CN201558659U - Flue gas carbon dioxide capture device and regenerator thereof - Google Patents
Flue gas carbon dioxide capture device and regenerator thereof Download PDFInfo
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- CN201558659U CN201558659U CN2009202777885U CN200920277788U CN201558659U CN 201558659 U CN201558659 U CN 201558659U CN 2009202777885 U CN2009202777885 U CN 2009202777885U CN 200920277788 U CN200920277788 U CN 200920277788U CN 201558659 U CN201558659 U CN 201558659U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
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- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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Abstract
The utility model discloses a flue gas carbon dioxide capture device, which comprises an absorbing system, a regeneration system and a heat exchanging system. The regeneration system includes a regenerator, and the lower portion of the regenerator is provided with a barren liquor tank, while the upper portion is provided with a rich liquor sprinkler and a chilling sprinkler, accordingly forming a regeneration area and a chilling area in the regenerator. The utility model further discloses a regenerator for the flue gas carbon dioxide capture device. The device and the regenerator can effectively carry out heat dispensation for the system, reduces circulation speed of barren liquor and rich liquor, and reduces temperature of the barren liquor discharged from the barren liquor and rich liquor heat exchanger and fluid passing through a regeneration gas condenser, thereby reducing load of cooling water, reducing system energy consumption and electric consumption, reducing expensive system inner parts, reducing height of the regenerator, and reducing manufacturing cost of the system.
Description
Technical field
The utility model relates to flue gas CO
2The trapping technique field, the low pressure low concentration CO in especially coal-fired (oil, gas) station boiler (combustion machine), Industrial Boiler, lime burner furnace and the chemical process
2The recovery field is specifically related to the flue gas carbon dioxide capture equipment and the flue gas carbon dioxide capture equipment regenerator of combustion apparatus.
Background technology
The climate warming problem is the problem of the whole human development of influence, CO
2Be the main contributor of climate warming, and large-scale combustion apparatus is CO
2Maximum emission source anyly wants to control on a large scale CO
2Discharging, the reply climate warming, all must put forth effort on large-scale combustion apparatus is carried out CO
2Capture.
Large-scale combustion apparatus is caught and is captured after carbon mainly contains the preceding capture of burning, oxygen-enriched combustion technology and burning.Capture before the burning and be mainly used in the IGCC power station, afterwards both then can apply to the transformation to traditional power plant.Wherein, oxygen-enriched combustion technology not only needs to increase oxygen generating plant, also needs existing generating body is transformed, and catches carbon after the burning and then need not transform body, has adaptability widely.Because traditional power station and other large-scale combustion apparatus flue gas have big flow, characteristics such as low dividing potential drop adopt the alkanolamine solution with alkalescence, are best suited for technology in this smoke characteristic as monoethanolamine (MEA).
It is ripe in chemical industry to utilize alkanolamine solution to carry out the technology that carbon captures from flue gas.But, because that large-scale combustion apparatus flue gas such as power plant has is large-minded, divide characteristics such as force down, the problem that this technology applies to power plant's maximum is the energy consumption height, volume is big.
China's utility application (application number is 200810018343.5) discloses a kind of trapping carbon dioxide in flue gas device, and it comprises Flue Gas Pretreatment Device, absorption tower and regenerator.
Wherein, the flue gas of handling through Flue Gas Pretreatment Device links to each other with the bottom on absorption tower by blower fan pressurization back, flue gas is bottom-up to flow, with go into from top, absorption tower tower can absorbing carbon dioxide ethanolamine solutions form counter current contacting, the flue gas that removes carbon dioxide is discharged through the tail gas evacuation port, the rich solution that has absorbed carbon dioxide is entered by regenerator top by the pressurization of rich solution pump, be provided with built-in boiling device in the regenerator bottom, the gas outlet, top of regenerator also successively with product gas rich solution heat exchanger, product gas cooler, gas-liquid separator links to each other with carbon-dioxide gas compressor, carbon dioxide after the separation is discharged after the carbon-dioxide gas compressor compression, and the lean solution behind the desorb carbon dioxide is gone out by the regenerator underflow.
