CN201419074Y - Shunting type energy-saving scrubbing unit using low temperature methanol - Google Patents
Shunting type energy-saving scrubbing unit using low temperature methanol Download PDFInfo
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- CN201419074Y CN201419074Y CN2009200733204U CN200920073320U CN201419074Y CN 201419074 Y CN201419074 Y CN 201419074Y CN 2009200733204 U CN2009200733204 U CN 2009200733204U CN 200920073320 U CN200920073320 U CN 200920073320U CN 201419074 Y CN201419074 Y CN 201419074Y
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P20/50—Improvements relating to the production of bulk chemicals
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Abstract
A shunting type energy-saving scrubbing unit using low temperature methanol comprises an absorption tower, a flash evaporation tower of medium pressure, a reabsorption tower, a heat regeneration tower, a methanol water tower, an exhaust gas scrubbing tower, a plurality of heat exchangers, a pump and a circulating compressor, wherein the upper section of the reabsorption tower is a flash evaporation section. The scrubbing unit is not provided with a CO2 product tower. The complexity of technical processes and the investment are reduced on the premise of ensuring the quality of CO2 products. Inthe utility model adopting novel shunting type energy-saving scrubbing (acid gas deprivation) processes using low temperature methanol, half-depleted methanol liquid on the upper section of the reabsorption tower flows back to the absorption tower and is used for absorption again, so the use quantity of the absorption tower for depleted methanol is reduced, which further results in the reduction of the quantity of energy consumed by the heat regeneration tower for heat regeneration, nitrogen used for gas stripping and steam consumed, and low level refrigeration quantity used while cooling depleted methanol.
Description
Technical field
The utility model relates to the gas purification technique field, specifically relates to use low-temp methanol as absorbent, removes the split-flow rectisol device of impurity such as organic impurities in the mist, CO2, sulfide and moisture.The energy-saving low temperature washing device for methanol of this shunting is to be applicable to that synthesis gas (hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, nitrogen, methane etc.) purifies the novel split-flow rectisol of low energy consumption (acid gas removal technology) of system synthetic ammonia, synthesizing methanol, artificial oil (gasoline, diesel oil etc.) and artificial synthetic natural gas fields such as (SNG) or natural gas purification system LNG (liquefied natural gas).
Background technology
The low-temperature rectisol technology adopts low-temp methanol as absorbent, utilizes bigger to the sour gas solubility at low temperatures physical characteristic of methyl alcohol, removes the sour gas in the unstripped gas.Low-temperature rectisol is a kind of typical Physical Absorption process, can optionally remove various sulfide and organic impurities, water etc. earlier from unstripped gas, then removes CO2, makes the purified gas after removing can reach very high degree of purification.
The first cover low temperature washing device for methanol starts from the 1950's, by the research and development of strange (Lurgi) company of German woods moral (Linde) and Shandong.Through years development, low temperature washing device for methanol mainly adopts device as shown in Figure 1 at present.This device is by absorption tower T1, middle pressure flash column T2, CO
2Compositions such as product tower T3, reabsorber T4, hot regenerator T5, methyl alcohol water tower T6, tail gas washing tower T7, some heat exchangers, pump, recycle compressor C1.Unstripped gas mixes with circulating air, enters the bottom of absorption tower T1 after first heat exchanger E1 cooling.The epimere of absorption tower T1 is CO
2Absorber portion, hypomere are H
2The S absorber portion.Unstripped gas wherein CO behind the T1 of absorption tower
2Effectively removed with impurity such as sulfide, the purified gas that is come out by absorption tower T1 goes out device after the heat exchange in the first heat exchanger E1.Absorption tower T1 epimere connects the second heat exchanger E2 and the 3rd heat exchanger E3, and the methanol gas 1,2 that absorption tower T1 epimere comes out is carried out the condensation recovery, and the methanol liquid 3,4 of recovery is back to absorption tower T1 epimere again.
