CN204799090U - Flue gas carbon dioxide entrapment recovery system - Google Patents

Abstract

The utility model provides a flue gas carbon dioxide entrapment recovery system, it includes: residual heat from flue gas heat exchanger, absorption tower, rich solution pump, absorption tower interstage circulating pump, absorption tower interstage circulation heat exchanger, the rich or poor liquid heat exchanger of one -level, rich solution shunt, the rich or poor liquid heat exchanger of second grade, desorber, boil vapor compressor at the bottom of ware, flash tank, the desorber, lean solution pump, desorber interstage circulation heat exchanger and lean solution cooler. In the basis flue gas carbon dioxide entrapment recovery system in, experienced seven heat exchanges to can improve flue gas carbon dioxide entrapment recovery system's energy utilization, to the thermal demand of outside general facilities when reducing the desorption.

Description

Smoke carbon dioxide capture recovery system

Technical field

The utility model relates to collecting carbonic anhydride and reclaims field, particularly relates to a kind of smoke carbon dioxide capture recovery system.

Background technology

Carbon dioxide is one of main component of the greenhouse gases causing global warming, reaches 55% to the contribution of greenhouse effects.Coal-burning power plant is then the maximum industry of discharge carbon dioxide.Carbon dioxide, except the impact causing global warming, can also do industrial chemicals, also the carbon dioxide after trapping, purifying can be injected oil reservoir to improve tar productivity with supercriticality.Can predict, the continuous expansion with range of application is improved in the development along with trapping technique, and carbon dioxide improves Development Response of Oilfield by becoming China, improves the valuable source of oil recovery factor.

Current collecting carbonic anhydride purifying process is still main based on absorption tower and desorber, uses alkanolamine solution to make absorbent.Through chemical absorbing and desorb, obtain highly purified carbon dioxide.In process, main energy consumption is desorb tower bottom reboiler, uses steam heating rich solution with Desorption of Carbon Dioxide.In absorption and desorption process, many places energy is underutilized, and causes capacity usage ratio low.

Utility model content

In view of Problems existing in background technology, the purpose of this utility model is to provide a kind of smoke carbon dioxide capture recovery system, and it can improve the capacity usage ratio of smoke carbon dioxide capture recovery system, the demand to outside utility heat during reduction desorb.

To achieve these goals, the utility model provides a kind of smoke carbon dioxide capture recovery system, and it comprises: vapour compression machine, lean pump, desorber inter-stage circulation heat exchanger and lean solution cooler at the bottom of flue gas waste heat recovery heat exchanger, absorption tower, rich solution pump, absorption tower inter-stage circulating pump, absorption tower inter-stage circulation heat exchanger, one-level poor rich liquid heat exchanger, rich solution current divider, secondary poor rich liquid heat exchanger, desorber, boiling device, flash tank, desorber.

Absorption tower has: absorption tower tower body, is formed with the absorbing tower chamber holding absorbent in advance; First absorption tower entrance, is arranged at the bottom of absorption tower tower body and is communicated in absorbing tower chamber and is communicated in flue gas waste heat recovery heat exchanger; First absorption tower outlet, is arranged at the top of absorption tower tower body and is communicated in absorbing tower chamber; Second absorption tower entrance, is arranged at the top of absorption tower tower body and is communicated in absorbing tower chamber; Second absorption tower exports, and is arranged at the bottom of absorption tower tower body and is communicated in absorbing tower chamber; 3rd absorption tower entrance, be arranged at absorption tower tower body bottom and be positioned at the first absorption tower entrance below and be positioned at second absorption tower outlet top; And the 3rd absorption tower outlet, be arranged at absorption tower tower body bottom and between the first absorption tower entrance and the 3rd absorption tower entrance.Rich solution pump side is communicated in the second absorption tower outlet on absorption tower.Absorption tower inter-stage circulating pump, side is communicated in the 3rd absorption tower entrance on absorption tower.Absorption tower inter-stage circulation heat exchanger has: the first absorption tower inter-stage circulation heat exchanger entrance, is communicated in the opposite side of rich solution pump; First absorption tower inter-stage circulation heat exchanger outlet, is communicated in flue gas waste heat recovery heat exchanger; Second absorption tower inter-stage circulation heat exchanger entrance, is communicated in the 3rd absorption tower outlet on absorption tower; And the outlet of second absorption tower inter-stage circulation heat exchanger, be communicated in the opposite side of absorption tower inter-stage circulating pump.One-level poor rich liquid heat exchanger has: the first one-level poor rich liquid heat exchanger entrance, is communicated in flue gas waste heat recovery heat exchanger; First one-level poor rich liquid heat exchanger outlet; Second one-level poor rich liquid heat exchanger entrance; And second one-level poor rich liquid heat exchanger outlet.Rich solution current divider has: rich solution splitter inlet, is communicated in the first one-level poor rich liquid heat exchanger outlet of one-level poor rich liquid heat exchanger; First rich solution current divider outlet; And second rich solution current divider outlet.Secondary poor rich liquid heat exchanger has: the first secondary poor rich liquid heat exchanger entrance, is communicated in the second rich solution current divider outlet of rich solution current divider; First secondary poor rich liquid heat exchanger outlet; Second secondary poor rich liquid heat exchanger entrance; And second secondary poor rich liquid heat exchanger outlet, be communicated in the second one-level poor rich liquid heat exchanger entrance of one-level poor rich liquid heat exchanger.Desorber has: desorber tower body, is formed with desorber tower chamber; First desorber entrance, be arranged at desorber tower body and be communicated in desorber tower chamber and be communicated in rich solution current divider first rich solution current divider outlet; Second desorber entrance, be arranged at desorber tower body and be communicated in desorber tower chamber and be communicated in rich solution current divider second rich solution current divider outlet; 3rd desorber entrance, is arranged at the bottom of desorber tower body and is positioned at the below of the second desorber entrance and is communicated in desorber tower chamber; 4th desorber entrance, is arranged at the bottom of desorber tower body and is positioned at the below of the 3rd desorber entrance and is communicated in desorber tower chamber; 5th desorber entrance, is arranged at the bottom of desorber tower body and is communicated in desorber tower chamber; First desorber outlet, is arranged at the top of desorber tower body and is communicated in desorber tower chamber; Second desorber outlet, is arranged at the bottom of desorber tower body and is positioned at the below of the 4th desorber entrance and the 5th desorber entrance and is communicated in desorber tower chamber; And the 3rd desorber outlet, be arranged at the bottom of desorber tower body and be communicated in desorber tower chamber between the second desorber entrance and the 3rd desorber entrance.Boiling device can produce water vapour and have: boiling device entrance, is communicated in the second desorber outlet of desorber; First boiling device outlet, is communicated in the 5th desorber entrance of desorber; Second boiling device outlet, is communicated in boiling device entrance.Flash tank has: flash tank tank body; Flash tank entrance, be arranged at flash tank tank body and be communicated in boiling device second boiling device outlet; First flash tank outlet, is arranged at the top of flash tank tank body; And second flash tank outlet, be arranged at the bottom of flash tank tank body.Vapour compression machine side at the bottom of desorber is communicated in the first flash tank outlet of flash tank and opposite side is communicated in the 4th desorber entrance of Analytic Tower.Lean pump side is communicated in the second flash tank outlet of flash tank.Desorber inter-stage circulation heat exchanger has: the first desorber inter-stage circulation heat exchanger entrance, is communicated in the opposite side of lean pump; First desorber inter-stage circulation heat exchanger outlet, is communicated in the second secondary poor rich liquid heat exchanger entrance of secondary poor rich liquid heat exchanger; Second desorber inter-stage circulation heat exchanger entrance, is communicated in the 3rd desorber outlet of desorber; And second desorber inter-stage circulation heat exchanger outlet, be communicated in the 3rd desorber entrance of desorber.Lean solution cooler side is communicated in the second one-level poor rich liquid heat exchanger outlet of one-level poor rich liquid heat exchanger and opposite side is communicated in the second absorption tower entrance on absorption tower.

Wherein, flowing through flue gas waste heat recovery heat exchanger containing hot flue gas with pressure and to enter in absorbing tower chamber via the first absorption tower entrance on absorption tower and move from the bottom up in absorbing tower chamber from outside, absorbent to enter in absorbing tower chamber from the second absorption tower entrance on absorption tower and down sprays in absorbing tower chamber, the absorbent down sprayed contacts with the flue gas adverse current moved from the bottom up, thus the absorbent down sprayed absorbs the carbon dioxide in flue gas, the absorbent absorbing carbon dioxide becomes rich solution and is gathered in absorbing tower chamber, and the flue gas being stripped of carbon dioxide is discharged from the first absorption tower outlet, the rich solution be gathered in absorbing tower chamber is discharged from second absorption tower outlet, pressurize via rich solution pump, absorption tower inter-stage circulation heat exchanger is entered via the first absorption tower inter-stage circulation heat exchanger entrance, and the rich solution in absorption tower is discharged via the 3rd absorption tower outlet and enters in the inter-stage circulation heat exchanger of absorption tower via second absorption tower inter-stage circulation heat exchanger entrance, thus since second absorption tower outlet rich solution and from the 3rd absorption tower outlet rich solution in the inter-stage circulation heat exchanger of absorption tower, carry out the first heat exchange, rich solution heat release thus from the 3rd absorption tower outlet is lowered the temperature and exports via second absorption tower inter-stage circulation heat exchanger afterwards, absorption tower inter-stage circulating pump and the 3rd absorption tower entrance are back in absorption tower, and heat up from the rich solution heat absorption of second absorption tower outlet, completing the rich solution after the first heat exchange escapes and enter in flue gas waste heat recovery heat exchanger via the first absorption tower inter-stage circulation heat exchanger outlet, to carry out the second heat exchange at flue gas waste heat recovery heat exchanger and the flue gas flowing through flue gas waste heat recovery heat exchanger, flue gas heat release is lowered the temperature, and rich solution heat absorption heats up, the rich solution completing the second heat exchange out, enters in one-level poor rich liquid heat exchanger via the first one-level poor rich liquid heat exchanger entrance afterwards, to carry out the 3rd heat exchange in one-level poor rich liquid heat exchanger from flue gas waste heat recovery heat exchanger, the rich solution completing the 3rd heat exchange enters in rich solution current divider via rich solution splitter inlet, to be split into two-way, one tunnel enters in the desorber tower chamber of desorber via the first rich solution current divider outlet and the first desorber entrance, another road enters in secondary poor rich liquid heat exchanger via the second rich solution current divider outlet and the first secondary poor rich liquid heat exchanger entrance, to carry out the 4th heat exchange in secondary poor rich liquid heat exchanger, the rich solution completing the 4th heat exchange enters in the desorber tower chamber of desorber via the first secondary poor rich liquid heat exchanger outlet and the second desorber entrance, rich solution from two-way is all collected in the desorber tower chamber of desorber, boiling device produces water vapour and enters in desorber tower chamber by water vapour via the first boiling device outlet and the 5th desorber entrance, water vapour carries out heating desorption to the rich solution be collected in desorber tower chamber, become lean solution after rich solution desorb and discharge carbon dioxide, cooling after desorb and the water vapour of condensation is mixed into lean solution, and be mixed into cooling and the lean solution sedimentation of the water vapour of condensation be collected in desorber tower chamber, the carbon dioxide discharged after desorb via first desorber outlet discharge, after desorb cooling but uncondensable water vapour with the carbon dioxide discharged after desorb together via first desorber outlet discharge, lean solution is discharged via the second desorber outlet, enter via boiling device entrance the water vapour produced with boiling device in boiling device carries out the 6th heat exchange, and lean solution heat absorption heats up, complete the lean solution after the 6th heat exchange to discharge via the second boiling device outlet, enter in flash tank tank body via flash tank entrance afterwards and carry out flash distillation, to flash off water vapour, the water vapour flashed off discharge via the first flash tank outlet and by after vapour compression machine pressurization at the bottom of desorber through entering in desorber tower chamber by the 4th desorber entrance, to carry out heating desorption with exporting via the first boiling device together with the water vapour that to enter into the 5th desorber entrance in desorber tower chamber of boiling device to the rich solution be collected in desorber tower chamber, lean solution after flash distillation process is discharged in flash tank tank body via the second flash tank outlet, pressurizeed by lean pump afterwards, enter in desorber inter-stage circulation heat exchanger via the first desorber inter-stage circulation heat exchanger entrance, and the lean solution in Analytic Tower enters in desorber inter-stage circulation heat exchanger via the 3rd desorber outlet, thus the 7th heat exchange is carried out from the lean solution of the 3rd desorber outlet with the lean solution exported from the second flash tank in desorber inter-stage circulation heat exchanger, lean solution heat absorption thus from the 3rd desorber outlet heats up, afterwards via the second desorber inter-stage circulation heat exchanger outlet, 3rd desorber entrance turns back in Analytic Tower, and lower the temperature from the lean solution heat release of the second flash tank outlet, the lean solution completing the 7th heat exchange is discharged via the first desorber inter-stage circulation heat exchanger outlet and enters in secondary poor rich liquid heat exchanger via the second secondary poor rich liquid heat exchanger entrance, thus in secondary poor rich liquid heat exchanger, enter the rich solution in secondary poor rich liquid heat exchanger via the first secondary poor rich liquid heat exchanger entrance and carry out described 4th heat exchange via the second secondary poor rich liquid heat exchanger entrance lean solution entered in secondary poor rich liquid heat exchanger, rich solution heat absorption heats up, and lean solution heat release is lowered the temperature, the lean solution completing the 4th heat exchange is discharged via the second secondary poor rich liquid heat exchanger outlet and enters in one-level poor rich liquid heat exchanger via the second one-level poor rich liquid heat exchanger entrance, thus in one-level poor rich liquid heat exchanger, enter the rich solution in one-level poor rich liquid heat exchanger via the first one-level poor rich liquid heat exchanger entrance and carry out described 3rd heat exchange via the second one-level poor rich liquid heat exchanger entrance lean solution entered in one-level poor rich liquid heat exchanger, rich solution heat absorption heats up, and lean solution heat release is lowered the temperature, the lean solution completing described 3rd heat exchange escapes and enter in lean solution cooler from one-level poor rich liquid heat exchanger, with cooled in lean solution cooler via the second one-level poor rich liquid heat exchanger outlet, cooled lean solution is discharged and is entered in desorber tower chamber via the second desorber entrance as absorbent in lean solution cooler, thus moves from the bottom up in absorbing tower chamber.

The beneficial effects of the utility model are as follows: according in smoke carbon dioxide capture recovery system described in the utility model, experienced by seven heat exchanges, thus the capacity usage ratio of smoke carbon dioxide capture recovery system can be improved, the demand to outside utility heat during reduction desorb.

Accompanying drawing explanation

Fig. 1 is the schematic diagram according to smoke carbon dioxide capture recovery system of the present utility model.

Wherein, description of reference numerals is as follows:

10 flue gas waste heat recovery heat exchangers

11 absorption towers

111 absorption tower tower bodies

1111 absorbing tower chambeies

112A first absorption tower entrance

112B first absorption tower exports

113A second absorption tower entrance

113B second absorption tower exports

114A the 3rd absorption tower entrance

114B the 3rd absorption tower exports

115 absorption tower silk screens

12 rich solution pumps

13 absorption tower inter-stage circulating pumps

14 absorption tower inter-stage circulation heat exchangers

141A first absorption tower inter-stage circulation heat exchanger entrance

The inter-stage circulation heat exchanger outlet of 141B first absorption tower

142A second absorption tower inter-stage circulation heat exchanger entrance

142B second absorption tower inter-stage circulation heat exchanger exports

15 one-level poor rich liquid heat exchangers

151A first one-level poor rich liquid heat exchanger entrance

151B first one-level poor rich liquid heat exchanger exports

152A second one-level poor rich liquid heat exchanger entrance

152B second one-level poor rich liquid heat exchanger exports

16 rich solution current dividers

161 rich solution splitter inlets

162 first rich solution current divider outlets

163 second rich solution current divider outlets

17 secondary poor rich liquid heat exchangers

171A first secondary poor rich liquid heat exchanger entrance

171B first secondary poor rich liquid heat exchanger exports

172A second secondary poor rich liquid heat exchanger entrance

172B second secondary poor rich liquid heat exchanger exports

18 desorbers

180 desorber silk screens

181 desorber tower bodies

1811 desorber tower chambeies

182A first desorber entrance

183A second desorber entrance

184A the 3rd desorber entrance

185A the 4th desorber entrance

186A the 5th desorber entrance

187A the 6th desorber entrance

188A the 7th desorber entrance

189A the 8th desorber entrance

182B first desorber exports

183B second desorber exports

184B the 3rd desorber exports

185B the 4th desorber exports

186B the 5th desorber exports

19 boiling devices

191 boiling device entrances

192 first boiling device outlets

193 second boiling device outlets

20 flash tanks

201 flash tank tank bodies

202 flash tank entrances

203 first flash tank outlets

204 second flash tank outlets

Vapour compression machine at the bottom of 21 desorbers

22 lean pumps

23 desorber inter-stage circulation heat exchangers

231A first desorber inter-stage circulation heat exchanger entrance

231B first desorber inter-stage circulation heat exchanger exports

232A second desorber inter-stage circulation heat exchanger entrance

232B second desorber inter-stage circulation heat exchanger exports

24 lean solution coolers

25 one-level vapour compression machines

26 second steam compressors

27 choke valves

28 water washing mechanisms

281 water scrubbers

2811 water scrubber tower bodies

2812A first water scrubber entrance

2812B first water scrubber exports

2813A second water scrubber entrance

2813B second water scrubber exports

2814 water scrubber filter screens

282 washing water circulating pumps

283 washing water water coolers

284 washing waters feed pipe

285 washing water blowoff valves

29 washing water pH controlling organizations

291 alkali grooves

292 alkali lye transfer pipelines

293 perform valve

294 online pH instrument

J connectivity points

295 flowmeters

30 corrugated plating separators

301 corrugated plating shell separators

3011 corrugated plating separator cavitys

302 corrugated platings

303 corrugated plating separator inlets

304 first wave card separator outlets

305 Second Wave card separator outlets

306 corrugated plating separator silk screens

307 self-draining valves

31 booster fans

32 washing mechanisms

321 scrubbing towers

3211 scrubbing tower tower bodies

3212A first washing tower inlet

3212B first scrubbing tower exports

3213A second washing tower inlet

3213B second scrubbing tower exports

322 cleaning solution surge tanks

323 washing pumps

324 delivery pipes

33 reclaim carbon dioxide treatment mechanism

331 desorber top heat exchangers

3311 desorber top heat exchanger silk screens

332 carbon dioxide coolers

333 desorber top gas liquid/gas separators

3331 desorber top gas liquid/gas separator silk screens

334 desorb tower top surge tanks

335 desorb tower top vapour compression machines

336 delivery pipes

337 compression units

3371 compressors

3372 water coolers

Detailed description of the invention

Describe in detail with reference to the accompanying drawings according to smoke carbon dioxide capture recovery system of the present utility model.

With reference to Fig. 1, comprise according to smoke carbon dioxide capture recovery system of the present utility model: vapour compression machine 21, lean pump 22, desorber inter-stage circulation heat exchanger 23 and lean solution cooler 24 at the bottom of flue gas waste heat recovery heat exchanger 10, absorption tower 11, rich solution pump 12, absorption tower inter-stage circulating pump 13, absorption tower inter-stage circulation heat exchanger 14, one-level poor rich liquid heat exchanger 15, rich solution current divider 16, secondary poor rich liquid heat exchanger 17, desorber 18, boiling device 19, flash tank 20, desorber.

Absorption tower 11 has: absorption tower tower body 111, is formed with the absorbing tower chamber 1111 holding absorbent in advance; First absorption tower entrance 112A, is arranged at the bottom of absorption tower tower body 111 and is communicated in absorbing tower chamber 1111 and is communicated in flue gas waste heat recovery heat exchanger 10; First absorption tower outlet 112B, is arranged at the top of absorption tower tower body 111 and is communicated in absorbing tower chamber 1111; Second absorption tower entrance 113A, is arranged at the top of absorption tower tower body 111 and is communicated in absorbing tower chamber 1111; Second absorption tower outlet 113B, is arranged at the bottom of absorption tower tower body 111 and is communicated in absorbing tower chamber 1111; 3rd absorption tower entrance 114A, is arranged at the bottom of absorption tower tower body 111 and is positioned at the below of the first absorption tower entrance 112A and is positioned at the top that second absorption tower exports 113B; And the 3rd absorption tower outlet 114B, be arranged at absorption tower tower body 111 bottom and between the first absorption tower entrance 112A and the 3rd absorption tower entrance 114A.

Rich solution pump 12 side is communicated in the second absorption tower outlet 113B on absorption tower 11.

Inter-stage circulating pump 13 side, absorption tower is communicated in the 3rd absorption tower entrance 114A on absorption tower 11.