The inventor finds that in above-mentioned collecting carbonic anhydride device, system energy consumption is big, the operating cost height.
The utility model content
The utility model purpose is to provide a kind of and has the flue gas carbon dioxide capture equipment of more low energy consumption than conventional art, to satisfy large-scale combustion apparatus, CO such as chemical industry
2Dividing potential drop is lower, the CO that need significantly cut down the consumption of energy
2Trapping system.Another purpose of the present utility model is to provide a kind of flue gas carbon dioxide capture equipment regenerator.
For this reason, on the one hand, the utility model provides a kind of flue gas carbon dioxide capture equipment, and it comprises: absorption system, utilize the carbon dioxide in the poor carbon dioxide absorption liquid absorption flue gas, to form carbon dioxide enriched absorption liquid; Regenerative system is used for the carbon dioxide of the carbon dioxide enriched absorption liquid of desorb, with the poor carbon dioxide absorption liquid that forms the carbon dioxide regeneration gas and recycle for absorption system; And heat-exchange system, for carbon dioxide enriched absorption liquid and poor carbon dioxide absorption liquid and/the carbon dioxide regeneration gas between heat exchange, wherein, regenerative system comprises regenerator, its underpart has the Quench spray thrower that lean solution groove, top have the rich solution spray thrower and be positioned at rich solution spray thrower top, wherein, the space on the liquid level of the poor carbon dioxide absorption liquid of lean solution groove, under the rich solution spray thrower forms the renewing zone, and the space between Quench spray thrower and the rich solution spray thrower forms chill zone.
Preferably, supply with the rich solution spray thrower after 70%～95% process heat-exchange system heat exchange of the carbon dioxide enriched absorption liquid that above-mentioned regenerative system provides, remaining directly supplies with the Quench spray thrower.
Preferably, the upper end of above-mentioned regenerator is provided with demister, and the rich solution spray thrower is arranged on 2/3～4/5 between lean solution tank liquor face and the demister and highly locates, and the Quench spray thrower is arranged between rich solution spray thrower and the demister.
Preferably, above-mentioned regenerative system also comprises regeneration gas cooler and the regeneration gas separator that is connected to regenerator, and wherein, the regeneration gas separator separates the liquid that obtains and mixes with the cooled poor carbon dioxide absorption liquid phase of lean solution cooler.
Preferably, above-mentioned heat-exchange system comprises: poor rich liquid heat exchanger; And the lean solution cooler, wherein, the poor carbon dioxide absorption liquid in the lean solution groove of regenerator is supplied with the lean solution spray thrower on absorption tower through lean solution cooler cooling back.
Preferably, the upper end of above-mentioned regenerator is provided with demister, and the rich solution spray thrower is arranged on 2/3～4/5 between lean solution tank liquor face and the demister and highly locates, and the Quench spray thrower is arranged between rich solution spray thrower and the demister.
Preferably, above-mentioned absorption system comprises at least one absorption tower that is connected with blower fan, the bottom on absorption tower has that rich solution groove, middle part have the self-loopa spray thrower, top has the lean solution spray thrower, the self-loopa spray thrower is arranged on 1/3～2/3 between rich solution tank liquor face and the lean solution spray thrower and highly locates, wherein, constitute the lean solution uptake zone between self-loopa spray thrower and the lean solution spray thrower, form the semi lean solution uptake zone between self-loopa spray thrower and the rich solution groove, the top of the lean solution spray thrower on absorption tower also has circulation cleaning system and demister.
In addition, the utility model also provides a kind of flue gas carbon dioxide capture equipment regenerator, the bottom of this regenerator has the lean solution groove and has the rich solution spray thrower and also be provided with the Quench spray thrower above the rich solution spray thrower with the evaporimeter, the top that are arranged in the lean solution groove, wherein, space on the liquid level of the poor carbon dioxide absorption liquid of lean solution groove, under the rich solution spray thrower forms the renewing zone, and the space between Quench spray thrower and the rich solution spray thrower forms chill zone.