Absorbed H
2Behind S and the COS, the sulfur-bearing methyl alcohol rich solution 5 that comes out at the bottom of the T1 tower of absorption tower is through the 4th heat exchanger E4, the 6th heat exchanger E6 heat exchange cooling again after the decompression, presses gases such as the H2, the CO that flash off dissolving in the flash column T2 hypomere and portion C O2 in being fed in.Equally, the methyl alcohol rich solution 6 of the not sulfur-bearing that comes out from absorption tower T1 hypomere is through the 4th heat exchanger E4, the 5th heat exchanger E5 heat exchange cooling again after the decompression, presses gases such as the H2, the CO that flash off dissolving in the flash column T2 epimere and portion C O2 in sending into.Two parts flash gas 7 turns back in the unstripped gas after recycle gas compressor C1 supercharging after being come out by middle pressure flash column T2.
Send into CO after sulfur-bearing methyl alcohol 8 decompressions of coming out at the bottom of the middle pressure flash column T2 tower
2Product tower T3 midsection flashes off the CO2 of dissolving, simultaneously Rong Xie H2S also the part flash distillation come out.The not sulfur-bearing methanol solution 9 of therefrom pressing flash column T2 epimere to come out enters CO
2Product tower T3 cat head flashes off the CO of dissolving
2Gas.
From CO
2 Liquid phase part 10 parts that product tower T3 epimere comes out are got back to CO
2Product tower T3 midsection washing sulfurous gas, another part is sent into reabsorber T4 top of tower.CO
2Product tower T3 cat head obtains CO
2Purified gas, this CO2 purified gas leave system after by the first heat exchanger E1 heat exchange.
CO
2The liquid 11 that pars infrasegmentalis comes out on the product tower T3 tower is sent into pars infrasegmentalis on the reabsorber T4 tower, further flashes off partly soluble CO2, simultaneously Rong Xie H2S also the part flash distillation come out.
Reabsorber T4 cat head is with the not methanol solution washing of sulfur-bearing, to absorb the sulfide in the gas.Reabsorber T4 cat head obtains the not tail gas 12 of sulfur-bearing, and the tail gas 12 of sulfur-bearing does not enter tail gas washing tower T7 hypomere after the first heat exchanger E1 heat exchange.In tail gas washing tower T7, tail gas is washed, reclaim methyl alcohol wherein with desalted water.Tail gas after washing leaves system.
After pars infrasegmentalis came out the solution 13 usefulness second pump P2 pressurization of sulfur-bearing on the reabsorber T4 tower, after the 7th heat exchanger E7, the 3rd heat exchanger E3 reclaimed cold, gas-liquid two-phase 14 entered knockout drum 15 and carries out gas-liquid separation.Gas 16 after knockout drum 15 separates enters CO
2At the bottom of the product tower T3 tower, liquid 17 is pumped into by the first pump P1 and enters CO after the 4th heat exchanger E4 further reclaims cold
2At the bottom of the product tower T3 tower, flash off dissolved gases.
CO
2The methanol solution 18 that comes out at the bottom of the product tower T3 enters reabsorber T4 tower hypomere, obtaining the lower rich sulphur methanol solution 19 of CO2 content after carrying with nitrogen gas is gone out by reabsorber T4 bottom, after these richness sulphur methanol solution 18 usefulness the 3rd pump P3 boosts, by after the 8th heat exchanger E8 and the tenth heat exchanger E10 and poor methanol 20 heat exchange that at the bottom of hot regenerator T5 tower, come, enter hot regenerator T5 tower and carry out heat and regenerate.
Obtain poor methanol 20 at the bottom of the hot regenerator T5 tower, cat head obtains being rich in the sour gas 21 of sulphur.The sour gas 21 that is rich in sulphur is after the 11 heat exchanger E11 cooling, sending into return tank 22 refluxes, the liquid 23 that forms that refluxes is sent into hot regenerator T5 epimere after the 7th pump P7 pressurization, the gas 24 that backflow forms is after the 12 heat exchanger E12 cooling, send into sour gas knockout drum 25 and carry out gas-liquid separation, the sour gas part that sour gas knockout drum 25 separates goes out device, and another part sour gas 26 is back to reabsorber T4 hypomere.Pass through the poor methanol 20 in the 13 heat exchanger E13 usefulness Steam Heating rectifying recycle-water at the bottom of the hot regenerator T5 tower.