Absorption tower inter-stage circulation heat exchanger 14 has: the first absorption tower inter-stage circulation heat exchanger entrance 141A, is communicated in the opposite side of rich solution pump 12; First absorption tower inter-stage circulation heat exchanger outlet 141B, is communicated in flue gas waste heat recovery heat exchanger 10; Second absorption tower inter-stage circulation heat exchanger entrance 142A, is communicated in the 3rd absorption tower outlet 114B on absorption tower 11; And second absorption tower inter-stage circulation heat exchanger outlet 142B, be communicated in the opposite side of absorption tower inter-stage circulating pump 13.

One-level poor rich liquid heat exchanger 15 has: the first one-level poor rich liquid heat exchanger entrance 151A, is communicated in flue gas waste heat recovery heat exchanger 10; First one-level poor rich liquid heat exchanger outlet 151B; Second one-level poor rich liquid heat exchanger entrance 152A; And second one-level poor rich liquid heat exchanger outlet 152B.

Rich solution current divider 16 has: rich solution splitter inlet 161, is communicated in the first one-level poor rich liquid heat exchanger outlet 151B of one-level poor rich liquid heat exchanger 15; First rich solution current divider outlet 162; And second rich solution current divider outlet 163.

Secondary poor rich liquid heat exchanger 17 has: the first secondary poor rich liquid heat exchanger entrance 171A, is communicated in the second rich solution current divider outlet 163 of rich solution current divider 16; First secondary poor rich liquid heat exchanger outlet 171B; Second secondary poor rich liquid heat exchanger entrance 172A; And second secondary poor rich liquid heat exchanger outlet 172B, be communicated in the second one-level poor rich liquid heat exchanger entrance 152A of one-level poor rich liquid heat exchanger 15.

Desorber 18 has: desorber tower body 181, is formed with desorber tower chamber 1811; First desorber entrance 182A, be arranged at desorber tower body 181 and be communicated in desorber tower chamber 1811 and be communicated in rich solution current divider 16 first rich solution current divider outlet 162; Second desorber entrance 183A, be arranged at desorber tower body 181 and be communicated in desorber tower chamber 1811 and be communicated in rich solution current divider 16 second rich solution current divider outlet 163; 3rd desorber entrance 184A, is arranged at the bottom of desorber tower body 181 and is positioned at the below of the second desorber entrance 183A and is communicated in desorber tower chamber 1811; 4th desorber entrance 185A, is arranged at the bottom of desorber tower body 181 and is positioned at the below of the 3rd desorber entrance 184A and is communicated in desorber tower chamber 1811; 5th desorber entrance 186A, is arranged at the bottom of desorber tower body 181 and is communicated in desorber tower chamber 1811; First desorber outlet 182B, is arranged at the top of desorber tower body 181 and is communicated in desorber tower chamber 1811; Second desorber outlet 183B, is arranged at the bottom of desorber tower body 181 and is positioned at the below of the 4th desorber entrance 185A and the 5th desorber entrance 186A and is communicated in desorber tower chamber 1811; And the 3rd desorber outlet 184B, be arranged at the bottom of desorber tower body 181 and be communicated in desorber tower chamber 1811 between the second desorber entrance 183A and the 3rd desorber entrance 184A.

Boiling device 19 can produce water vapour and have: boiling device entrance 191, is communicated in the second desorber outlet 183B of desorber 18; First boiling device outlet 192, is communicated in the 5th desorber entrance 186A of desorber 18; Second boiling device outlet 193, is communicated in boiling device entrance 191.

Flash tank 20 has: flash tank tank body 201; Flash tank entrance 202, be arranged at flash tank tank body 201 and be communicated in boiling device 19 second boiling device outlet 193; First flash tank outlet 203, is arranged at the top of flash tank tank body 201; And second flash tank outlet 204, be arranged at the bottom of flash tank tank body 201.

Vapour compression machine 21 side at the bottom of desorber is communicated in the first flash tank outlet 203 of flash tank 20 and opposite side is communicated in the 4th desorber entrance 185A of Analytic Tower 18.

Lean pump 22 side is communicated in the second flash tank outlet 204 of flash tank 20.

Desorber inter-stage circulation heat exchanger 23 has: the first desorber inter-stage circulation heat exchanger entrance 231A, is communicated in the opposite side of lean pump 22; First desorber inter-stage circulation heat exchanger outlet 231B, is communicated in the second secondary poor rich liquid heat exchanger entrance 172A of secondary poor rich liquid heat exchanger 17; Second desorber inter-stage circulation heat exchanger entrance 232A, is communicated in the 3rd desorber outlet 184B of desorber 18; And second desorber inter-stage circulation heat exchanger outlet 232B, be communicated in the 3rd desorber entrance 184A of desorber 18.

Lean solution cooler 24 side is communicated in the second one-level poor rich liquid heat exchanger outlet 152B of one-level poor rich liquid heat exchanger 15 and opposite side is communicated in the second absorption tower entrance 113A on absorption tower 11.

Wherein, flowing through flue gas waste heat recovery heat exchanger 10 containing hot flue gas with pressure and to enter in absorbing tower chamber 1111 via the first absorption tower entrance 112A on absorption tower 11 and move from the bottom up in absorbing tower chamber 1111 from outside, absorbent to enter in absorbing tower chamber 1111 from the second absorption tower entrance 113A on absorption tower 11 and down sprays in absorbing tower chamber 1111, the absorbent down sprayed contacts with the flue gas adverse current moved from the bottom up, thus the absorbent down sprayed absorbs the carbon dioxide in flue gas, the absorbent absorbing carbon dioxide becomes rich solution and is gathered in absorbing tower chamber 1111, and the flue gas being stripped of carbon dioxide is discharged from the first absorption tower outlet 112B, the rich solution be gathered in absorbing tower chamber 1111 is discharged from second absorption tower outlet 113B, pressurize via rich solution pump 12, absorption tower inter-stage circulation heat exchanger 14 is entered via the first absorption tower inter-stage circulation heat exchanger entrance 141A, and the rich solution in absorption tower 11 is discharged via the 3rd absorption tower outlet 114B and enters in absorption tower inter-stage circulation heat exchanger 14 via second absorption tower inter-stage circulation heat exchanger entrance 142A, thus export the rich solution of 113B since second absorption tower and in absorption tower inter-stage circulation heat exchanger 14, carry out the first heat exchange from the rich solution of the 3rd absorption tower outlet 114B, rich solution heat release thus from the 3rd absorption tower outlet 114B is lowered the temperature and exports 142B via second absorption tower inter-stage circulation heat exchanger afterwards, absorption tower inter-stage circulating pump 13 and the 3rd absorption tower entrance 114A are back in absorption tower 11, and heat up from the rich solution heat absorption of second absorption tower outlet 113B, completing the rich solution after the first heat exchange escapes and enter in flue gas waste heat recovery heat exchanger 10 via the first absorption tower inter-stage circulation heat exchanger outlet 141B, to carry out the second heat exchange at flue gas waste heat recovery heat exchanger 10 and the flue gas flowing through flue gas waste heat recovery heat exchanger 10, flue gas heat release is lowered the temperature, and rich solution heat absorption heats up, the rich solution completing the second heat exchange out, enters in one-level poor rich liquid heat exchanger 15, to carry out the 3rd heat exchange in one-level poor rich liquid heat exchanger 15 via the first one-level poor rich liquid heat exchanger entrance 151A afterwards from flue gas waste heat recovery heat exchanger 10, the rich solution completing the 3rd heat exchange enters in rich solution current divider 16 via rich solution splitter inlet 161, to be split into two-way, one tunnel enters in the desorber tower chamber 1811 of desorber 18 via the first rich solution current divider outlet 162 and the first desorber entrance 182A, another road enters in secondary poor rich liquid heat exchanger 17 via the second rich solution current divider outlet 163 and the first secondary poor rich liquid heat exchanger entrance 171A, to carry out the 4th heat exchange in secondary poor rich liquid heat exchanger 17, the rich solution completing the 4th heat exchange enters in the desorber tower chamber 1811 of desorber 18 via the first secondary poor rich liquid heat exchanger outlet 171B and the second desorber entrance 183A, rich solution from two-way is all collected in the desorber tower chamber 1811 of desorber 18, boiling device 19 produces water vapour and enters in desorber tower chamber 1811 by water vapour via the first boiling device outlet 192 and the 5th desorber entrance 186A, water vapour carries out heating desorption to the rich solution be collected in desorber tower chamber 1811, become lean solution after rich solution desorb and discharge carbon dioxide, cooling after desorb and the water vapour of condensation is mixed into lean solution, and be mixed into cooling and the lean solution sedimentation of the water vapour of condensation be collected in desorber tower chamber 1811, the carbon dioxide discharged after desorb via first desorber outlet 182B discharge, after desorb cooling but uncondensable water vapour with the carbon dioxide discharged after desorb together via first desorber outlet 182B discharge, lean solution is discharged via the second desorber outlet 183B, enter the water vapour produced with boiling device 19 in boiling device 19 via boiling device entrance 191 carries out the 6th heat exchange, and lean solution heat absorption heats up, complete the lean solution after the 6th heat exchange to discharge via the second boiling device outlet 193, enter in flash tank tank body 201 via flash tank entrance 202 afterwards and carry out flash distillation, to flash off water vapour, the water vapour flashed off is discharged via the first flash tank outlet 203 and is entered in desorber tower chamber 1811 by warp after vapour compression machine at the bottom of desorber 21 pressurization by the 4th desorber entrance 185A, to carry out heating desorption with exporting via the first boiling device together with 192 water vapours entering in desorber tower chamber 1811 with the 5th desorber entrance 186A of boiling device 19 to the rich solution be collected in desorber tower chamber 1811, lean solution after flash distillation process is discharged in flash tank tank body 201 via the second flash tank outlet 204, pressurizeed by lean pump 22 afterwards, enter in desorber inter-stage circulation heat exchanger 23 via the first desorber inter-stage circulation heat exchanger entrance 231A, and the lean solution in Analytic Tower 18 enters in desorber inter-stage circulation heat exchanger 23 via the 3rd desorber outlet 184B, thus the 7th heat exchange is carried out from the lean solution of the 3rd desorber outlet 184B with the lean solution exporting 204 from the second flash tank in desorber inter-stage circulation heat exchanger 23, lean solution heat absorption thus from the 3rd desorber outlet 184B heats up, afterwards via the second desorber inter-stage circulation heat exchanger outlet 232B, 3rd desorber entrance 184A turns back in Analytic Tower 18, and lower the temperature from the lean solution heat release of the second flash tank outlet 204, the lean solution completing the 7th heat exchange is discharged via the first desorber inter-stage circulation heat exchanger outlet 231B and enters in secondary poor rich liquid heat exchanger 17 via the second secondary poor rich liquid heat exchanger entrance 172A, thus in secondary poor rich liquid heat exchanger 17, enter the rich solution in secondary poor rich liquid heat exchanger 17 via the first secondary poor rich liquid heat exchanger entrance 171A and carry out described 4th heat exchange via the second secondary poor rich liquid heat exchanger entrance 172A lean solution entered in secondary poor rich liquid heat exchanger 17, rich solution heat absorption heats up, and lean solution heat release is lowered the temperature, the lean solution completing the 4th heat exchange is discharged via the second secondary poor rich liquid heat exchanger outlet 172B and enters in one-level poor rich liquid heat exchanger 15 via the second one-level poor rich liquid heat exchanger entrance 152A, thus in one-level poor rich liquid heat exchanger 15, enter the rich solution in one-level poor rich liquid heat exchanger 15 via the first one-level poor rich liquid heat exchanger entrance 151A and carry out described 3rd heat exchange via the second one-level poor rich liquid heat exchanger entrance 152A lean solution entered in one-level poor rich liquid heat exchanger 15, rich solution heat absorption heats up, and lean solution heat release is lowered the temperature, the lean solution completing described 3rd heat exchange escapes and enter in lean solution cooler 24 from one-level poor rich liquid heat exchanger 15, with cooled in lean solution cooler 24 via the second one-level poor rich liquid heat exchanger outlet 152B, cooled lean solution is discharged and is entered in desorber tower chamber 1811 via the second desorber entrance 183A as absorbent in lean solution cooler 24, thus moves from the bottom up in absorbing tower chamber 1111.