Preferably, the upper end of above-mentioned regenerator is provided with demister, and the rich solution spray thrower is arranged on 2/3～4/5 between lean solution tank liquor face and the demister and highly locates, and the Quench spray thrower is arranged between rich solution spray thrower and the demister.
In the equipment of the utility model preferred embodiment, absorption tower and regenerator all adopt spray process, and increased circulation in the cover spray in the absorption tower, increased by a cover spray Quench system in regenerator, condensate liquid directly mixes with the lean solution behind the cooler behind the regenerator.On the one hand, can be effectively carry out heat and distribute, reduce rich or poor liquid circulation rate, reduce and lean solution behind the poor rich liquid heat exchanger and, thereby reduce the cooling water load, reduce system energy consumption and power consumption through the temperature of fluid behind the regeneration gas condenser to system; On the other hand, reduce expensive system's internals, reduced the absorption tower height, thereby reduced the cost of system.
Except purpose described above, feature and advantage, the utility model also has other purpose, feature and advantage.Below with reference to figure, other purpose, feature and effect of the present utility model is described in further detail.
Description of drawings
Constitute this specification a part, be used for further understanding accompanying drawing of the present utility model and show preferred embodiment of the present utility model, and be used for illustrating principle of the present utility model with specification.Among the figure:
Fig. 1 is the structural representation according to the flue gas carbon dioxide capture equipment of the utility model preferred embodiment.
The specific embodiment
Below in conjunction with accompanying drawing embodiment of the present utility model is elaborated, but the multitude of different ways that the utility model can be defined by the claims and cover is implemented.Identical in the accompanying drawings parts are represented with identical label.
Flue gas carbon dioxide capture equipment of the present utility model comprises: absorption system, utilize the carbon dioxide in the poor carbon dioxide absorption liquid absorption flue gas, to form carbon dioxide enriched absorption liquid; Regenerative system is used for the carbon dioxide of the carbon dioxide enriched absorption liquid of desorb, with the poor carbon dioxide absorption liquid that forms the carbon dioxide regeneration gas and recycle for absorption system; And heat-exchange system, for carbon dioxide enriched absorption liquid and poor carbon dioxide absorption liquid and/the carbon dioxide regeneration gas between heat exchange.Elaborate respectively below in conjunction with the concrete characteristics of preferred embodiment to absorption system, regenerative system and the heat-exchange system of flue gas carbon dioxide capture equipment.
Fig. 1 is the structural representation according to the flue gas carbon dioxide capture equipment of the utility model preferred embodiment.As shown in Figure 1, in this preferred embodiment, the absorption system of flue gas carbon dioxide capture equipment is the fountain absorption system of band self-loopa, and this absorption system comprises the absorption tower 5 that is connected with air-introduced machine 2.
The bottom on this absorption tower 5 forms rich solution groove 1, middle part and is provided with self-circulation system, the top is made up of self-circulating pump 3 and self-loopa spray thrower 4 and is provided with absorption tower spray thrower 6 (perhaps being called the lean solution spray thrower) and washes circulation cleaning system, the upper end that pump 7 and hydrops groove 8 form by circulation and be provided with absorption tower demisting device 9.
So, the lean solution uptake zone 5-2 that constitutes between self-loopa spray thrower 4 and the absorption tower spray thrower 6, the semi lean solution uptake zone 5-1 that forms between self-loopa spray thrower 4 and the rich solution groove 1.Preferably, self-loopa spray thrower 4 is arranged on 1/3～2/3 between rich solution groove 1 liquid level and the absorption tower spray thrower 6 and highly locates, and links to each other with rich solution groove 1 by self-circulating pump.
So, when flue gas enters when entering the absorption tower 5 from the bottom on absorption tower 5, has higher concentration CO
2At first at semi lean solution uptake zone 5-1, with the lower solution reaction of concentration of absorbing that is atomized by self-loopa spray thrower 4; And then enter into the lean solution uptake zone, at CO
2With solution reaction, optimized reaction interval like this when concentration is low, improved the CO of rich solution with higher absorption agent concentration
2Loading.Thereby reduce rich or poor liquid internal circulating load, reduce the load of lean solution cooler and then reduce the consumption of system's heat loss and cooling water and fall low pump work, and can reduce the height on absorption tower.
The inventor finds that in the absorption tower that the lean solution uptake zone only is set, 1/3 to 1/2 place has absorbed about 90% CO under the tower
2, it is about 5% that half remaining tower height is only deviate from, and this is a bigger major reason of rich or poor liquid internal circulating load, and the utility model has been done above-mentioned improvement to the absorption tower in view of the above.
In this preferred embodiment, regenerative system is the fountain regenerative system of band Quench, it comprises regenerator 20, Quench spray thrower 15 and regenerator demister 16 that the bottom formation lean solution groove 21 of this regenerator 20, top are provided with regenerator spray thrower 14 (perhaps being called the rich solution spray thrower), upper end.
In the utility model, the Quench spray thrower is common spray thrower, is used to spray the rich solution from the absorption tower that does not heat up through heat exchange.The regenerator spray thrower is common spray thrower also, is used to spray the rich solution that heats up through heat exchange.
Like this, the space on the liquid level of the poor carbon dioxide absorption liquid of lean solution groove 21, under rich solution spray thrower 14 forms renewing zone 20-1, and the space between Quench spray thrower 14 and the rich solution spray thrower 14 forms chill zone 20-2.The temperature of the relative renewing zone 20-1 of the temperature of chill zone 20-2 reduces significantly, for example reduces by 30～50 ℃, is called chill zone.
The part rich solution directly enters the absorption tower by Quench spray thrower 15 without heat exchange; Because the process that steam rises in regenerator progressively is condensed, the vapor phase that the gas of arrival chill zone 20-2 carries is to less, the rich solution of part low temperature can reduce its temperature rapidly, this will reduce the regenerator outlet temperature significantly, promptly under the suitable situation of input heat, pass through chill zone, kept a higher temperature in the renewing zone, and chill zone is kept a lower temperature, thereby reduce the load of regeneration gas cooler, reduce the consumption of system's heat loss and cooling water and the pump merit that reduces cooling water.
In addition, the upper end of regenerator 20 is connected with regeneration gas separator 17, and the lower end is connected with lean pump, and regenerator spray thrower 14 links to each other with poor rich liquid heat exchanger 12, Quench spray thrower 15 with link to each other with rich solution pump 10.70%～95% lean solution heats up by poor rich liquid heat exchanger 12 heat exchange, enter regenerator after atomizing by regenerator spray thrower 14 then, and remaining lean solution directly enters regenerator 20 by Quench spray thrower 15, the gas that cooling is risen.
Heat-exchange system comprises: the regeneration gas piece-rate system, and it is made of regeneration gas cooler 17, regeneration gas separator 18 and backflow fluid infusion pump 19; And rich or poor liquid heat-exchange system, it is made of rich solution pump 10, lean pump 13, poor rich liquid heat exchanger 12 and lean solution cooler 11.
Because the existence of chill zone, backflow fluid infusion pump 19 can not return regenerator 20 with the low-concentration liquid of condensation separation, and directly with lean solution cooler 11 after liquid mixed mutually, not only reduced the heat loss of regenerator, can also directly reduce the lean solution temperature, thereby part reduces the thermic load of lean solution cooler.
In addition, in absorption tower and regenerator, because poor/carbon dioxide enriched absorption liquid all adopts the spray atomizing, so strengthened the heat and mass reaction, simplified tower internals, reducing tower body cost of investment atomizing object is pure liquid solution, and atomizer is simple.So, overcome in the conventional art, adopted reinforcement mass transfer technology such as stuffing box column plate, it is big to run into tower body in super-huge system, internals complexity and liquid maldistribution, problems such as investment height.
In absorption tower 5 and regenerator 20, preferably adopt a plurality of nozzles evenly to arrange along tower section, so will be evenly distributed in the tower behind the solution atomization, and in dropping process, finish heat transfer, mass transfer and chemical reaction.In addition, between absorption tower spray thrower 6 and the self-loopa spray thrower 4 and regenerator spray thrower 14 and Quench spray thrower 15 between the nozzle arrangement mode preferably carry out complementation, to reduce the gas short circuit in the tower.
Be appreciated that absorption tower 5 described above can be applied to separately in the flue gas carbon dioxide capture equipment of other frameworks.Regenerator 20 described above also can be applied to separately in the flue gas carbon dioxide capture equipment of other frameworks.
Concrete operation method to flue gas carbon dioxide capture equipment of the present utility model is described below.
At first the absorption liquid for preparing is injected in the absorption tower, starts rich solution pump 10 then, solution is pumped in the regenerator 20, after absorption tower and regenerator liquid level reach setting value, start lean pump 13, set up the balance of system's liquid phase circulation; In regenerative system, progressively add low-pressure steam, open poor rich liquid heat exchanger 12, lean solution cooler 11, regeneration gas cooler 17 starts backflow fluid infusion pump 19 when regeneration gas separator 18 liquid levels reach setting value by the time.After balance was set up, at first ON cycle washing pump 7 was opened blower fan 2 then, and flue gas is incorporated into the carbon system of catching.
, under the effect of blower fan 2, enter in the absorption tower 5 by pretreated flue gas from rich solution groove 1 liquid level top; The flue gas that enters the absorption tower axially rises along the absorption tower, successively passes through by semi lean solution uptake zone 5-1 lean solution uptake zone 5-2.Atomized drop in the latter space is formed by 6 atomizings of absorption tower spray thrower, has higher solution concentration, so to CO
2Absorbability is stronger, and the CO in should the interval gas phase
2Be absorbed in semi lean solution uptake zone 5-1, concentration is relatively low; Liquid phase among the semi lean solution district 5-1 is by having absorbed portion C O through lean solution uptake zone 5-2
2Atomized drop and extract and the drop of atomizing is formed from rich solution groove 1 by self-circulation system, in this zone, the concentration of absorbent is relatively low in the drop, but CO in the gas phase
2Concentration higher relatively.
,, directly be discharged in the atmosphere or turn back to flue system after spraying cooling and the demist through circulation water wash system 7,8 and demister 9 through the gas after the decarburization.
Absorbed CO
2Rich solution under the effect of rich solution pump 10, enter regenerative system in two sub-sections.At first, main portions improves temperature (end difference minimum controllable system is to about 5 ℃), by entering renewing zone 20-1 after 14 atomizings of regenerator spray thrower by poor rich liquid heat exchanger 12.Another part rich solution then no longer passes through poor rich liquid heat exchanger 12, directly by entering into regenerator chill zone 20-2 after 15 atomizings of Quench spray thrower.
Because this zone atomized drop temperature is lower, and the water vapour in the gas phase is less relatively, so the regenerator outlet temperature can be reduced rapidly.After rich solution drop after process heats up passes chill zone, enter into renewing zone 20-1.On the other hand, in the lean solution groove, low-pressure steam boils solution, and the steam after the gasification carries out heat transfer effect with the drop that falls in the 20-1 of renewing zone, improved the drop temperature.When the drop temperature reaches CO
2After absorbent back reaction occurrence temperature, CO
2Just desorb from drop, the water vapour in the gas phase then is condensed into droplets fall, gets back to the lean solution groove.For making the atomizing effect adjustment flexible, can before regenerator spray thrower 14 and Quench spray thrower 15, increase a pump or a cover controlled valve adjusting device.
By being mainly CO in the gas after the Quench
2And water vapour, and the drop that is partly carried by gas.After their process regeneration gas cooler 17 condensations, enter into regeneration gas separator 18.Regeneration gas separator 17 is with drop and CO
2Gas separates, and has obtained the CO of low temperature and high concentration
2The solution of gas and low-temperature and low-concentration.These solution are through phegma fluid infusion pumps 19, join constantly in the lean solution behind the lean solution cooler 11, to reduce the temperature of lean solution.