By the poor methanol 20 that comes out at the bottom of the hot regenerator T5 tower, after boosting by the 4th pump P4, part 20a is after the tenth heat exchanger E10, the 9th heat exchanger E9, the 8th heat exchanger E8 and the 7th heat exchanger E7 heat exchange cooling, delivering to T1 top, absorption tower uses poor methanol, another part 20b to send into methyl alcohol water tower T6 top of tower as phegma as absorbing.
Methanol aqueous solution 27 from tail gas washing tower T7 tower bottom is by the 6th pump P6 pressurization and after the 15 heat exchanger E15 cooling, methanol solution 27 is sent into methyl alcohol water tower T6 middle part, after the water 28 that the methanol content that comes out in methyl alcohol water tower T6 bottom reaches discharge standard is pumped into the 15 heat exchanger E15 and is reclaimed heat by the 5th pump P5, direct discharger.
Methyl alcohol water tower T6 bottom is by the methyl alcohol in the 14 heat exchanger E14 usefulness Steam Heating rectifying recycle-water.
There is following deficiency in said apparatus:
(1) heat-exchange network complexity, interdependence is big between the logistics, and the whole device driving time is long, the stable difficulty of control.
(2) absorbing with methyl alcohol all is the poor methanol of heat regeneration, regeneration energy consumption height.
(3) adopt many wound tube heat exchangers, for example the multiple flow first heat exchanger E1, the 3rd heat exchanger E3, the 4th heat exchanger E4 must adopt wound tube heat exchanger; The 7th heat exchanger E7, the 8th heat exchanger E8, the 9th heat exchanger E9 adopt wound tube heat exchanger, and heat balance influences each other greatly between the heat exchanger, and investment is big.
The utility model content
Technical problem to be solved in the utility model is to provide a kind of energy-efficient shunting energy-saving low temperature washing device for methanol, the energy-saving low temperature washing device for methanol of this shunting reduces the complexity of flow process and the relevance of multiple flow wound tube heat exchanger material and heat greatly, economy system is driven the time, cut down the consumption of energy, overcome the problem that exists in the existing low-temp methanol washing process.
Technical problem to be solved in the utility model can realize by following technical solution:
The energy-saving low temperature washing device for methanol of shunting comprises that absorption tower T1, middle pressure flash column T2, reabsorber T4, hot regenerator T5, methyl alcohol water tower T6, tail gas washing tower T7, some heat exchangers, pump, recycle compressor C1 form; It is characterized in that, flash zone is set at described reabsorber T4 epimere; Directly being fed in, the sulfur-bearing methyl alcohol rich solution that comes out at the bottom of the T1 tower of absorption tower presses the H that flashes off dissolving in the flash column T2 hypomere
2, CO and portion C O
2Gas; Directly sending into, the methyl alcohol rich solution part of the not sulfur-bearing that comes out from absorption tower T1 hypomere press flash column T2 epimere to flash off the H of dissolving
2, CO and portion C O
2Gas, another part returns absorption tower T1 hypomere by after the 3rd heat exchanger E3 heat exchange; Two parts flash gas by the rich sulphur methanol wash of coming with the 3rd pump P3 pump after, after coming out by middle pressure flash column T2 hypomere top, after recycle gas compressor C1 supercharging, turn back in the unstripped gas; Directly send into reabsorber T4 hypomere after the middle sulfur-bearing methyl alcohol decompression of pressing flash column T2 hypomere to come out, flash off the CO of dissolving
2, Rong Xie H simultaneously
2S also part flash distillation comes out; Therefrom press not sulfur-bearing methanol solution that flash column T2 epimere comes out after the 4th heat exchanger E4 and the 5th heat exchanger E5 heat exchange, enter the flash zone of reabsorber T4 epimere, flash off the CO of dissolving
2Gas; Get back to reabsorber T4 hypomere washing sulfurous gas from the half poor methanol liquid part that the flash zone of reabsorber T4 comes out, another part enters absorption tower T1 after the first pump P1 boosts, use semi lean solution as absorbing; The flash zone of absorption tower T4 obtains CO
2Product gas, this CO
2Product gas leaves system after by the first heat exchanger E1 heat exchange; Reabsorber T4 tower hypomere middle part come out the solution of sulfur-bearing with second pump P2 pressurization after, behind the 7th heat exchanger E7, the 4th heat exchanger E4, the 3rd heat exchanger E3 recovery cold, return the hypomere that enters reabsorber T4, flash off dissolved gases; The CO that reabsorber T4 comes out the bottom
2After the rich sulphur methanol solution that content is lower boosts with the 3rd pump P3, press flash column T2 hypomere during a part is sent into, be used for absorbing the CO that pressure flashes off
2, another part carries out heat and regenerates by entering hot regenerator T5 after the 8th heat exchanger E8 and the tenth heat exchanger E10 and the poor methanol heat exchange that comes from hot regenerator T5 bottom, obtains poor methanol at the bottom of the tower of hot regenerator T5, and cat head obtains being rich in the sour gas of sulphur; After poor methanol comes out at the bottom of the tower of hot regenerator T5, after boosting by the 4th pump P4, delivering to T1 top, absorption tower after a part the tenth heat exchanger E10, the 9th heat exchanger E9, the 8th heat exchanger E8, poor methanol cooler E16, the 7th heat exchanger E7 heat exchange cooling uses poor methanol, another part to send into methyl alcohol water tower T6 top of tower as phegma as absorbing.
In the utility model, described the 3rd heat exchanger E3 and the 4th heat exchanger E4 are shell-and-tube heat exchanger.
Unstripped gas of the present utility model can be washed by the unstripped gas scrubbing tower earlier, enters absorption tower T1 after the washing.
Owing to adopted technical scheme as above, the utility model compared with prior art has following advantage:
(1) do not establish CO
2Product tower T3 tower is provided with CO on reabsorber T4 tower top
2Flash zone is guaranteeing CO
2Under the qualified prerequisite of product gas, reduce the complexity of flow process, reduce investment.
(2) the half poor methanol liquid that is provided with from reabsorber T4 epimere advances split-flow rectisol (acid gas removal) new technological process that absorption tower T1 is used to absorb, reduce the consumption of absorption tower T1 poor methanol, and then can reduce the energy consumption that hot regenerator T5 carries out heat regeneration, save gas and carry nitrogen use level, the low level cold of using when saving the cooling of steam consumption quantity and poor methanol.
(3) flow process of pressing the flash gas of flash column T2 tower to wash with the rich sulphur methanol solution of reabsorber T4 tower bottom centering is set.Use from the CO in the rich sulphur methanol solution washing flash gas of reabsorber T4 tower bottom
2, can effectively reduce the CO in the circulating air
2Amount, thus the tolerance that absorption tower T1 absorbs methanol usage and advances recycle gas compressor C1, saveall energy consumption reduced.
(4) change the 3rd heat exchanger E3 and the 4th heat exchanger E4 into shell-and-tube heat exchanger by original wound tube heat exchanger, simultaneously the 3rd heat exchanger E3 and the 4th heat exchanger E4 position are adjusted, satisfying under the prerequisite of cold balancing, can effectively reduce the investment of device.
(5) behind the 8th heat exchanger E8 of poor/rich methanol, poor methanol cooler E16 is set.This poor methanol cooler E16 only uses when driving, and can effectively reduce the used time of system cools when driving, and can remedy the phenomenon of the cold deficiency that exists when driving, thereby shortens the driving time.
(6) by the unstripped gas scrubbing tower is set, washing removes the NH in the unstripped gas
3, impurity such as HCN, avoid the sour gas condensation-crystallization, and the equipment and pipeline corrosion of high temperature position.
(7) CO is set
2Washing flow.The CO that bears again
2Gas can gentlely be carried tail gas and advance tail gas washing tower T7 together, reduces the methyl alcohol loss, avoids environmental pollution.
The present invention is applicable in coal and the devices such as derivative, natural gas preparing synthetic gas and then production ammonia, methyl alcohol thereof to reclaim CO
2, desulfurization and organic impurities technology.After adopting the present invention, low temperature washing device for methanol has tangible investment reduction, energy consumption reduction, process simplification, the advantage rapidly of driving.Adopted semi lean solution to advance shunting flow process configuration mode that the absorption tower is used to absorb and with rich sulphur methanol solution to the flow process configuration mode that flash gas washs, saved the freezing energy consumption and the heat regeneration energy consumption of device; Cancel T3 tower and E3, E4 wound tube heat exchanger, simplified flow process, saved investment; Set up the poor methanol cooler, the driving time shortens greatly.
Description of drawings
Fig. 1 is present low temperature washing device for methanol schematic flow sheet.
Fig. 2 is the schematic flow sheet of the energy-saving low temperature washing device for methanol of the utility model shunting.
The specific embodiment
The energy-saving low temperature washing device for methanol of shunting as shown in Figure 2 comprises that absorption tower T1, middle pressure flash column T2, reabsorber T4, hot regenerator T5, methyl alcohol water tower T6, tail gas washing tower T7, some heat exchangers, pump, recycle compressor C1 form; Unstripped gas is washed by unstripped gas scrubbing tower (not shown) earlier, and mix with circulating air the washing back, enters the hypomere of absorption tower T1 after first heat exchanger E1 cooling; The epimere of absorption tower T1 is CO
2Absorber portion, hypomere are H
2The S absorber portion.
Unstripped gas wherein CO behind the T1 of absorption tower
2Effectively removed with sulfide impurities, the purified gas that is come out by T1 top, absorption tower goes out device after the heat exchange in the first heat exchanger E1.
Absorption tower T1 epimere connects the second heat exchanger E2, and the methanol gas that absorption tower T1 epimere comes out is carried out the condensation recovery, and the methanol liquid of recovery is back to absorption tower T1 epimere again.
Absorbed H
2Behind S and the COS, directly being fed in, the sulfur-bearing methyl alcohol rich solution 5 that comes out at the bottom of the T1 tower of absorption tower presses the H that flashes off dissolving in the flash column T2 hypomere
2, CO and portion C O
2Gas; Directly sending into, the methyl alcohol rich solution part of the not sulfur-bearing that comes out from absorption tower T1 hypomere press flash column T2 epimere to flash off the H of dissolving
2, CO and portion C O
2Gas, another part returns absorption tower T1 hypomere by after the 3rd heat exchanger E3 heat exchange; Two parts flash gas 7 by rich sulphur methyl alcohol 19 washings that come with the 3rd pump P3 pump after, after coming out by middle pressure flash column T2 hypomere top, after recycle gas compressor C1 supercharging, turn back in the unstripped gas.
Send into reabsorber T4 hypomere after middle sulfur-bearing methyl alcohol 8 decompressions of pressing flash column T2 hypomere to come out, flash off the CO of dissolving
2, Rong Xie H simultaneously
2S also part flash distillation comes out.Therefrom press not sulfur-bearing methanol solution 9 that flash column T2 epimere comes out after the 4th heat exchanger E4 and the 5th heat exchanger E5 heat exchange, enter the flash zone 30 of reabsorber T4, flash off the CO of dissolving
2Gas.
Get back to reabsorber T4 hypomere washing sulfurous gas from half poor methanol liquid, 29 parts that the flash zone 30 of reabsorber T4 comes out, another part enters absorption tower T1 after the first pump P1 boosts, as the absorption semi lean solution.The flash zone 30 of reabsorber T4 obtains CO
2Product gas, this CO2 product gas leave system after by the first heat exchanger E1 heat exchange; Reabsorber T4 hypomere adopts nitrogen gas to carry, hypomere top obtains the not tail gas 12 of sulfur-bearing, the tail gas 12 of sulfur-bearing does not enter tail gas washing tower T7 hypomere after the first heat exchanger E1 heat exchange, in tail gas washing tower T7, tail gas is washed with desalted water, reclaim methyl alcohol wherein, the tail gas after washing leaves system.
Reabsorber T4 tower hypomere middle part comes out behind the 7th heat exchanger E7, the 4th heat exchanger E4, the 3rd heat exchanger E3 recovery cold, to return the hypomere that enters reabsorber T4 after solution 13 usefulness the pump P2 pressurization of sulfur-bearing, flashes off dissolved gases.
