of carbon dioxide is increased to more than 50% in the flue gas.
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 this embodiment, use 41 pairs of flue gases of handling 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 the back temperature and is reduced to 35 ℃ ~ 55 ℃.In this embodiment, the high pressure flue gas that 41 compressions form through compressor at first gets into cooler 42 and cools off the temperature with the flue gas that reduces compressor 41 outputs.
Flue gas through subcooler 42 coolings uses oil water separator 43 to remove the profit in the flue gas, flue.In this embodiment, oil water separator 43 is a cyclone separator.
The flue gas of removing profit through water-oil separating uses drier 44 to dehydrate to remove the steam in the flue gas.
Step S106, flue gas is carried out secondary filter remove the impurity in the flue gas
In this 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 handled and to be purified air with formation.
In this 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 to remove dust in air and particle through drying and dehydrating.
Preferably, oil water separator 52 is a cyclone separator.
Step S108, carry out purifying air pre-cooled.
In this embodiment, use cooler 61 will pass through to purify air and be precooled to normal temperature.
Step S109, cool off purifying air to form Cryogenic air.
The temperature of Cryogenic air is-40 ℃～-60 ℃.
In this embodiment, use air cooling device 70 air to be cooled to-40 ℃～-60 ℃.Preferably, air cooling device 70 is an air wave refrigerating device.
The air pressure of Cryogenic air is 0.6MPa ~ 1.2MPa, is preferably 0.8MPa.
Step S110, the flue gas that will pass through secondary filter and Cryogenic air are carried out heat exchange and are formed 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 this embodiment, carry out heat exchange through heat-exchange device 80, make the high pressure flue gas become the high pressure low temperature flue gas through the flue gas and the Cryogenic air of secondary filter.At air pressure is 1.5MPa ~ 2.5MPa, and temperature is under-25 ℃～-35 ℃ the condition, and the partial CO 2 liquefaction in the flue gas generates liquid carbon dioxide.
Cryogenic air becomes normal temperature air through after the heat exchange, can discharge, and in this embodiment, normal temperature air is through 85 emptyings of air emptier.
Step S110, separate the carbon dioxide of the liquefaction in the said 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 in heat-exchange device 80, carries out forming after the heat exchange gets into 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 this embodiment, use carbon dioxide collecting device 95 collection liquid carbon dioxides and liquid towards carbon dioxide to carry out can.
Step S112, with tail gas with carry out heat exchange through pre-cooled air.
Temperature through the tail gas after separating is lower, can be used as low-temperature receiver to carrying out pre-cooled once more through pre-cooled air.In this embodiment, the air pre-cooled through tail gas after separating and process passes through heat exchanger 62 heat exchange.
Step S113, the tail gas that will pass through heat exchange separate purification again.
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 gets into flue gas compression set 40 through the tail gas after heat exchanger 62 heat exchange once more carries out the separation of carbon dioxide again.
In the carbon dioxide method of purification, make through the flue gas and the Cryogenic air of pressurization and carry out heat exchange in the above-mentioned flue gas, 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 cryogenic gas that other do not liquefy carries out heat exchange with the pre-cooled air of process, with the cold recovery utilization, thus the comprehensive utilization of realization energy.
Need to prove; In the flue gas in the carbon dioxide method of purification each step might not carry out according to cited order; 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 with the step (step S107 is to step S109) that the processing that air is carried out forms Cryogenic air simultaneously, 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.Impurity is less in flue gas need not purification, sulphur removal and steam more after a little while, and step S105 and step S106 also can omit, will pass through this moment step S104 air compressed directly and Cryogenic air carry out heat exchange and get final product.In air impurity less need not to purify and steam more after a little while, step S106 and step S107 can omit, 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 kinds of embodiments of the present invention, and it describes comparatively concrete and detailed, but can not therefore be interpreted as the restriction to claim of the present invention.Should be pointed out that for the person of ordinary skill of the art under the prerequisite that does not break away from the present invention's design, can also make some distortion and improvement, these all belong to protection scope of the present invention.Therefore, the protection domain of patent of the present invention should be as the criterion with accompanying claims.
Claims (10)
1. CO 2 purification system in the flue gas, the carbon dioxide of the flue gas that contains carbon dioxide of being used for separating, purifying is characterized in that CO 2 purification system comprises in the said flue gas:
The flue gas compression set is used for the flue gas pressurization is formed the high pressure flue gas;
The air cooling device is used for the air cooling is formed Cryogenic air;
Heat-exchange device; Be communicated with said flue gas compression set and said air cooling device; Said heat-exchange device is used for said high pressure flue gas and said Cryogenic air are carried out heat exchange formation high pressure low temperature flue gas, so that part co 2 liquefaction in the said high pressure low temperature flue gas;
Gas-liquid separation device is used for separating the carbon dioxide that said high pressure low temperature flue gas liquefies.