By the solution after the regeneration, through lean pump 13, in poor rich liquid heat exchanger 12, carry out the heat exchange cooling with rich solution after, further lower the temperature through the lean solution cooler again, at last by entering into lean solution uptake zone 5-2 after 6 atomizings of absorption tower spray thrower.In order to control atomizing effect, can before absorption tower spray thrower 6, increase an atomizer pump or a cover controlled valve adjusting device.
Flue gas carbon dioxide capture method according to the utility model equipment is described below.In the utility model, flue gas carbon dioxide capture method may further comprise the steps: A) in absorption tower 5, utilize the carbon dioxide in the poor carbon dioxide absorption liquid absorption flue gas, to form carbon dioxide enriched absorption liquid; B) in regenerator 20, the carbon dioxide in the carbon dioxide enriched absorption liquid of desorb is with the poor carbon dioxide absorption liquid that forms the carbon dioxide regeneration gas and recycle for absorption system; And C) in heat-exchange system, make carbon dioxide enriched absorption liquid and poor carbon dioxide absorption liquid and/the carbon dioxide regeneration gas carries out heat exchange.Concrete characteristics to each step of the present utility model are described below.
In steps A, 5 bottoms enter into absorption tower 5 from the absorption tower by blower fan 2 can to make the pretreated flue gas of process, and allow the carbon dioxide enriched absorption liquid of atomizing absorb earlier, allow the poor carbon dioxide absorption liquid of atomizing absorb again, wherein, in the rich solution groove 1 of carbon dioxide enriched absorption liquid from 5 bottoms, absorption tower.
In step B, the Quench spray thrower 15 that can make the part of the carbon dioxide enriched absorption liquid in the rich solution groove 1 on absorption tower 5 offer regenerator 20 makes its atomizing, and the rich solution spray thrower 14 that another part offers Quench spray thrower 15 belows after by cooling makes its atomizing.
In step C, the poor carbon dioxide absorption liquid in the lean solution groove 21 of regenerator 20 is mixed mutually via the liquid that cools off and vapor-liquid separation obtains with the carbon dioxide regeneration gas via heat-exchange system cooling back.
Flue gas carbon dioxide capture method to preferred embodiment equipment of the present utility model is elaborated below.
Will be through pretreated flue gas, 5 middle and lower parts enter into the absorption tower from the absorption tower by blower fan 2, and rise in the absorption tower; On the other hand, absorption liquid is atomized by absorption tower spray thrower 6.The flue gas that rises carries out mass transfer and chemical reaction with the drop that atomizing descends, thereby with the CO in the flue gas
2Trap in the solution; Self-circulating pump 3 links to each other with rich solution groove 1, enters into the absorption tower after the solution in the rich solution groove is atomized by self-loopa spray thrower 4, absorbs CO once more
2, and the CO in the raising solution
2Concentration (CO
2Stressor).
Absorbed CO
2Rich solution, enter into regenerative system by the rich solution pump; Wherein a part after the raising temperature, enters into regenerator by 14 atomizings of regenerator spray thrower by poor rich liquid heat exchanger 12, and the lean solution in the lean solution groove is by low-pressure steam heating evaporation, CO
2From absorbent, decompose to come out steam and CO that evaporation is risen
2Contact with the drop of atomizing, by heat and mass transfer process, drop added ratio of specific heat and from solution with CO
2Desorb; Another part rich solution is not then by heat exchanger, directly by entering into regenerator after 15 atomizings of Quench spray thrower.
The steam that rises in the regenerator only has part by the regenerator spray thrower, and condensation becomes drop all the other heat drop in uphill process after.The solution of the lower temperature of Quench spray thrower 15 atomizing rapidly with these steam condensations coolings, thereby reduces the temperature that regenerator exports with after these small part gases contacts, thus the load of reduction regeneration gas cooler 17.
Cooled steam and CO
2Be reproduced gas cooler 17 and further condense to 25～40 ℃, the solution of the low concentration that condenses carries out gas-liquid separation by regeneration gas separator 18.Wherein gas is discharged from the top outlet, becomes the high concentration CO of recovery
2Gas.And the liquid part then by backflow fluid infusion pump 19, is mixed into the absorption tower with lean solution behind the lean solution cooler 11, to reduce the lean solution temperature, reduces lean solution cooler 11 loads.
CO is crossed in desorb
2Solution, through lean pump 13, carry out the heat exchange cooling at the rich solution of poor rich liquid heat exchanger 12 and low temperature,, enter the absorption tower by absorption tower spray thrower 6 and carry out CO further after the cooling through lean solution cooler 11 again
2Capture.
By above description as can be seen, in the utility model, absorption tower and regenerator all adopt spray process, and have increased circulation in the cover spray in the absorption tower, increased by a cover spray Quench system in regenerator, condensate liquid directly mixes with the lean solution behind the cooler behind the regenerator.The utility model has the advantages that: on the one hand, can carry out heat to system effectively distributes, reduce rich or poor liquid circulation rate, reduce and lean solution behind the poor rich liquid heat exchanger and, thereby reduce the cooling water load, reduce system energy consumption and power consumption through the temperature of fluid behind the regeneration gas condenser; On the other hand, reduce expensive system's internals, reduced the absorption tower height, thereby reduced the cost of system.
Be preferred embodiment of the present utility model only below, be not limited to the utility model, for a person skilled in the art, the utility model can have various changes and variation.All within spirit of the present utility model and principle, any modification of being done, be equal to replacement, improvement etc., all should be included within the protection domain of the present utility model.
Claims (9)
1. flue gas carbon dioxide capture equipment comprises:
Absorption system utilizes the carbon dioxide in the poor carbon dioxide absorption liquid absorption flue gas, to form carbon dioxide enriched absorption liquid;
Regenerative system is used for the carbon dioxide of the described carbon dioxide enriched absorption liquid of desorb, with the poor carbon dioxide absorption liquid that forms the carbon dioxide regeneration gas and recycle for described absorption system; And
Heat-exchange system, for described carbon dioxide enriched absorption liquid and described poor carbon dioxide absorption liquid and/described carbon dioxide regeneration gas between heat exchange, it is characterized in that,
Described regenerative system comprises regenerator (20), and its underpart has the Quench spray thrower (15) that lean solution groove (21), top have rich solution spray thrower (14) and be provided with above described rich solution spray thrower,
Wherein, space on the liquid level of the poor carbon dioxide absorption liquid of described lean solution groove (21), under described rich solution spray thrower (14) forms renewing zone (20-1), the space formation chill zone (20-2) between described Quench spray thrower (14) and the described rich solution spray thrower (14).
2. flue gas carbon dioxide capture equipment according to claim 1 is characterized in that,
Supply with described rich solution spray thrower (14) after the described heat-exchange system heat exchange of 70%～95% process of the carbon dioxide enriched absorption liquid that described regenerative system provides, remaining directly supplies with described Quench spray thrower (15).
3. flue gas carbon dioxide capture equipment according to claim 2 is characterized in that,
The upper end of described regenerator (20) is provided with demister, described rich solution spray thrower (14) is arranged on 2/3～4/5 between described lean solution groove (21) liquid level and the demister (16) and highly locates, and described Quench spray thrower (15) is arranged between described rich solution spray thrower (14) and the demister (16).
4. flue gas carbon dioxide capture equipment according to claim 2 is characterized in that,
Described regenerative system also comprises regeneration gas cooler (17) and the regeneration gas separator (18) that is connected to described regenerator (16),
Wherein, described regeneration gas separator (18) separates the liquid obtain and mixes with the cooled poor carbon dioxide absorption liquid phase of described lean solution cooler (11).
5. flue gas carbon dioxide capture equipment according to claim 1 is characterized in that,
Described heat-exchange system comprises:
Poor rich liquid heat exchanger (12); And
Lean solution cooler (11),
Wherein, the poor carbon dioxide absorption liquid in the lean solution groove (21) of described regenerator (20) is supplied with the lean solution spray thrower (6) on described absorption tower (5) through described lean solution cooler (11) cooling back.