According in smoke carbon dioxide capture recovery system described in the utility model, experienced by seven heat exchanges, thus the capacity usage ratio of smoke carbon dioxide capture recovery system can be improved, the demand to outside utility heat during reduction desorb.

According in smoke carbon dioxide capture recovery system described in the utility model, the rich solution completing the 3rd heat exchange enters in rich solution current divider 16, to be split into two-way via rich solution splitter inlet 161.

According in smoke carbon dioxide capture recovery system described in the utility model, the setting position of the 3rd absorption tower entrance 114A and the 3rd absorption tower outlet 114B can the concrete condition of apparent absorption tower 11 be determined.Because being usually filled with multistage filler (not shown) in absorption tower 11, therefore the 3rd absorption tower outlet 114B is usually located at the below of final stage filler.So, temperature difference between the rich solution that can make full use of the differing heights place in absorption tower 11 (in other words, the temperature of temperature higher than the rich liquid stream of discharging from second absorption tower outlet 113B of the rich liquid stream that 114B discharges is exported) from the 3rd absorption tower, the rich solution at differing heights place is drawn and makes them carry out heat exchange in outside, thus the rich solution of discharging from second absorption tower outlet 113B to be absorbed heat by heat exchange intensification, thus be conducive to the desorb of rich solution in desorber 18.

According in smoke carbon dioxide capture recovery system described in the utility model, the setting position of the 3rd desorber entrance 184A and the 3rd desorber outlet 184B can be determined depending on the concrete condition of desorber 18.Such as, be usually filled with multistage filler (not shown) in Analytic Tower 18, therefore the 3rd desorber outlet 184B is usually located at the below of the second from the bottom section of filler being vertically in below, and the 3rd desorber entrance 184A is usually located at the below of the final stage filler being vertically in below.Lean solution from the 3rd desorber outlet 184B carries out heat exchange outside desorber 18, heat absorption is back in Analytic Tower 18 via the 3rd desorber entrance 184A after heating up, improve the temperature of Analytic Tower 18 in the part at the 3rd desorber entrance 184A place, be conducive to Desorption of Carbon Dioxide.

According in smoke carbon dioxide capture recovery system described in the utility model, the first desorber entrance 182A is usually located at the epimere of desorber 18, and the second desorber entrance 183A is usually located at the stage casing of desorber 18.The rich solution completing the 3rd heat exchange enters in rich solution current divider 16, to be split into two-way via rich solution splitter inlet 161.For the road rich solution entered via the second desorber entrance 183A, the water vapour entered in desorber tower chamber 1811 from the 5th desorber entrance 186A can be made to carry out desorb to the rich solution from described two-way, thus make to rise to the first desorber entrance 182A place carries out the water vapour of desorb amount minimizing to the rich solution from the first desorber entrance 182A, water vapour is made to make full use of in absorption tower 18 thus, and effective top controlling steam heating Analytic Tower 18, and be conducive to controlling the amount of steam from the first desorber outlet 182B discharge.

According in smoke carbon dioxide capture recovery system described in the utility model, lean solution discharges a large amount of water vapour through flash tank 20 flash distillation, this part water vapour temperature and pressure after vapour compression machine at the bottom of Analytic Tower 21 pressurizes all improves (being such as forced into 110-120 DEG C by 70-90 DEG C), the quality of water vapour significantly promotes, and higher than the lean solution temperature in desorber 18; The rich solution sprayed with top two-way after entering the bottom of desorber 18 via the 4th desorber entrance 185A carries out heat exchange, water recovery Cheng Shui discharges a large amount of latent heat of vaporization, can effectively promote rich solution desorption efficiency, reduce the consumption from the hot water and steam of boiling device 19, thus reduce the energy consumption that boiling device 19 produces water vapour.

According in smoke carbon dioxide capture recovery system described in the utility model, the amount that absorbing tower chamber 1111 holds absorbent in advance can be determined in the process of smoke carbon dioxide capture recovery system actual cycle in apparent absorption agent.

In one embodiment, described from outside containing hot flue gas with pressure can from coal-burning power plant.

In one embodiment, the described temperature containing hot flue gas with pressure from outside can be 100 ~ 300 DEG C.。

In one embodiment, described absorbent can be alkanolamine solution, is certainly not limited thereto, and those skilled in the art can select other suitable absorbent any.

In one embodiment, with reference to Fig. 1, absorption tower 11 also can have: absorption tower silk screen 115, for filtering the water vapour of the cooling that may be mixed in the carbon dioxide discharged after desorb and condensation.

In one embodiment, lean solution cooler 24 can be water cooler.

In one embodiment, with reference to Fig. 1, described smoke carbon dioxide capture recovery system also can comprise one-level vapour compression machine 25.Correspondingly, Analytic Tower 18 also can have: the 6th desorber entrance 187A, be arranged at desorber tower body 181, be communicated in desorber tower chamber 1811 lower than the first desorber entrance 182A, higher than the second desorber entrance 183A, and be communicated in the side of one-level vapour compression machine 25; And the 4th desorber outlet 185B, be arranged at desorber tower body 181, be communicated in desorber tower chamber 1811 lower than the 6th desorber entrance 187A, higher than the second desorber entrance 183A, and be communicated in the opposite side of one-level vapour compression machine 25.Wherein, in desorber tower chamber 1811 on flowing water vapour via the 4th desorber outlet 185B extract out, via one-level vapour compression machine 25 pressurize heat up, be back in desorber tower chamber 1811 via the 6th desorber entrance 187A afterwards, to carry out auxiliary heating desorb to the rich solution entered in desorber tower chamber 1811 via the first desorber entrance 182A.

In one embodiment, with reference to Fig. 1, described smoke carbon dioxide capture recovery system also can comprise second steam compressor 26.Correspondingly, Analytic Tower 18 also can have: the 7th desorber entrance 188A, be arranged at desorber tower body 181, higher than the second desorber entrance 183A, lower than the 4th desorber outlet 185B and be communicated in desorber tower chamber 1811, and be communicated in the side of second steam compressor 26; 5th desorber outlet 186B, is arranged at desorber tower body 181, is communicated in desorber tower chamber 1811 lower than the second desorber entrance 183A, and be communicated in the opposite side of second steam compressor 26.Wherein, in desorber tower chamber 1811 on flowing water vapour via the 5th desorber outlet 186B extract out, via second steam compressor 26 pressurize heat up, be back in desorber tower chamber 1811 via the 7th desorber entrance 188A afterwards, to carry out auxiliary heating desorb to the rich solution entered in desorber tower chamber 1811 via the second desorber entrance 183A.

In one embodiment, with reference to Fig. 1, Analytic Tower 18 also can have: desorber silk screen 180, be arranged at the top in the desorber tower chamber 1811 of desorber tower body 181, for filtering the carbon dioxide discharged after rich solution parsing in Analytic Tower 18, the carbon dioxide after filtration is discharged via the first desorber outlet 182B.

In one embodiment, with reference to Fig. 1, described smoke carbon dioxide capture recovery system also can comprise: choke valve 27, and the second boiling device of one end connection boiling device 19 exports the flash tank entrance 202 of 193 and other end connection flash tank 20, for regulating the flow of the lean solution entered in flash tank 20.

In one embodiment, boiling device 19 can be shell-and-tube heat exchanger.Wherein, shell is used for passing into water and produces steam, and pipe is used for passing into lean solution.

In one embodiment, with reference to Fig. 1, described smoke carbon dioxide capture recovery system also can comprise: water washing mechanism 28, and water washing mechanism 28 can comprise water scrubber 281, washing water circulating pump 282, washing water water cooler 283 and washing water and feed pipe 284.Water scrubber 281 is arranged between flue gas waste heat recovery heat exchanger 10 and absorption tower 11, has: water scrubber tower body 2811, is formed with the water scrubber tower chamber 28111 holding washing water; First water scrubber entrance 2812A, is arranged at the top of water scrubber tower body 2811 and is communicated with water scrubber tower chamber 28111; First water scrubber outlet 2812B, is arranged at the bottom of water scrubber tower body 2811 and is communicated with water scrubber tower chamber 28111; Second water scrubber entrance 2813A, is arranged at the bottom of water scrubber tower body 2811 and is communicated with water scrubber tower chamber 28111, entering in water scrubber tower chamber 28111 for the flue gas in the flue gas delivery pipe of flue gas waste heat recovery heat exchanger 10; And second water scrubber outlet 2813B, be arranged at water scrubber tower body 2811 top and be communicated with water scrubber tower chamber 28111.Washing water circulating pump 282 is communicated with the first water scrubber outlet 2812B of water scrubber 28.Washing water water cooler 283 one end is communicated with washing water circulating pump 282.Washing water feeds the first water scrubber entrance 2812A that pipe 284 one end is communicated with washing water water cooler 283 and other end connection water scrubber 28.Wherein, water scrubber tower chamber 28111, first water scrubber outlet 2812B, washing water circulating pump 282, washing water water cooler 283, washing water feeds pipe 284 and the first water scrubber entrance 2812A forms washing water closed circuit, when washing water circulating pump 282 is opened, washing water in the water scrubber tower chamber 28111 of water scrubber 28 is discharged via the first water scrubber outlet 2812B, pressurize via washing water circulating pump 282, lowered the temperature by washing water water cooler 283, to feed in water scrubber tower chamber 28111 that pipe 284 and the first water scrubber entrance 2812A be back to water scrubber via washing water afterwards and down spray in water scrubber, to enter in water scrubber tower chamber 28111 via the second water scrubber entrance 2813A through the flue gas of flue gas waste heat recovery heat exchanger 10 and move from the bottom up in water scrubber tower chamber 28111, the washing water down sprayed in water scrubber tower chamber 28111 contacts with the flue gas adverse current moved from the bottom up in water scrubber tower chamber 28111, to carry out impurity and purification to flue gas, flue gas after impurity and purification is discharged from the second water scrubber outlet 2813B, supplies with the first absorption tower entrance 112A to absorption tower 11.

In one embodiment, with reference to Fig. 1, water scrubber 281 also can have: water scrubber filter screen 2814, to be arranged in water scrubber tower chamber 28111 and higher than the first water scrubber entrance 2812A and lower than the second water scrubber outlet 2813B, for removing steam in flue gas and mist.

In one embodiment, with reference to Fig. 1, water washing mechanism 28 also can comprise: washing water blowoff valve 285, the first water scrubber outlet 2812B of the controlled connection water scrubber 281 in one end; And cesspool (not shown), the controlled other end being communicated in washing water blowoff valve 285; When work opened by washing water blowoff valve 285, the washing water in water scrubber 281 is discharged from the first water scrubber outlet 2812B and is discharged into cesspool via washing water blowoff valve 285.

In one embodiment, with reference to Fig. 1, described smoke carbon dioxide capture recovery system also can comprise washing water pH controlling organization 29.Washing water pH controlling organization 29 can comprise: alkali groove 291, contains alkali lye; Alkali lye transfer pipeline 292, one end is communicated in the washing water that alkali groove 291 and the other end be communicated in water scrubber and feeds pipe 284; Perform valve 293, be arranged at alkali lye transfer pipeline 292; And online pH instrument 294, be arranged at washing water and feed on pipe 284 and the downstream feeding the connectivity points J between pipe 284 at alkali lye transfer pipeline 292 and washing water.When online pH detects that washing water feeds the pH of the washing water in pipe 284 lower than during in alkaline setting, perform valve 293 to open, alkali lye in alkali groove 291 is carried via alkali lye transfer pipeline 292 and is entered washing water via alkali lye transfer pipeline 292 and the washing water connectivity points J fed between pipe 284 and feeds pipe 284, pH value adjustment is carried out with the washing water fed in pipe 284 washing water, to make pH be not less than described setting, the washing water after pH regulates feeds pipe 284 via washing water and the first water scrubber entrance 2812A enters in the water scrubber tower chamber 28111 of water scrubber; When online pH detects that the pH of the washing water that washing water feeds in pipe 284 is not less than described setting, perform valve 293 and automatically close; PH is not less than the water water suction of described setting for removing sulfide contained by flue gas and itrated compound impurity in water scrubber, to realize described impurity and purification.

In one embodiment, also can comprise with reference to Fig. 1, washing water pH controlling organization 29: flowmeter 295, is arranged at alkali lye transfer pipeline 292, for measuring the flow of the alkali lye in alkali lye transfer pipeline 292.

In one embodiment, described setting is 8.

In one embodiment, alkali lye can be sodium bicarbonate aqueous solution, is certainly not limited thereto, and those skilled in the art can select any suitable concrete alkali lye.

In one embodiment, with reference to Fig. 1, described smoke carbon dioxide capture recovery system also can comprise corrugated plating separator 30.Corrugated plating separator 30 has: corrugated plating shell separator 301, is formed with corrugated plating separator cavity 3011; Corrugated plating 302, is arranged in corrugated plating separator cavity 3011; Corrugated plating separator inlet 303, is arranged at corrugated plating shell separator 301 in the position lower than corrugated plating and the second water scrubber outlet 2813B of connection water scrubber; First wave card separator outlet 304, is arranged at the top of corrugated plating shell separator 301 and is communicated in corrugated plating separator cavity 3011 higher than corrugated plating 302; And Second Wave card separator outlet 305, be arranged at the bottom of corrugated plating shell separator 301 and be communicated in corrugated plating separator cavity 3011.Wherein, the flue gas of discharging via the second water scrubber outlet 2813B of water scrubber enters in corrugated plating separator cavity 3011 by corrugated plating separator inlet 303, flue gas moves from the bottom up in corrugated plating separator cavity 3011, through corrugated plating 302, to remove the free water in flue gas, the flue gas of removing free water is discharged via first wave card separator outlet 304 and is supplied with the first absorption tower entrance 112A to absorption tower 11, and free water is collected in the bottom of corrugated plating separator cavity 3011 and can discharges via Second Wave card separator outlet 305.

In one embodiment, with reference to Fig. 1, corrugated plating separator 30 also can have: corrugated plating separator silk screen 306, to be arranged in corrugated plating separator cavity 3011 and between corrugated plating 301 and first wave card separator outlet 304, for removing steam in flue gas and impurity.Wherein, flue gas moves from the bottom up in corrugated plating separator cavity 3011, through corrugated plating 301, to remove the free water in flue gas, the flue gas of removing free water removes steam and impurity through corrugated plating separator silk screen 306 again, flue gas is discharged via first wave card separator outlet 304 and is supplied with the first absorption tower entrance 112A to absorption tower 11 afterwards, free water, condensation after steam and impurity sedimentation and be collected in corrugated plating separator cavity 3011 bottom and can discharge via Second Wave card separator outlet 305.

In one embodiment, with reference to Fig. 1, corrugated plating separator also can have: self-draining valve 307, be arranged at corrugated plating shell separator 301 outer and be communicated in Second Wave card separator outlet 305, after the hydraulic pressure of the water layer that the steam being collected in the free water of the bottom of corrugated plating separator cavity 3011 and condensation when sedimentation is formed reaches setting, self-draining valve 307 is opened automatically, with the free water of the bottom by being collected in corrugated plating separator cavity 3011, steam after condensation and impurity are expelled to cesspool (not shown) via Second Wave card separator outlet 305.

In one embodiment, with reference to Fig. 1, smoke carbon dioxide capture recovery system also can comprise: booster fan 31, side is communicated in the first absorption tower entrance 112A that the first wave card separator outlet 304 of corrugated plating separator 30 and opposite side are communicated in absorption tower 11, carries out aspirating and pressurize and supplied to the first absorption tower entrance 112A by the flue gas after pressurization with the flue gas of discharging via the first wave card separator outlet 304 of corrugated plating separator 30.

According in smoke carbon dioxide capture recovery system described in the utility model, water washing mechanism 28, washing water pH controlling organization 29 and corrugated plating separator 30 can process accordingly as the pretreatment unit of the flue gas entering the first absorption tower entrance 112A, and booster fan 31 pressurizes, thus make flue gas with pressure.

In one embodiment, the flue gas of discharging from the first absorption tower outlet 112B also carries and partially absorbs agent.Correspondingly, with reference to Fig. 1, described smoke carbon dioxide capture recovery system also can comprise washing mechanism 32.Washing mechanism 32 comprises scrubbing tower 321, cleaning solution surge tank 322 and washing pump 323.Scrubbing tower 321 has: scrubbing tower tower body 3211, is formed with the scrubbing tower cavity 32111 of accommodating cleaning solution; First washing tower inlet 3212A, be arranged at the side of scrubbing tower tower body 3211 and be positioned at the middle part of scrubbing tower tower body 3211 and be communicated in scrubbing tower cavity 32111, be communicated with the first absorption tower outlet 112B on absorption tower 11, receive the flue gas of the carbon dioxide removal that the first absorption tower outlet 112B discharges; First scrubbing tower outlet 3212B, is arranged at the top of scrubbing tower tower body 3211 and is communicated in scrubbing tower cavity 32111; Second washing tower inlet 3213A, is arranged at the opposite side of scrubbing tower tower body 3211 and is communicated in scrubbing tower cavity 32111 higher than the first washing tower inlet 3212A; And second scrubbing tower outlet 3213B, be arranged at the bottom of scrubbing tower tower body 3211 and be communicated in scrubbing tower cavity 32111.Cleaning solution surge tank 322 one end is communicated in the second scrubbing tower outlet 3213B of scrubbing tower 321.Washing pump 323 side is communicated in the other end of cleaning solution surge tank 322 and opposite side is communicated in the second washing tower inlet 3213A of scrubbing tower 321.Wherein, the scrubbing tower cavity 32111 of the second washing tower inlet 3213A of scrubbing tower 321, the scrubbing tower tower body 3211 of scrubbing tower 321, the second scrubbing tower outlet 3213B of scrubbing tower 321, cleaning solution surge tank 322, washing pump 323 form cleaning solution closed circuit; When washing pump 323 is opened, the cleaning solution in the scrubbing tower cavity 32111 of the scrubbing tower tower body 3211 of scrubbing tower 321 exports 3213B discharge via the second scrubbing tower of scrubbing tower 321, enters in the scrubbing tower cavity 32111 of the scrubbing tower tower body 3211 of scrubbing tower 321 and down spray in scrubbing tower cavity 32111 via the second washing tower inlet 3213A of cleaning solution surge tank 322, washing pump 323 and scrubbing tower 321; The carbon dioxide removal that the first absorption tower outlet 112B on absorption tower 11 discharges and to carry in the flue gas that partially absorbs agent enters the scrubbing tower tower body 3211 of scrubbing tower 321 scrubbing tower cavity 32111 via the first washing tower inlet 3212A of scrubbing tower 321 and to move from lower to upper in scrubbing tower cavity 32111; The cleaning solution down sprayed in scrubbing tower cavity 32111 contacts with the flue gas adverse current partially absorbing agent that carries moved from the bottom up in scrubbing tower cavity 32111, to purify flue gas, thus the agent that partially absorbs entrained in flue gas is deviate from, washings and the absorbent sedimentation of deviating from also are gathered in scrubbing tower cavity 32111; The flue gas deviating from absorbent is discharged from the first scrubbing tower outlet 3212B of scrubbing tower.

In one embodiment, the first scrubbing tower outlet 3212B of scrubbing tower 321 can be communicated in power-plant flue gas pipeline.

In one embodiment, cleaning solution can be deionized water.

In one embodiment, with reference to Fig. 1, washing mechanism 32 also can comprise: delivery pipe 324, is communicated in cleaning solution surge tank 322 and is communicated in cleaning solution storage tank (not shown).

In one embodiment, with reference to Fig. 1, Analytic Tower 18 also can have: the 8th desorber entrance 189A, is arranged at desorber tower body 181 and is communicated in desorber tower chamber 1811.Correspondingly, with reference to Fig. 1, described smoke carbon dioxide capture recovery system also can comprise recovery carbon dioxide treatment mechanism 33.Reclaim carbon dioxide treatment mechanism 33 to comprise: desorber top heat exchanger 331, be communicated with the first desorber outlet 182B of desorber 18; Carbon dioxide cooler 332, is communicated with desorber top heat exchanger 331; Desorber top gas liquid/gas separator 333, is communicated with carbon dioxide cooler 332 and desorb tower top heat exchanger 331; Desorb tower top surge tank 334, is communicated with desorber top heat exchanger 333; And desorb tower top vapour compression machine 335, one end is communicated with desorb tower top surge tank 334, and the other end is communicated with the 8th desorber entrance 189A of desorber 18.Wherein, via the first desorber outlet 182B of desorber 18 discharge containing cooling after desorb but the carbon dioxide of uncondensable water vapour enters desorber top heat exchanger 331 carries out heat exchange and cool, after heat exchange containing cooling after desorb but the carbon dioxide of uncondensable water vapour enters carbon dioxide cooler 332 is further cooled, cooled containing cooling after desorb but the carbon dioxide of uncondensable water vapour enters desorber top gas liquid/gas separator 333, gas-liquid separation is carried out by cooling in desorber top gas liquid/gas separator 333, cooling makes water vapour condensation form aqueous water and decline and be collected in desorber top heat exchanger 331, the carbon dioxide isolating steam is discharged via the top of desorber top gas liquid/gas separator 333, the aqueous water formed escapes and enter desorber top heat exchanger 331 to carry out described heat exchange via the bottom of desorber top gas liquid/gas separator 333, in desorber top heat exchanger 331, carbon dioxide heat release is lowered the temperature, isolated water heat absorption heats up and becomes water vapour, water vapour via desorb tower top surge tank 334 buffer storage, afterwards via after the pressurization of desorb tower top vapour compression machine 335 through entering in desorber tower chamber 1811 by the 8th desorber entrance 189A of desorber 18, carry out heating desorption for the rich solution be collected in desorber tower chamber 1811.

In one embodiment, with reference to Fig. 1, reclaim carbon dioxide treatment mechanism 33 and also can comprise: delivery pipe 336, be communicated with desorb tower top surge tank 334 and collecting storage tank (not shown).

In one embodiment, with reference to Fig. 1, reclaim carbon dioxide treatment mechanism 33 also can comprise: compression unit 337, be communicated in desorber top gas liquid/gas separator 333 and receive desorber top gas liquid/gas separator 333 discharge separation after carbon dioxide and received carbon dioxide is compressed.

In one embodiment, with reference to Fig. 1, compression unit 337 is at least one.

In one embodiment, with reference to Fig. 1, compression unit 337 comprises: compressor 3371; And water cooler 3372, be arranged on the downstream of compressor 3371 and be communicated with compressor 3371 to cool the carbon dioxide after compression.

In one embodiment, with reference to Fig. 1, compression unit 337 is four and is cascaded, and is certainly not limited thereto, and the series connection number of compression unit 337 can change depending on specific requirement.

In one embodiment, with reference to Fig. 1, reclaim carbon dioxide treatment mechanism 33 and also can comprise: desorber top heat exchanger silk screen 3311, for filtering the aqueous water isolating the condensation formation that may contain in the carbon dioxide of steam.

Claims (10)

1. a smoke carbon dioxide capture recovery system, is characterized in that, comprising:

Flue gas waste heat recovery heat exchanger (10);

Absorption tower (11), has:

Absorption tower tower body (111), is formed with the absorbing tower chamber (1111) holding absorbent in advance;

First absorption tower entrance (112A), is arranged at the bottom of absorption tower tower body (111) and is communicated in absorbing tower chamber (1111) and is communicated in flue gas waste heat recovery heat exchanger (10);

First absorption tower outlet (112B), is arranged at the top of absorption tower tower body (111) and is communicated in absorbing tower chamber (1111);

Second absorption tower entrance (113A), is arranged at the top of absorption tower tower body (111) and is communicated in absorbing tower chamber (1111);

Second absorption tower outlet (113B), is arranged at the bottom of absorption tower tower body (111) and is communicated in absorbing tower chamber (1111);

3rd absorption tower entrance (114A), is arranged at the bottom of absorption tower tower body (111) and is positioned at the below of the first absorption tower entrance (112A) and is positioned at the top that second absorption tower exports (113B); And

3rd absorption tower outlet (114B), is arranged at the bottom of absorption tower tower body (111) and is positioned between the first absorption tower entrance (112A) and the 3rd absorption tower entrance (114A);

Rich solution pump (12), side is communicated in second absorption tower outlet (113B) on absorption tower (11);

Absorption tower inter-stage circulating pump (13), side is communicated in the 3rd absorption tower entrance (114A) on absorption tower (11);

Absorption tower inter-stage circulation heat exchanger (14), has:

First absorption tower inter-stage circulation heat exchanger entrance (141A), is communicated in the opposite side of rich solution pump (12);

First absorption tower inter-stage circulation heat exchanger outlet (141B), is communicated in flue gas waste heat recovery heat exchanger (10);

Second absorption tower inter-stage circulation heat exchanger entrance (142A), is communicated in the 3rd absorption tower outlet (114B) on absorption tower (11); And

Second absorption tower inter-stage circulation heat exchanger outlet (142B), is communicated in the opposite side on absorption tower inter-stage circulating pump (13);

One-level poor rich liquid heat exchanger (15), has:

First one-level poor rich liquid heat exchanger entrance (151A), is communicated in flue gas waste heat recovery heat exchanger (10);

First one-level poor rich liquid heat exchanger outlet (151B);

Second one-level poor rich liquid heat exchanger entrance (152A); And

Second one-level poor rich liquid heat exchanger outlet (152B);

Rich solution current divider (16), has:

Rich solution splitter inlet (161), is communicated in the first one-level poor rich liquid heat exchanger outlet (151B) of one-level poor rich liquid heat exchanger (15);

First rich solution current divider outlet (162); And

Second rich solution current divider outlet (163);

Secondary poor rich liquid heat exchanger (17), has:

First secondary poor rich liquid heat exchanger entrance (171A), is communicated in the second rich solution current divider outlet (163) of rich solution current divider (16);

First secondary poor rich liquid heat exchanger outlet (171B);

Second secondary poor rich liquid heat exchanger entrance (172A); And

Second secondary poor rich liquid heat exchanger outlet (172B), is communicated in the second one-level poor rich liquid heat exchanger entrance (152A) of one-level poor rich liquid heat exchanger (15);

Desorber (18), has:

Desorber tower body (181), is formed with desorber tower chamber (1811);

First desorber entrance (182A), be arranged at desorber tower body (181) and be communicated in desorber tower chamber (1811) and be communicated in rich solution current divider (16) first rich solution current divider outlet (162);

Second desorber entrance (183A), be arranged at desorber tower body (181) and be communicated in desorber tower chamber (1811) and be communicated in rich solution current divider (16) second rich solution current divider outlet (163);

3rd desorber entrance (184A), is arranged at the bottom of desorber tower body (181) and is positioned at the below of the second desorber entrance (183A) and is communicated in desorber tower chamber (1811);

4th desorber entrance (185A), is arranged at the bottom of desorber tower body (181) and is positioned at the below of the 3rd desorber entrance (184A) and is communicated in desorber tower chamber (1811);

5th desorber entrance (186A), is arranged at the bottom of desorber tower body (181) and is communicated in desorber tower chamber (1811);

First desorber outlet (182B), is arranged at the top of desorber tower body (181) and is communicated in desorber tower chamber (1811);

Second desorber outlet (183B), is arranged at the bottom of desorber tower body (181) and is positioned at the below of the 4th desorber entrance (185A) and the 5th desorber entrance (186A) and is communicated in desorber tower chamber (1811); And

3rd desorber outlet (184B), is arranged at the bottom of desorber tower body (181) and is positioned between the second desorber entrance (183A) and the 3rd desorber entrance (184A) and is communicated in desorber tower chamber (1811);

Boiling device (19), can produce water vapour, have:

Boiling device entrance (191), is communicated in the second desorber outlet (183B) of desorber (18);

First boiling device outlet (192), is communicated in the 5th desorber entrance (186A) of desorber (18);

Second boiling device outlet (193), is communicated in boiling device entrance (191);

Flash tank (20), has:

Flash tank tank body (201);

Flash tank entrance (202), be arranged at flash tank tank body (201) and be communicated in boiling device (19) second boiling device outlet (193);

First flash tank outlet (203), is arranged at the top of flash tank tank body (201);

Second flash tank outlet (204), is arranged at the bottom of flash tank tank body (201);

Vapour compression machine at the bottom of desorber (21), side is communicated in the first flash tank outlet (203) of flash tank (20) and opposite side is communicated in the 4th desorber entrance (185A) of Analytic Tower (18);

Lean pump (22), side is communicated in the second flash tank outlet (204) of flash tank (20); Desorber inter-stage circulation heat exchanger (23), has:

First desorber inter-stage circulation heat exchanger entrance (231A), is communicated in the opposite side of lean pump (22);

First desorber inter-stage circulation heat exchanger outlet (231B), is communicated in the second secondary poor rich liquid heat exchanger entrance (172A) of secondary poor rich liquid heat exchanger (17);

Second desorber inter-stage circulation heat exchanger entrance (232A), is communicated in the 3rd desorber outlet (184B) of desorber (18); And

Second desorber inter-stage circulation heat exchanger outlet (232B), is communicated in the 3rd desorber entrance (184A) of desorber (18);

Lean solution cooler (24), side is communicated in the second one-level poor rich liquid heat exchanger outlet (152B) of one-level poor rich liquid heat exchanger (15) and opposite side is communicated in the second absorption tower entrance (113A) on absorption tower (11);

Wherein,

Flowing through flue gas waste heat recovery heat exchanger (10) containing hot flue gas with pressure and to enter in absorbing tower chamber (1111) via the first absorption tower entrance (112A) of absorption tower (11) and move from the bottom up in absorbing tower chamber (1111) from outside;