2. CO 2 purification system in the flue gas according to claim 1; It is characterized in that; CO 2 purification system also comprises the flue gas desulfur device that is communicated with said flue gas compression set in the said flue gas, and said flue gas desulfur device is used for before said flue gas pressurization forms the high pressure flue gas, removing said sulfur in smoke.
3. carbon dioxide method of purification in the flue gas is characterized in that, may further comprise the steps:
The compression flue gas forms the high pressure flue gas;
Said high pressure flue gas and Cryogenic air are carried out heat exchange formation high pressure low temperature flue gas, so that part co 2 liquefaction in the said high pressure low temperature flue gas, the air pressure of wherein said high pressure low temperature flue gas is 1.5MPa ~ 2.5MPa, and temperature is-25 ℃～-35 ℃;
Tail gas after separating the carbon dioxide of the liquefaction in the said high pressure low temperature flue gas and removing the carbon dioxide of liquefaction.
4. carbon dioxide method of purification in the flue gas according to claim 3 is characterized in that, said flue gas carries out desulfurization to flue gas earlier before compression handles to remove sulfur in smoke.
5. carbon dioxide method of purification in the flue gas according to claim 4 is characterized in that, removes sulfur in smoke and may further comprise the steps:
Flue gas is carried out low temperature plasma excite oxidation, make sulfur in smoke be oxidized to sulfur trioxide;
To pass through flue gas and alkaline reaction that low temperature plasma excites oxidation, and said sulfur trioxide in smoke gas and alkaline reaction solution reaction generated contain SO
4 2-Solution, said alkali lye is sodium hydroxide solution or potassium hydroxide solution.
6. carbon dioxide method of purification in the flue gas according to claim 3 is characterized in that, said flue gas uses molecular sieve to improve gas concentration lwevel in the flue gas before compression earlier.
7. carbon dioxide method of purification in the flue gas according to claim 3 is characterized in that, after the compression flue gas forms the high pressure flue gas, carry out cooling off successively before the heat exchange with said Cryogenic air, water-oil separating and dehydrate processing.
8. carbon dioxide method of purification in the flue gas according to claim 7 is characterized in that, said flue gas is carrying out water-oil separating and dehydrating the back, carries out carrying out secondary filter to remove the dust in the flue gas before the heat exchange with said Cryogenic air.
9. carbon dioxide method of purification in the flue gas according to claim 3; It is characterized in that said Cryogenic air is prepared by following steps: air is compressed successively, water-oil separating, dehydrates and secondary filter forms and purifies air to remove airborne steam and minute impurities; Through cooling off said purifying air to form Cryogenic air.
10. carbon dioxide method of purification in the flue gas according to claim 9 is characterized in that, said purifying air carried out heat exchange with said tail gas and carried out pre-cooled before cooling forms Cryogenic air.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210142125.9A CN102706102B (en) | 2012-05-09 | 2012-05-09 | System and method for purifying carbon dioxide in flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210142125.9A CN102706102B (en) | 2012-05-09 | 2012-05-09 | System and method for purifying carbon dioxide in flue gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102706102A true CN102706102A (en) | 2012-10-03 |
| CN102706102B CN102706102B (en) | 2014-12-10 |
Family
ID=46899056
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210142125.9A Active CN102706102B (en) | 2012-05-09 | 2012-05-09 | System and method for purifying carbon dioxide in flue gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102706102B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104755153A (en) * | 2012-10-24 | 2015-07-01 | 株式会社Ihi | System for removal of impurities by compressor |
| CN108376001A (en) * | 2018-01-31 | 2018-08-07 | 中国科学院合肥物质科学研究院 | A kind of particulate matter humidity quick control device and its control method |
| 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 |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1289720A (en) * | 2000-10-17 | 2001-04-04 | 重庆理想科技有限公司 | Process for preparing food-class high-purity liquid CO2 |
| CN1353085A (en) * | 2000-11-14 | 2002-06-12 | 湖南凯美特干冰有限公司 | Dynamic vacuumizing process for purifying CO2 |
| CN1626271A (en) * | 2003-12-14 | 2005-06-15 | 徐宝安 | Equipment of desulfurizing fume by alkalifying method, through dissolved in cold water and electrolysis of removing hard water |
| CN101052852A (en) * | 2004-07-16 | 2007-10-10 | 斯塔托伊尔公司 | Method and device for liquifiing carbon dioxide |
| CN101343061A (en) * | 2008-08-15 | 2009-01-14 | 杭州快凯高效节能新技术有限公司 | Method and apparatus for preparing food level liquid carbon dioxide with flue gas |