The CO that reabsorber T4 comes out the bottom
2After the rich sulphur methanol solution that content is lower boosts with the P3 pump, press flash column T2 hypomere during a part is sent into, be used for absorbing the CO that pressure flashes off
2, another part carries out heat and regenerates by entering hot regenerator T5 tower after the 8th heat exchanger E8 and the tenth heat exchanger E10 and poor methanol 20 heat exchange that come from hot regenerator T5 bottom, obtains poor methanol 20 at the bottom of the tower of hot regenerator T5, and cat head obtains being rich in the sour gas 21 of sulphur.
After poor methanol 20 comes out at the bottom of the tower of hot regenerator T5, after boosting by the 4th pump P4, part 20a delivers to T1 top, absorption tower and uses poor methanol, another part 21b to send into methyl alcohol water tower T6 top of tower as phegma as absorbing after the tenth heat exchanger E10, the 9th heat exchanger E9, the 8th heat exchanger E8, poor methanol cooler E16, the 7th heat exchanger E7 heat exchange cooling.
The sour gas 21 that is rich in sulphur is after the 11 heat exchanger E11 cooling, sending into return tank 22 refluxes, the liquid 23 that forms that refluxes is sent into hot regenerator T5 epimere after pump P7 pressurization, the gas 24 that backflow forms is after the 12 heat exchanger E12 cooling, send into sour gas knockout drum 25 and carry out gas-liquid separation, the sour gas part that sour gas knockout drum 25 separates goes out device, and another part 26 is back to reabsorber T4 hypomere.
Produce poor methanol 20 by the 13 heat exchanger E13 with Steam Heating rectifying at the bottom of the hot regenerator T5 tower; Methanol aqueous solution 27 from tail gas washing tower T7 tower bottom is by pump P6 pressurization and after the 15 heat exchanger E15 heats up, methanol solution is sent into methyl alcohol water tower T6 middle part, the water 28 that the methanol content that comes out in methyl alcohol water tower T6 bottom reaches discharge standard through the 5th pump P5 boost, after the 15 heat exchanger E15 reclaims heat, direct discharger; Methyl alcohol water tower T6 bottom is by the methyl alcohol in the 14 heat exchanger E14 usefulness Steam Heating rectifying recycle-water.
Above-mentioned the 3rd heat exchanger E3 and the 4th heat exchanger E4 are shell-and-tube heat exchanger.
Present embodiment adopts the shunting washing flow: promptly half poor methanol liquid 29 is used for main the absorption in the middle part of advancing absorption tower T1, and a part of poor methanol 20a enters T1 top, absorption tower and is used for fine purifiation, heat regeneration energy consumption and cold consumption decline; Shunt the flow process that 19 pairs of flash gas of rich sulphur methanol solution wash, the recycle compressor power consumption descends.Behind the 8th heat exchanger E8 of poor/rich methanol, poor methanol cooler E16 is set.This poor methanol cooler E16 only uses when driving, and can effectively reduce the used time of system cools when driving, and can remedy the phenomenon of the cold deficiency that exists when driving, thereby shortens the driving time.
For raw gas flow is 420000Nm3/h, pressure 5.0～6.0MPa (G), and the present invention is 5.8Gcal/h-40 ℃ of cold consumption, and heat regeneration steam consumption is 21t/h, and the driving time shortens.And prior art is 6.1Gcal/h-40 ℃ of cold consumption, and the used quantity of steam of heat regeneration is 22t/h, and the driving time is long.Comparing result shows, adopts the flow process of embodiment obviously to reduce investment, and flow process is simple, the control simple and stable, and steam and cold consumption reduce, and aspect shortening the driving time greater advantage are being arranged.
Claims (3)
1. the energy-saving low temperature washing device for methanol of shunting comprises absorption tower (T1), middle pressure flash column (T2), reabsorber (T4), hot regenerator (T5), methyl alcohol water tower (T6), tail gas washing tower (T7), some heat exchangers, pump, recycle compressor (C1) composition; It is characterized in that, flash zone is set at described reabsorber (T4) epimere; Press in flash column (T2) hypomere the sulfur-bearing methyl alcohol rich solution that comes out at the bottom of the tower of absorption tower (T1) directly is fed in; Press flash column (T2) epimere the methyl alcohol rich solution part of the not sulfur-bearing that comes out from absorption tower (T1) hypomere is directly sent into, another part returns absorption tower (T1) hypomere by after the 3rd heat exchanger (E3) heat exchange; Two parts flash gas by the rich sulphur methanol wash of coming with the 3rd pump (P3) pump after, after coming out by middle pressure flash column (T2) hypomere top, after recycle gas compressor (C1) supercharging, turn back in the unstripped gas; Directly send into reabsorber (T4) hypomere after the middle sulfur-bearing methyl alcohol decompression of pressing flash column (T2) hypomere to come out; Therefrom press not sulfur-bearing methanol solution that flash column (T2) epimere comes out after the 4th heat exchanger (E4) and the 5th heat exchanger (E5) heat exchange, enter the flash zone of reabsorber (T4) epimere; Get back to reabsorber (T4) hypomere washing sulfurous gas from the half poor methanol liquid part that the flash zone of reabsorber (T4) comes out, another part enters absorption tower (T1) after first pump (P1) boosts, use semi lean solution as absorbing; The flash zone of reabsorber (T4) obtains CO
2Product gas, this CO
2Product gas leaves system after by first heat exchanger (E1) heat exchange; Reabsorber (T4) tower hypomere middle part come out the solution of sulfur-bearing with second pump (P2) pressurization after, behind the 7th heat exchanger (E7), the 4th heat exchanger (E4), the 3rd heat exchanger (E3) recovery cold, return the hypomere that enters reabsorber (T4); The CO that comes out in reabsorber (T4) bottom
2After the rich sulphur methanol solution that content is lower boosts with the 3rd pump (P3), during sending into, a part presses flash column (T2) hypomere, another part is by the 8th heat exchanger (E8) and the tenth heat exchanger (E10) and enter hot regenerator (T5) after the next poor methanol heat exchange in hot regenerator (T5) bottom, obtain poor methanol at the bottom of the tower of hot regenerator (T5), cat head obtains being rich in the sour gas of sulphur; After poor methanol comes out at the bottom of the tower of hot regenerator (T5), after boosting by the 4th pump (P4), delivering to top, absorption tower (T1) after a part the tenth heat exchanger (E10), the 9th heat exchanger (E9), the 8th heat exchanger (E8), poor methanol cooler (E16), the 7th heat exchanger (E7) the heat exchange cooling uses poor methanol, another part to send into methyl alcohol water tower (T6) top of tower as phegma as absorbing.
2. the energy-saving low temperature washing device for methanol of shunting as claimed in claim 1 is characterized in that, described the 3rd heat exchanger (E3) and the 4th heat exchanger (E4) are shell-and-tube heat exchanger.
3. the energy-saving low temperature washing device for methanol of shunting as claimed in claim 1 is characterized in that, unstripped gas enters absorption tower (T1) after being washed by the unstripped gas scrubbing tower.
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| CN2009200733204U CN201419074Y (en) | 2009-06-03 | 2009-06-03 | Shunting type energy-saving scrubbing unit using low temperature methanol |
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| CN2009200733204U CN201419074Y (en) | 2009-06-03 | 2009-06-03 | Shunting type energy-saving scrubbing unit using low temperature methanol |
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| WO2012009965A1 (en) * | 2010-07-23 | 2012-01-26 | 镇海石化建安工程有限公司 | Cooler for feed gas of low-temperature methanol washing |
| CN102806000A (en) * | 2012-09-05 | 2012-12-05 | 大连佳纯气体净化技术开发有限公司 | Energy-saving one-step rectisol method |
| CN104140852A (en) * | 2013-11-22 | 2014-11-12 | 上海国际化建工程咨询公司 | Device and method for treating low temperature methanol washing ammonium crystallization and purifying barren solution methanol |
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2009
- 2009-06-03 CN CN2009200733204U patent/CN201419074Y/en not_active Expired - Lifetime
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| CN106512649B (en) * | 2016-11-09 | 2019-01-11 | 中石化宁波工程有限公司 | A kind of sour gas re-absorption technology of mating coal water slurry gasification |
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| CN110791327A (en) * | 2019-11-13 | 2020-02-14 | 中建安装集团有限公司 | Device and process for deeply removing purified gas sulfide of low-temperature methanol washing system |
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