Absorbent to enter in absorbing tower chamber (1111) from the second absorption tower entrance (113A) of absorption tower (11) and down sprays in absorbing tower chamber (1111);

The absorbent down sprayed contacts with the flue gas adverse current moved from the bottom up, thus the absorbent down sprayed absorbs the carbon dioxide in flue gas, the absorbent absorbing carbon dioxide becomes rich solution and is gathered in absorbing tower chamber (1111), and the flue gas being stripped of carbon dioxide exports (112B) and discharges from the first absorption tower;

The rich solution be gathered in absorbing tower chamber (1111) is discharged from second absorption tower outlet (113B), pressurize via rich solution pump (12), absorption tower inter-stage circulation heat exchanger (14) is entered via the first absorption tower inter-stage circulation heat exchanger entrance (141A), and the rich solution in absorption tower (11) exports (114B) discharge via the 3rd absorption tower and enters in absorption tower inter-stage circulation heat exchanger (14) via second absorption tower inter-stage circulation heat exchanger entrance (142A), thus export the rich solution of (113B) since second absorption tower and in absorption tower inter-stage circulation heat exchanger (14), carry out the first heat exchange from the rich solution on the 3rd absorption tower outlet (114B), rich solution heat release thus from the 3rd absorption tower outlet (114B) is lowered the temperature and exports (142B) via second absorption tower inter-stage circulation heat exchanger afterwards, absorption tower inter-stage circulating pump (13) and the 3rd absorption tower entrance (114A) are back in absorption tower (11), and heat up from the rich solution heat absorption of second absorption tower outlet (113B),

Completing the rich solution after the first heat exchange escapes and enter in flue gas waste heat recovery heat exchanger (10) via the first absorption tower inter-stage circulation heat exchanger outlet (141B), to carry out the second heat exchange at flue gas waste heat recovery heat exchanger (10) and the flue gas flowing through flue gas waste heat recovery heat exchanger (10), flue gas heat release is lowered the temperature, and rich solution heat absorption heats up;

The rich solution completing the second heat exchange from flue gas waste heat recovery heat exchanger (10) out, enter in one-level poor rich liquid heat exchanger (15) via the first one-level poor rich liquid heat exchanger entrance (151A) afterwards, to carry out the 3rd heat exchange in one-level poor rich liquid heat exchanger (15);

The rich solution completing the 3rd heat exchange enters in rich solution current divider (16) via rich solution splitter inlet (161), to be split into two-way, one tunnel exports (162) via the first rich solution current divider and the first desorber entrance (182A) enters in the desorber tower chamber (1811) of desorber (18), another road exports (163) via the second rich solution current divider and the first secondary poor rich liquid heat exchanger entrance (171A) enters in secondary poor rich liquid heat exchanger (17), to carry out the 4th heat exchange in secondary poor rich liquid heat exchanger (17), the rich solution completing the 4th heat exchange exports (171B) via the first secondary poor rich liquid heat exchanger and the second desorber entrance (183A) enters in the desorber tower chamber (1811) of desorber (18), rich solution from two-way is all collected in the desorber tower chamber (1811) of desorber (18),

Boiling device (19) produces water vapour and water vapour is exported (192) via the first boiling device and the 5th desorber entrance (186A) enters in desorber tower chamber (1811), water vapour carries out heating desorption to the rich solution be collected in desorber tower chamber (1811), become lean solution after rich solution desorb and discharge carbon dioxide, cooling after desorb and the water vapour of condensation is mixed into lean solution, and be mixed into cooling and the lean solution sedimentation of the water vapour of condensation be collected in desorber tower chamber (1811);

The carbon dioxide discharged after desorb via the first desorber export (182B) discharge, after desorb cooling but uncondensable water vapour with the carbon dioxide discharged after desorb together via first desorber outlet (182B) discharge;

Lean solution via the second desorber export (183B) discharge, to enter boiling device (19) via boiling device entrance (191) in the water vapour that produces with boiling device (19) carry out the 6th heat exchange, lean solution heat absorption heats up;

Complete the lean solution after the 6th heat exchange and export (193) discharge via the second boiling device, enter in flash tank tank body (201) via flash tank entrance (202) afterwards and carry out flash distillation, to flash off water vapour, the water vapour flashed off exports (203) via the first flash tank and to discharge and through entering in desorber tower chamber (1811) by the 4th desorber entrance (185A) after passing through vapour compression machine at the bottom of desorber (21) pressurization, to enter into the exporting via the first boiling device of boiling device (19) (192) and the 5th desorber entrance (186A) together with the water vapour in desorber tower chamber (1811), heating desorption is carried out to the rich solution be collected in desorber tower chamber (1811),

Lean solution after flash distillation process exports (204) via the second flash tank and discharges in flash tank tank body (201), afterwards by lean pump (22) pressurization, enter in desorber inter-stage circulation heat exchanger (23) via the first desorber inter-stage circulation heat exchanger entrance (231A), and the lean solution in Analytic Tower (18) exports (184B) via the 3rd desorber enters in desorber inter-stage circulation heat exchanger (23), thus the 7th heat exchange is carried out from the lean solution of the 3rd desorber outlet (184B) and the lean solution exporting (204) from the second flash tank in desorber inter-stage circulation heat exchanger (23), lean solution heat absorption thus from the 3rd desorber outlet (184B) heats up, afterwards via the second desorber inter-stage circulation heat exchanger outlet (232B), 3rd desorber entrance (184A) turns back in Analytic Tower (18), and lower the temperature from the lean solution heat release of the second flash tank outlet (204),

The lean solution completing the 7th heat exchange is discharged via the first desorber inter-stage circulation heat exchanger outlet (231B) and enters in secondary poor rich liquid heat exchanger (17) via the second secondary poor rich liquid heat exchanger entrance (172A), thus in secondary poor rich liquid heat exchanger (17), enter the rich solution in secondary poor rich liquid heat exchanger (17) via the first secondary poor rich liquid heat exchanger entrance (171A) and carry out described 4th heat exchange via the second secondary poor rich liquid heat exchanger entrance (172A) lean solution entered in secondary poor rich liquid heat exchanger (17), rich solution heat absorption heats up, lean solution heat release is lowered the temperature,

The lean solution completing the 4th heat exchange exports (172B) via the second secondary poor rich liquid heat exchanger and discharges and enter in one-level poor rich liquid heat exchanger (15) via the second one-level poor rich liquid heat exchanger entrance (152A), thus in one-level poor rich liquid heat exchanger (15), enter the rich solution in one-level poor rich liquid heat exchanger (15) via the first one-level poor rich liquid heat exchanger entrance (151A) and carry out described 3rd heat exchange via the second one-level poor rich liquid heat exchanger entrance (152A) lean solution entered in one-level poor rich liquid heat exchanger (15), rich solution heat absorption heats up, lean solution heat release is lowered the temperature,

The lean solution completing described 3rd heat exchange exports (152B) via the second one-level poor rich liquid heat exchanger and escapes and enter in lean solution cooler (24) from one-level poor rich liquid heat exchanger (15), with cooled in lean solution cooler (24);

Cooled lean solution is discharged and is entered in desorber tower chamber (1811) via the second desorber entrance (183A) as absorbent in lean solution cooler (24), thus moves from the bottom up in absorbing tower chamber (1111).

2. smoke carbon dioxide capture recovery system according to claim 1, is characterized in that,

Described smoke carbon dioxide capture recovery system also comprises one-level vapour compression machine (25);

Analytic Tower (18) also has:

6th desorber entrance (187A), be arranged at desorber tower body (181), be communicated in desorber tower chamber (1811) lower than the first desorber entrance (182A), higher than the second desorber entrance (183A), and be communicated in the side of one-level vapour compression machine (25); And

4th desorber outlet (185B), be arranged at desorber tower body (181), be communicated in desorber tower chamber (1811) lower than the 6th desorber entrance (187A), higher than the second desorber entrance (183A), and be communicated in the opposite side of one-level vapour compression machine (25);

Wherein, the water vapour upwards flowed in desorber tower chamber (1811) exports (185B) via the 4th desorber and extracts out, heats up via one-level vapour compression machine (25) pressurization, be back in desorber tower chamber (1811) via the 6th desorber entrance (187A) afterwards, to carry out auxiliary heating desorb to the rich solution entered in desorber tower chamber (1811) via the first desorber entrance (182A).

3. smoke carbon dioxide capture recovery system according to claim 2, is characterized in that,

Described smoke carbon dioxide capture recovery system also comprises second steam compressor (26);

Analytic Tower (18) also has:

7th desorber entrance (188A), be arranged at desorber tower body (181), higher than the second desorber entrance (183A), lower than the 4th desorber outlet (185B) and be communicated in desorber tower chamber (1811), and be communicated in the side of second steam compressor (26);

5th desorber outlet (186B), be arranged at desorber tower body (181), be communicated in desorber tower chamber (1811) lower than the second desorber entrance (183A), and be communicated in the opposite side of second steam compressor (26);

Wherein, the water vapour upwards flowed in desorber tower chamber (1811) exports (186B) via the 5th desorber and extracts out, heats up via second steam compressor (26) pressurization, be back in desorber tower chamber (1811) via the 7th desorber entrance (188A) afterwards, to carry out auxiliary heating desorb to the rich solution entered in desorber tower chamber (1811) via the second desorber entrance (183A).