| CN101522286A (en) * | 2006-08-07 | 2009-09-02 | 阿尔斯托姆科技有限公司 | Method for separating CO2 from a gas flow CO2 separating device for carrying out said method swirl nozzle for a CO2 separating device and use of the CO2 separating device |
| CN101556103A (en) * | 2008-04-09 | 2009-10-14 | 西门子公司 | Method and device for co2 liquefaction |
| CN202902749U (en) * | 2012-05-09 | 2013-04-24 | 深圳市明鑫高分子技术有限公司 | Carbon dioxide in flue gas purification system |
-
2012
- 2012-05-09 CN CN201210142125.9A patent/CN102706102B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1289720A (en) * | 2000-10-17 | 2001-04-04 | 重庆理想科技有限公司 | Process for preparing food-class high-purity liquid CO2 |
| CN1353085A (en) * | 2000-11-14 | 2002-06-12 | 湖南凯美特干冰有限公司 | Dynamic vacuumizing process for purifying CO2 |
| CN1626271A (en) * | 2003-12-14 | 2005-06-15 | 徐宝安 | Equipment of desulfurizing fume by alkalifying method, through dissolved in cold water and electrolysis of removing hard water |
| CN101052852A (en) * | 2004-07-16 | 2007-10-10 | 斯塔托伊尔公司 | Method and device for liquifiing carbon dioxide |
| CN101522286A (en) * | 2006-08-07 | 2009-09-02 | 阿尔斯托姆科技有限公司 | Method for separating CO2 from a gas flow CO2 separating device for carrying out said method swirl nozzle for a CO2 separating device and use of the CO2 separating device |
| CN101556103A (en) * | 2008-04-09 | 2009-10-14 | 西门子公司 | Method and device for co2 liquefaction |
| CN101343061A (en) * | 2008-08-15 | 2009-01-14 | 杭州快凯高效节能新技术有限公司 | Method and apparatus for preparing food level liquid carbon dioxide with flue gas |
| CN202902749U (en) * | 2012-05-09 | 2013-04-24 | 深圳市明鑫高分子技术有限公司 | Carbon dioxide in flue gas purification system |
Non-Patent Citations (2)
| Title |
|---|
| 《广东化工》 20090930 李清方 烟气联合脱硫脱硝技术综述 第36卷, 第9期 * |
| 李清方: "烟气联合脱硫脱硝技术综述", 《广东化工》, vol. 36, no. 9, 30 September 2009 (2009-09-30) * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104755153A (en) * | 2012-10-24 | 2015-07-01 | 株式会社Ihi | System for removal of impurities by compressor |
| CN104755153B (en) * | 2012-10-24 | 2016-08-24 | 株式会社Ihi | Compressor impurity removes system |
| CN108376001A (en) * | 2018-01-31 | 2018-08-07 | 中国科学院合肥物质科学研究院 | A kind of particulate matter humidity quick control device and its control method |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102706102B (en) | 2014-12-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108452632B (en) | VOCs recovery system utilizing air deep cooling | |
| CN102000486B (en) | Method for catching carbon dioxide in flue gas by active sodium carbonate and apparatus thereof | |
| CN101343061B (en) | Method and apparatus for preparing food level liquid carbon dioxide with flue gas | |
| CN102227248A (en) | Carbon dioxide purification using activated carbon as nox and so2 sorbent / catalyst | |
| CN107081045A (en) | The method and its special equipment of a kind of collecting carbon dioxide from fuel gas | |
| CN102706102B (en) | System and method for purifying carbon dioxide in flue gas | |
| US9375673B2 (en) | CO2 separation unit | |
| CN110407237B (en) | Method for jointly preparing electric vehicle-grade lithium carbonate and lithium hydroxide monohydrate | |
| CN202902749U (en) | Carbon dioxide in flue gas purification system | |
| CN108722118B (en) | Low-energy-consumption desulfurizer regeneration method and desulfurization method | |
| CN202212084U (en) | Purification treatment system for sulfur hexafluoride gas decomposition product | |
| WO2023066134A1 (en) | System and method for preparing nitrogen from waste gas obtained by recovering co2 via chemical method | |
| CN110407236B (en) | Preparation method of electric automobile-grade lithium carbonate | |
| CN103182232A (en) | Method for processing microscale dust in tail gas of calcium carbide furnace | |
| JP2011231002A (en) | Method of collecting and liquefying carbon dioxide from mixed gas | |
| CN111675220B (en) | CO-containing in tail gas from carbonate production 2 Extraction and refining system | |
| US20150101484A1 (en) | Emission gas treatment method and emission gas treatment apparatus | |
| CN203737087U (en) | Boiler tail flue gas compressing and centralized treating system | |
| CN101845329B (en) | Method for using waste heat boiler flue gas as pneumatic ash conveying inert gas of flammable and combustible system | |
| CN215085832U (en) | Ultralow emission system for tail gas washing of spray roasting hydrochloric acid regeneration device | |
| CN106731497B (en) | Decarbonizing and extracting N from nitric acid industrial tail gas 2 O purification device and process method | |
| CN102294168A (en) | Method for processing flue gas | |
| CN102441951A (en) | Continuous recovery system for polyurethane foam blowing agent of waste refrigerator | |
| CN112919413A (en) | Novel process for purifying and separating hydrogen produced by coal gas | |
| CN107140602B (en) | System and method for regenerating red smoke-free waste liquid from small high-concentration acid washing |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |