CN203139876U - Low-temperature methanol washing process device - Google Patents

Low-temperature methanol washing process device Download PDF

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Publication number
CN203139876U
CN203139876U CN2012207311489U CN201220731148U CN203139876U CN 203139876 U CN203139876 U CN 203139876U CN 2012207311489 U CN2012207311489 U CN 2012207311489U CN 201220731148 U CN201220731148 U CN 201220731148U CN 203139876 U CN203139876 U CN 203139876U
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methanol
tower
cooler
methyl alcohol
heat exchanger
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CN2012207311489U
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郭欣
李士雨
李金来
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ENN Science and Technology Development Co Ltd
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ENN Science and Technology Development Co Ltd
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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
    • 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
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

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Abstract

The utility model relates to a low-temperature methanol washing process device which comprises a methanol washing tower, an H2S evaporating tower, and a methanol thermal regeneration tower, wherein the methanol washing tower sequentially comprises a fine washing section, a CO2 main absorption section and a desulfurization section from top to bottom; and an effluent of the CO2 main absorption section flows through a circulating methanol cooler and then flows into a heat exchanger, so that the effluent of the CO2 main absorption section performs heat exchange with a methanol-enriched solution at the middle part of the H2S evaporating tower. According to the low-temperature methanol washing process device, a heat exchange area of a No. 2 poor methanol cooler connected to the bottom of the H2S evaporating tower, and a heat exchange area of a methanol water cooler connected to the bottom of the methanol thermal regeneration tower are increased. When a low-temperature methanol washing process is performed by the low-temperature methanol washing process device, the cooling water quantity is increased by 22.73%, but the ammonia cooling quantity is saved by 10.2% compared with that of the original process; the cost of cooling water is far below that of ammonia cooling, so that the low-temperature methanol washing process device has the advantages that the operating cost of an enterprise can be remarkably reduced; and an existing energy-saving effect can be achieved.

Description

A kind of low-temp methanol washing process device
Technical field
The utility model relates to gaseous mixture purification techniques field, and referring more particularly to coal, petroleum coke or residual oil is that raw material is produced technologies such as synthetic ammonia, synthesizing methanol, industrial hydrogen production, is specifically related to a kind of CO in the synthesis gas that removes 2With COS, H 2The low-temp methanol washing process device of acid gas such as S.
Background technology
Low-temperature rectisol is the acid gas purifying technology that the fifties in last century Germany Linde Co and LURGI develop jointly, is widely used in the technologies such as synthetic ammonia, synthesizing methanol.Domestic Dalian University of Technology just was engaged in the low temperature washing device for methanol sunykatuib analysis since nineteen eighty-three and optimizes research work, had successfully developed low temperature washing device for methanol simulation system (RPS, Rectiosl Process Simulator) in 1993.
The research background is 600,000 tons/coal gasification methanol technics processed.Existing low temperature washing device for methanol comprises methanol wash tower, CO 2Analytic Tower, H 2S concentration tower, the hot regenerator of methyl alcohol, methanol knockout tower, washing tail gas system.The methanol wash tower is according to the different solubility of sour gas in low-temp methanol, removes COS, H in the synthesis gas 2S, CO 2, the methyl alcohol rich solution that has absorbed sour gas is regenerated through modes such as decompression, air lift, heating.
As shown in Figure 1, existing low-temp methanol washing process is as follows:
The 5.4MPa that the transformation into itself comes, 40 ℃ conversion gas 1 converge with the circulating air 2 that flashed vapour compressor C3001 sends here, for preventing that conversion gas is cooled to the icing phenomenon of appearance below freezing, spray into the poor methanol liquid 23 of 1303kg/h, be cooled to-20.15 ℃ through unstripped gas heat exchanger E3001 and purified gas 4, carbon dioxide 5, tail gas 6 heat exchange then, after separator V3001 isolated methanol aqueous solution, dry unstripped gas entered methanol wash tower T3001 again.
Methanol wash tower T3001 divides two parts up and down, and lower tower section is mainly used in desulfurization, and upper tower section can be divided into three sections again: the top section is fine wash sections, absorbs a small amount of CO that remains in the gas with-54.99 ℃, the poor methanol stream of 358906kg/h strands 24 2And H 2S is to guarantee CO in the downstream purification gas 4 2≤ 3%, H 2S≤0.1ppm; Middle two sections is CO 2Absorber portion is used the fine wash sections cleaning solution 31 after recycle methanol cooler E3006 heat exchange, enters CO under-35.75 ℃ 2Absorber portion absorbs the CO in the gas 2CO 2The outflow liquid 30 of absorber portion is back to CO after 3# methyl alcohol chiller E3005, recycle methanol cooler E3006 cooling 2Absorber portion absorbs the CO in the gas 2About 52% methyl alcohol rich solution 25 takes out from last tower bottom tower tray, in methyl alcohol cooler E3017 and purified gas 4 heat exchange, be cooled to-31.65 ℃ through 2# methyl alcohol chiller E3004 again, enter 2# circulating air flash tank V3003 through reducing to 1850kPa, make the most of H that is dissolved in the methanol solution 2Steam.
Only need go up tower during following tower desulfurization and absorb CO 2The part methanol solution, its amount is about 48% of total amount, the methanol solution 26 that comprises whole sulphur after tower washs down flows out from methanol wash tower T3001 tower bottom, respectively in methyl alcohol heat exchanger E3007,1# methyl alcohol chiller E3003 heat exchange cooling, after being decompressed to 1850kPa, enter 1# circulating air flash tank V3002, make the most of H that is dissolved in the methanol solution 2Flash distillation is come out.The H that 1# circulating air flash tank V3002 and 2# circulating air flash tank V3003 flash distillation are come out 2By recycle gas compressor C3001, pressure-raising is cooled to-40 ℃ to the compressed machine water cooler of 5560kPa E3002, sends back to recycling on the unstripped gas pipeline of entrance.
That draws from 2# circulating air flash tank V3003 bottom contains CO 2The methanol solution 32 of sulfur-bearing not, through throttling expansion, pressure drops to 0.29MPa, enters CO 2Analytic Tower T3002 top of tower flashes off most of CO 2Gas, a part is as CO 2The phegma 37 on Analytic Tower T3002 top, a part is as H 2The phegma 36 on S concentration tower T3003 top.
The sulfur-bearing and the CO that draw from 1# circulating air flash tank V3002 bottom 2Methanol solution 33, through throttling expansion, pressure drops to 0.35MPa, enters CO 2The 8th column plate place, Analytic Tower T3002 middle part, at this, portion C O 2And H 2S parses from methanol solution, and methanol solution 38 is sent into H 2S concentration tower T3003 flashes off portion C O 2And H 2S obtains rich methanol liquid 34 by pressure-raising, enter methyl alcohol flash tank V3007 and separate through 3# poor methanol cooler E3008, recycle methanol cooler E3006 successively, liquid part 35 is gone methyl alcohol heat exchanger E3007 heat exchange through pressurization again, and flashed vapour 13, liquid part 35 enter CO simultaneously then 2Tower under the Analytic Tower T3002 tower is raised to-28.88 ℃ by-63.13 ℃ because advancing tower methanol solution temperature, along with the rising of temperature, CO 2Solubility in methyl alcohol reduces, at CO 2Tower parses a large amount of CO under the Analytic Tower T3002 2From CO 2The methanol solution 39 of Analytic Tower T3002 bottom enters H 2Behind the S concentration tower T3003 tower middle part, further gone out CO by low-pressure nitrogen 15 air lifts 2, this part CO 2In company with air lift nitrogen and CO 2The carbon dioxide 5 of Analytic Tower T3002 tower overhead gas reclaims cold through unstripped gas heat exchanger E3001 together.Crouse's hydrogenation tail gas 14 enters H 2At the bottom of the S concentration tower T3003 tower.H 2S concentration tower T3003 bottom methanol solution 41 temperature be-43.46 ℃, through pressurizeing, go into 2# poor methanol cooler E3009 successively and 1# poor methanol cooler E3010 temperature is elevated to 87.4 ℃, enter then on the 26th block of column plate of the hot regenerator T3004 of methyl alcohol.Be dissolved in the whole H in the methanol solution 2S, CO 2Be reproduced the methanol steam air lift that tower reboiler E3011 heating produces, simultaneously methanol steam 22 air lifts that distilled out by methanol-water/knockout tower T3005 cat head.The sour gas that heating is come out is carried the sour gas/methyl alcohol 16 of part methanol steam secretly and is drawn by cat head, after sour gas water cooler E3012 cooling, most of methanol vapor is condensed, isolate methanol condensed liquid 42 as phegma through backflow flow container V3006, send back to the hot regenerator T3004 of methyl alcohol top of tower, leave the rich sulphur steam 17 at backflow flow container V3006 top, at H 2By precooling, in the sour gas chiller E3013 of the hot regenerator of methyl alcohol, further cool off then among the S cut heat exchanger E3014.At this, nearly all methanol steam all is condensed, and separates through sour gas separator V3005 again, and condensate liquid 40 is delivered to H 2S concentration tower T3003 tower bottom is handled, and sour gas 18 parts are circulated to H 2On the 25th block of column plate of S concentration tower T3003, part is through H 2S cut heat exchanger E3014 delivers to out-of-bounds sulfur recovery after reclaiming cold.
Take out regenerated methanol 43 from the hot regenerator T3004 of methyl alcohol bottom, deliver to methyl alcohol collecting tank V3004 after in 1# poor methanol cooler E3010, being cooled, be pressurized to 6.5MPa then, after methanol-water cooler E3018 cooling, except a small amount of conduct spray methyl alcohol, all the other deliver to methanol wash tower T3001 top of tower as the fine wash sections cleaning solution after 2# poor methanol cooler E3009,3# poor methanol cooler E3008 are cooled to-54.99 ℃.
The methanol of coming from separator V3001 27 among methanol knockout tower feed heater E3016 with by methyl alcohol at the bottom of the hot regenerator T3004 tower through cooled poor methanol 45 heat exchange, temperature rises on 60.80 ℃ of the 21st block of column plates that enter methanol knockout tower T3005 tower through methanol knockout tower charging separator V3008, simultaneously, after washings 51 pressurizations behind the washing tail gas, in water-to-water heat exchanger E3019, heat up and deliver on the 13rd block of column plate of methanol-water/knockout tower T3005 tower, the distillation of their fellowships.Tower bottom steam is produced by methanol knockout tower reboiler E3015 heat exchange, methanol steam is directly sent into the hot regenerator T3004 of methyl alcohol after 51 column plate distillations, and delivers to methanol-water/knockout tower T3005 top as phegma by the cooled poor methanol 45 of methanol-water/knockout tower feed heater E3016.Waste water 49 at the bottom of the tower is disposed to Waste Water Treatment reclaim heat in water-to-water heat exchanger E3019 after, and its discharge capacity is 2277kg/h.
Be exothermic process in the liquid because gas is dissolved in, therefore the solubility along with sour gas in the low-temp methanol increases, and the temperature of methyl alcohol raises gradually, in order to guarantee methyl alcohol to the absorbability of sour gas, must provide cold in the external world.Keeping that low temperature washing device for methanol moves at low temperatures mainly is to replenish cold in the system by ice maker.
The utility model content
The purpose of this utility model is at the deficiencies in the prior art, and a kind of low-temp methanol washing process device that can effectively cut down the consumption of energy is provided.
For reaching this purpose, the utility model by the following technical solutions:
A kind of low-temp methanol washing process device, described device comprises methanol wash tower, H 2S concentration tower, the hot regenerator of methyl alcohol, described methanol wash tower is followed successively by fine wash sections, CO from top to bottom 2Main absorber portion and desulfurization section, described CO 2The outflow liquid of the main absorber portion recycle methanol cooler inflow heat exchanger of flowing through makes CO 2Outflow liquid and the H of main absorber portion 2The rich methanol liquid heat exchange at S concentration tower middle part.
Concrete annexation is: a kind of low-temp methanol washing process device, described device comprises methanol wash tower, CO 2Analytic Tower, H 2S concentration tower, the hot regenerator of methyl alcohol and methanol knockout tower, described methanol wash tower is followed successively by fine wash sections, CO from top to bottom 2Main absorber portion and desulfurization section, described CO 2The outflow liquid pipeline of main absorber portion connects heat exchanger after connecting the recycle methanol cooler again, described heat exchanger while and H 2The rich methanol liquid pipeline at S concentration tower middle part connects.
Methanol wash tower described in the utility model utilizes the difference of gas solubility in low-temp methanol, and sour gas is optionally absorbed.
Described CO 2Analytic Tower is dissolved in CO in the low-temp methanol by reducing pressure, making 2Parse.
Described H 2The S concentration tower passes through modes such as air lift, decompression with CO 2Resolve the H that parses 2S gas absorbs again with poor methanol liquid, makes H 2S is concentrated.
The hot regenerator of described methyl alcohol be by the heating mode with H 2S resolves, and makes methyl alcohol obtain regeneration.
Described methanol knockout tower, the moisture in the system can influence operation, thereby methyl alcohol is separated with water.
Described recycle methanol cooler, absorption process are exothermic process, and in order to guarantee assimilation effect, the cold when the methyl alcohol utilization is resolved cools off.
Described CO 2The outflow liquid of the main absorber portion 3# methyl alcohol chiller of before the recycle methanol cooler of flowing through, flowing through earlier.Specifically, described CO 2The outflow liquid pipeline of main absorber portion connects heat exchanger after connecting 3# methyl alcohol chiller, recycle methanol cooler again.
3# methyl alcohol chiller described in the utility model utilizes liquefied ammonia as cold public work cooling methyl alcohol.
The utility model is with respect to original low-temp methanol washing process device, at methanol wash tower CO 2The outflow liquid pipeline of main absorber portion increases heat exchanger after connecting 3# methyl alcohol chiller, recycle methanol cooler again, in described heat exchanger, and CO 2The outflow liquid of main absorber portion with from H 2In the middle part of the S concentration tower, through the further heat exchange of rich methanol liquid of 3# poor methanol cooler cooling, cooling can more take full advantage of H 2The cold of the rich methanol liquid at S concentration tower middle part makes CO 2The temperature of the outflow liquid of main absorber portion reduces, and therefore, in the 3# methyl alcohol chiller that connects before, can significantly reduce the colod-application amount of ammonia, makes phegma needn't be cooled to the temperature of original technology through 3# methyl alcohol chiller the time, and in the heat exchanger of follow-up increase, utilizes H 2The cold of the rich methanol liquid at S concentration tower middle part makes the temperature of phegma drop to suitable temperature and gets final product.The utility model can significantly reduce the colod-application amount of ammonia of whole technology by increasing a heat exchanger, saves cost.The concrete connected mode of the heat exchanger that the utility model is newly-increased is: the tube side entrance of described heat exchanger and the CO of recycle methanol cooler 2Main absorber portion flow export is communicated with, tube side outlet and the CO of described heat exchanger 2Main absorber portion entrance is communicated with; The shell side entrance of described heat exchanger is communicated with the shell side outlet of 3# poor methanol cooler, and the shell side outlet of described heat exchanger is communicated with the shell side entrance of recycle methanol cooler.
Described H 2S concentration tower bottom is connected with 2# poor methanol cooler.In described 2# poor methanol cooler, poor methanol utilizes H 2S concentration tower tower bottom flow thigh cools off.
The utility model is with described H 2The heat exchange area of the 2# poor methanol cooler that S concentration tower bottom connects increases.Described H 2The heat exchange area of the 2# poor methanol cooler that S concentration tower bottom connects increases 16.58%.
The hot regenerator of described methyl alcohol bottom is connected with the methanol-water cooler.Take out regenerated methanol from the hot regenerator of methyl alcohol bottom, after cooling, deliver to the methyl alcohol collecting tank, pressurization then, after the cooling of methanol-water cooler, a small amount of as spray methyl alcohol, all the other deliver to methanol wash Tata top as the fine wash sections cleaning solution.
The utility model increases the heat exchange area of the methanol-water cooler that the hot regenerator of described methyl alcohol bottom connects.The heat exchange area of the methanol-water cooler that the hot regenerator of described methyl alcohol bottom connects increases 58.74%.
For example, with described H 2The heat exchange area of the 2# poor methanol cooler that S concentration tower bottom connects increases 990m 2The heat exchange area of the methanol-water cooler that the hot regenerator of described methyl alcohol bottom is connected increases 430m 2
The mode of increase heat exchange area described in the utility model can be known from prior art by those skilled in the art.
The purpose that the utility model increases the heat exchange area of 2# poor methanol cooler is to take full advantage of H 2The cold of S concentration tower bottom methanol solution.The purpose that increases the heat exchange area of methanol-water cooler is the cold consumption of ammonia by further reduction 3# methyl alcohol chiller.
The utility model reduces its heat transfer temperature difference by suitably increasing the heat exchange area of 2# poor methanol cooler, thereby makes the poor methanol stream burst temperature that draws 2# poor methanol cooler tube side by-36.6 ℃, is reduced among the present invention-38.84 ℃.The rich methanol stream strand that goes out 3# poor methanol cooler shell side is reduced among the present invention-49.69 ℃ by original-47.83 ℃.Rich methanol stream thigh is supplied with newly-increased heat exchangers by-49.69 ℃ of colds that are reduced to-47.8 ℃.3# methyl alcohol chiller all is CO with the heat exchanger that increases newly 2Heat exchanger on the outflow liquid stream thigh of absorber portion, according to law of conservation of energy as can be known: 3# methyl alcohol chiller can reduce the heat exchange amount that is equal to newly-increased heat exchanger accordingly satisfy balance,, can significantly reduce the colod-application amount of ammonia that is.