4. smoke carbon dioxide capture recovery system according to claim 1, is characterized in that, described smoke carbon dioxide capture recovery system also comprises:

Water washing mechanism (28), comprising:

Water scrubber (281), is arranged between flue gas waste heat recovery heat exchanger (10) and absorption tower (11), has:

Water scrubber tower body (2811), is formed with the water scrubber tower chamber (28111) holding washing water;

First water scrubber entrance (2812A), is arranged at the top of water scrubber tower body (2811) and is communicated with water scrubber tower chamber (28111);

First water scrubber outlet (2812B), is arranged at the bottom of water scrubber tower body (2811) and is communicated with water scrubber tower chamber (28111);

Second water scrubber entrance (2813A), be arranged at the bottom of water scrubber tower body (2811) and be communicated with water scrubber tower chamber (28111), entering in water scrubber tower chamber (28111) for the flue gas in the flue gas delivery pipe of flue gas waste heat recovery heat exchanger (10); And

Second water scrubber outlet (2813B), is arranged at the top of water scrubber tower body (2811) and is communicated with water scrubber tower chamber (28111);

Washing water circulating pump (282), is communicated with the first water scrubber outlet (2812B) of water scrubber (28);

Washing water water cooler (283), one end is communicated with washing water circulating pump (282); And

Washing water feeds pipe (284), and one end is communicated with the first water scrubber entrance (2812A) of washing water water cooler (283) and other end connection water scrubber (28);

Wherein,

Water scrubber tower chamber (28111), first water scrubber outlet (2812B), washing water circulating pump (282), washing water water cooler (283), washing water feeds pipe (284) and the first water scrubber entrance (2812A) forms washing water closed circuit, when washing water circulating pump (282) is opened, washing water in the water scrubber tower chamber (28111) of water scrubber (28) exports (2812B) via the first water scrubber and discharges, pressurize via washing water circulating pump (282), lowered the temperature by washing water water cooler (283), to feed in water scrubber tower chamber (28111) that pipe (284) and the first water scrubber entrance (2812A) be back to water scrubber via washing water afterwards and down spray in water scrubber,

To enter in water scrubber tower chamber (28111) via the second water scrubber entrance (2813A) through the flue gas of flue gas waste heat recovery heat exchanger (10) and move from the bottom up in water scrubber tower chamber (28111);

The washing water down sprayed in water scrubber tower chamber (28111) contacts with the flue gas adverse current moved from the bottom up in water scrubber tower chamber (28111), to carry out impurity and purification to flue gas;

Flue gas after impurity and purification exports (2813B) from the second water scrubber and discharges, with the first absorption tower entrance (112A) supply to absorption tower (11).

5. smoke carbon dioxide capture recovery system according to claim 4, is characterized in that, described smoke carbon dioxide capture recovery system also comprises:

Washing water pH controlling organization (29), comprising:

Alkali groove (291), contains alkali lye;

Alkali lye transfer pipeline (292), one end is communicated in the washing water that alkali groove (291) and the other end be communicated in water scrubber and feeds pipe (284);

Perform valve (293), be arranged at alkali lye transfer pipeline (292); And

Online pH instrument (294), being arranged at washing water, to feed pipe (284) upper and be positioned at the downstream that alkali lye transfer pipeline (292) and washing water feed the connectivity points (J) of managing between (284);

When online pH detects that washing water feeds the pH of the washing water in pipe (284) lower than during in alkaline setting, perform valve (293) to open, alkali lye in alkali groove (291) is carried via alkali lye transfer pipeline (292) and is entered washing water via alkali lye transfer pipeline (292) and the washing water connectivity points (J) fed between pipe (284) and feeds pipe (284), pH value adjustment is carried out with the washing water fed in pipe (284) washing water, described setting is not less than to make pH, washing water after pH regulates feeds pipe (284) via washing water and the first water scrubber entrance (2812A) enters in the water scrubber tower chamber (28111) of water scrubber,

When online pH detects that the pH of the washing water that washing water feeds in pipe (284) is not less than described setting, perform valve (293) and automatically close;

PH is not less than the water water suction of described setting for removing sulfide contained by flue gas and itrated compound impurity in water scrubber, to realize described impurity and purification.

6. smoke carbon dioxide capture recovery system according to claim 4, is characterized in that, described smoke carbon dioxide capture recovery system also comprises:

Corrugated plating separator (30), has:

Corrugated plating shell separator (301), is formed with corrugated plating separator cavity (3011);

Corrugated plating (302), is arranged in corrugated plating separator cavity (3011);

Corrugated plating separator inlet (303), is arranged at corrugated plating shell separator (301) and the second water scrubber outlet (2813B) of connection water scrubber in the position lower than corrugated plating;

First wave card separator outlet (304), is arranged at the top of corrugated plating shell separator (301) and is communicated in corrugated plating separator cavity (3011) higher than corrugated plating (302); And

Second Wave card separator outlet (305), is arranged at the bottom of corrugated plating shell separator (301) and is communicated in corrugated plating separator cavity (3011);

Wherein, the flue gas of discharging via the second water scrubber outlet (2813B) of water scrubber enters in corrugated plating separator cavity (3011) by corrugated plating separator inlet (303), flue gas moves from the bottom up in corrugated plating separator cavity (3011), through corrugated plating (302), to remove the free water in flue gas, the flue gas of removing free water is discharged with the first absorption tower entrance (112A) supply to absorption tower (11) via first wave card separator outlet (304), free water is collected in the bottom of corrugated plating separator cavity (3011) and can discharges via Second Wave card separator outlet (305).

7. smoke carbon dioxide capture recovery system according to claim 6, is characterized in that, smoke carbon dioxide capture recovery system also comprises:

Booster fan (31), side is communicated in the first absorption tower entrance (112A) that the first wave card separator outlet (304) of corrugated plating separator (30) and opposite side are communicated in absorption tower (11), carries out aspirating and pressurize and supplied to the first absorption tower entrance (112A) by the flue gas after pressurization with the flue gas of discharging via the first wave card separator outlet (304) of corrugated plating separator (30).

8. smoke carbon dioxide capture recovery system according to claim 1, is characterized in that,

The flue gas of discharging from the first absorption tower outlet (112B) also carries and partially absorbs agent;

Described smoke carbon dioxide capture recovery system also comprises:

Washing mechanism (32), comprising:

Scrubbing tower (321), has:

Scrubbing tower tower body (3211), is formed with the scrubbing tower cavity (32111) of accommodating cleaning solution;

First washing tower inlet (3212A), be arranged at the side of scrubbing tower tower body (3211) and be positioned at the middle part of scrubbing tower tower body (3211) and be communicated in scrubbing tower cavity (32111), be communicated with first absorption tower outlet (112B) on absorption tower (11), receive the flue gas of the carbon dioxide removal that the first absorption tower outlet (112B) is discharged;

First scrubbing tower outlet (3212B), is arranged at the top of scrubbing tower tower body (3211) and is communicated in scrubbing tower cavity (32111);

Second washing tower inlet (3213A), is arranged at the opposite side of scrubbing tower tower body (3211) and is communicated in scrubbing tower cavity (32111) higher than the first washing tower inlet (3212A); And

Second scrubbing tower outlet (3213B), is arranged at the bottom of scrubbing tower tower body (3211) and is communicated in scrubbing tower cavity (32111);

Cleaning solution surge tank (322), one end is communicated in the second scrubbing tower outlet (3213B) of scrubbing tower (321); And

Washing pump (323), side is communicated in the other end of cleaning solution surge tank (322) and opposite side is communicated in second washing tower inlet (3213A) of scrubbing tower (321);

Wherein,

The scrubbing tower cavity (32111) of second washing tower inlet (3213A) of scrubbing tower (321), the scrubbing tower tower body (3211) of scrubbing tower (321), the second scrubbing tower outlet (3213B), cleaning solution surge tank (322) of scrubbing tower (321), washing pump (323) form cleaning solution closed circuit;

When washing pump (323) is opened, the cleaning solution in the scrubbing tower cavity (32111) of the scrubbing tower tower body (3211) of scrubbing tower (321) exports (3213B) discharge via the second scrubbing tower of scrubbing tower (321), enters in the scrubbing tower cavity (32111) of the scrubbing tower tower body (3211) of scrubbing tower (321) and down spray in scrubbing tower cavity (32111) via second washing tower inlet (3213A) of cleaning solution surge tank (322), washing pump (323) and scrubbing tower (321);

First absorption tower outlet (112B) carbon dioxide removal of discharging on absorption tower (11) and to carry in the flue gas that partially absorbs agent enters the scrubbing tower tower body (3211) of scrubbing tower (321) scrubbing tower cavity (32111) via first washing tower inlet (3212A) of scrubbing tower (321) and to move from lower to upper in scrubbing tower cavity (32111);

The cleaning solution down sprayed in scrubbing tower cavity (32111) contacts with the flue gas adverse current partially absorbing agent that carries moved from the bottom up in scrubbing tower cavity (32111), to purify flue gas, thus the agent that partially absorbs entrained in flue gas is deviate from, washings and the absorbent sedimentation of deviating from also are gathered in scrubbing tower cavity (32111);

The flue gas deviating from absorbent is discharged from the first scrubbing tower outlet (3212B) of scrubbing tower.

9. smoke carbon dioxide capture recovery system according to claim 1, is characterized in that,

Analytic Tower (18) also has:

8th desorber entrance (189A), is arranged at desorber tower body (181) and is communicated in desorber tower chamber (1811);

Described smoke carbon dioxide capture recovery system also comprises:

Reclaim carbon dioxide treatment mechanism (33), comprising:

Desorber top heat exchanger (331), is communicated with the first desorber outlet (182B) of desorber (18);

Carbon dioxide cooler (332), is communicated with desorber top heat exchanger (331);

Desorber top gas liquid/gas separator (333), is communicated with carbon dioxide cooler (332) and desorb tower top heat exchanger (331);

Desorb tower top surge tank (334), is communicated with desorber top heat exchanger (333); And

Desorb tower top vapour compression machine (335), one end is communicated with desorb tower top surge tank (334),

The other end is communicated with the 8th desorber entrance (189A) of desorber (18);

Wherein,

The first desorber outlet (182B) via desorber (18) discharge containing cooling after desorb but the carbon dioxide of uncondensable water vapour enters desorber top heat exchanger (331) carries out heat exchange and cool;

After heat exchange containing cooling after desorb but the carbon dioxide of uncondensable water vapour enters carbon dioxide cooler (332) is further cooled;

Cooled containing cooling after desorb but the carbon dioxide of uncondensable water vapour enters desorber top gas liquid/gas separator (333), gas-liquid separation is carried out by cooling in desorber top gas liquid/gas separator (333), cooling makes water vapour condensation form aqueous water and decline and be collected in desorber top heat exchanger (331), the carbon dioxide isolating steam is discharged via the top of desorber top gas liquid/gas separator (333), the aqueous water formed escapes and enter desorber top heat exchanger (331) to carry out described heat exchange via the bottom of desorber top gas liquid/gas separator (333), in desorber top heat exchanger (331), carbon dioxide heat release is lowered the temperature, isolated water heat absorption heats up and becomes water vapour,

Water vapour via desorb tower top surge tank (334) buffer storage, afterwards via after desorb tower top vapour compression machine (335) pressurization through entering in desorber tower chamber (1811) by the 8th desorber entrance (189A) of desorber (18), carry out heating desorption for the rich solution be collected in desorber tower chamber (1811).

10. smoke carbon dioxide capture recovery system according to claim 9, is characterized in that, reclaims carbon dioxide treatment mechanism (33) and also comprises:

Compression unit (337), is communicated in desorber top gas liquid/gas separator (333) and carbon dioxide after receiving the separation that desorber top gas liquid/gas separator (333) discharges and compressing received carbon dioxide.