6. flue gas carbon dioxide capture equipment according to claim 1 is characterized in that,
The upper end of described regenerator (20) is provided with demister (16), described rich solution spray thrower (14) is arranged on 2/3～4/5 between described lean solution groove (21) liquid level and the demister (16) and highly locates, and described Quench spray thrower (15) is arranged between described rich solution spray thrower (14) and the demister (16).
7. flue gas carbon dioxide capture equipment according to claim 1 is characterized in that,
Described absorption system comprises at least one absorption tower (5) that is connected with blower fan (2), the bottom on described absorption tower (5) has that rich solution groove (1), middle part have self-loopa spray thrower (4), top has lean solution spray thrower (6), described self-loopa spray thrower (4) is arranged on 1/3～2/3 between described rich solution groove (1) liquid level and the lean solution spray thrower (6) and highly locates
Wherein, constitute lean solution uptake zone (5-2) between described self-loopa spray thrower (4) and the lean solution spray thrower (6), form semi lean solution uptake zone (5-1) between described self-loopa spray thrower (4) and the rich solution groove (1),
The top of the lean solution spray thrower (6) on described absorption tower (5) also has circulation cleaning system and demister (9).
8. a flue gas carbon dioxide capture equipment regenerator is characterized in that,
Evaporimeter, the top that the bottom of described regenerator (20) has lean solution groove (21) and is arranged in described lean solution groove (21) has rich solution spray thrower (14) and also is provided with Quench spray thrower (15) in described rich solution spray thrower (14) top,
Wherein, space on the liquid level of the poor carbon dioxide absorption liquid of described lean solution groove (21), under described rich solution spray thrower (14) forms renewing zone (20-1), the space formation chill zone (20-2) between described Quench spray thrower (14) and the described rich solution spray thrower (14).
9. flue gas carbon dioxide capture equipment regenerator according to claim 8 is characterized in that,
The upper end of described regenerator (20) is provided with demister, described rich solution spray thrower (14) is arranged on 2/3～4/5 between described lean solution groove (21) liquid level and the demister (16) and highly locates, and described Quench spray thrower (15) is arranged between described rich solution spray thrower (14) and the demister (16).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202777885U CN201558659U (en) | 2009-12-14 | 2009-12-14 | Flue gas carbon dioxide capture device and regenerator thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202777885U CN201558659U (en) | 2009-12-14 | 2009-12-14 | Flue gas carbon dioxide capture device and regenerator thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201558659U true CN201558659U (en) | 2010-08-25 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102078745B (en) * | 2009-12-01 | 2013-08-21 | 华能集团技术创新中心 | Smoke decarbonizing system and method and regeneration column for smoke decarbonizing system |
| CN104160268A (en) * | 2012-03-09 | 2014-11-19 | 三菱重工业株式会社 | Degradation product-concentration measurement device, and acidic gas removal device |
| CN111672280A (en) * | 2020-05-20 | 2020-09-18 | 西安交通大学 | Solar-driven carbon dioxide capturing tower and operation method thereof |
-
2009
- 2009-12-14 CN CN2009202777885U patent/CN201558659U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102078745B (en) * | 2009-12-01 | 2013-08-21 | 华能集团技术创新中心 | Smoke decarbonizing system and method and regeneration column for smoke decarbonizing system |
| CN104160268A (en) * | 2012-03-09 | 2014-11-19 | 三菱重工业株式会社 | Degradation product-concentration measurement device, and acidic gas removal device |
| US9782720B2 (en) | 2012-03-09 | 2017-10-10 | Mitsubishi Heavy Industries, Ltd. | Degradant concentration measurement device and acidic gas removal device |
| CN111672280A (en) * | 2020-05-20 | 2020-09-18 | 西安交通大学 | Solar-driven carbon dioxide capturing tower and operation method thereof |
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Assignee: China Huaneng Group Clean Energy Technology Research Institute Co., Ltd. Assignor: Huaneng Group Technology Innovation Center Contract record no.: 2011990000326 Denomination of utility model: Flue gas carbon dioxide capture device and regenerator thereof Granted publication date: 20100825 License type: Exclusive License Record date: 20110503 |
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