Compare with the prior art scheme, the utlity model has following beneficial effect:
Carry out low-temp methanol washing process by the utility model process unit, though cooling water amount has increased by 22.73%, the more original technology of the colod-application amount of ammonia saves 10.2%.Because the Costco Wholesale of cooling water is cold far below ammonia, so the utility model scheme can significantly reduce the enterprise operation cost, and can reach existing energy-saving effect.
Process unit described in the utility model only needs to transform a little on original process unit and gets final product, and also can save improvement cost when saving operating cost.
Description of drawings
Fig. 1 is the process chart of original low-temperature rectisol;
Fig. 2 is the process chart of the utility model low-temperature rectisol.
Among Fig. 1: T3001-methanol wash tower; T3002-CO 2Analytic Tower; T3003-H 2The S concentration tower; The hot regenerator of T3004-methyl alcohol; T3005-methanol-water/knockout tower;
The C3001-recycle gas compressor; The V3001-separator; V3002-1# circulating air flash tank; V3003-2# circulating air flash tank; V3004-methyl alcohol collecting tank; V3005-sour gas separator; V3006-backflow flow container; V3007-methyl alcohol flash tank; V3008-methanol knockout tower charging separator;
1-conversion gas; 2-circulating air; The 4-purified gas; The 5-carbon dioxide; 6-tail gas; The 13-flashed vapour; 14-Crouse hydrogenation tail gas; The 15-low-pressure nitrogen; 16-sour gas/methyl alcohol; The rich sulphur steam of 17-; The 18-sour gas; The 22-methanol steam; 23-poor methanol liquid; 24-poor methanol stream thigh; 25-methyl alcohol rich solution; 26-comprises the methanol solution of whole sulphur; The 27-methanol; 30-CO 2The outflow liquid of absorber portion; 31-fine wash sections cleaning solution; 32-contains CO 2The methanol solution of sulfur-bearing not; 33-sulfur-bearing and CO 2Methanol solution; 34-rich methanol liquid; 35-liquid part; 36-H 2The phegma on S concentration tower top; 37-CO 2The phegma on Analytic Tower top; The 38-methanol solution; 39-CO 2The methanol solution of Analytic Tower bottom; The 40-condensate liquid; 41-H 2S concentration tower bottom methanol solution; 42-methanol condensed liquid; The 43-regenerated methanol; The cooled poor methanol of 45-; 49-waste water; The 51-washings;
E3001-unstripped gas heat exchanger; E3002-compressor water cooler; E3003-1# methyl alcohol chiller; E3004-2# methyl alcohol chiller; E3005-3# methyl alcohol chiller; E3006-recycle methanol cooler; E3007-methyl alcohol heat exchanger; E3008-3# poor methanol cooler; E3009-2# poor methanol cooler; E3010-1# poor methanol cooler; E3011-regenerator reboiler; E3012-sour gas water cooler; E3013-sour gas chiller; E3014-H 2S cut heat exchanger; E3015-methanol knockout tower reboiler; E3016-methanol-water/knockout tower feed heater; E3017-methyl alcohol cooler; E3018-methanol-water cooler; The E3019-water-to-water heat exchanger.
Among Fig. 2: the NEW-heat exchanger; Other are identical with Fig. 1.
Below the utility model is further described.But following example only is simple and easy example of the present utility model, does not represent or limit rights protection scope of the present utility model, and protection domain of the present utility model is as the criterion with claims.
The specific embodiment
For the utility model is described better, be convenient to understand the technical solution of the utility model, typical but non-limiting embodiment of the present utility model is as follows:
A kind of low-temp methanol washing process device, described device comprise methanol wash tower T3001, H 2S concentration tower T3003, the hot regenerator T3004 of methyl alcohol, described methanol wash tower T3001 is followed successively by fine wash sections, CO from top to bottom 2Main absorber portion and desulfurization section, described CO 2The outflow liquid 30 of the main absorber portion recycle methanol cooler E3006 inflow heat exchanger NEW that flows through makes CO 2Outflow liquid 30 and the H of main absorber portion 2The rich methanol liquid 34 at S concentration tower T3003 middle part) heat.Described CO 2The outflow liquid 30 of the main absorber portion 3# methyl alcohol chiller E3005 that before the recycle methanol cooler E3006 that flows through, flows through earlier.
A kind of low-temp methanol washing process device, described device comprise methanol wash tower T3001, CO 2Analytic Tower T3002, H 2S concentration tower T3003, the hot regenerator T3004 of methyl alcohol and methanol knockout tower T3005, described methanol wash tower T3001 is followed successively by fine wash sections, CO from top to bottom 2Main absorber portion and desulfurization section, described CO 2Main absorber portion flows out and connects heat exchanger NEW again, described heat exchanger NEW while and H after liquid 30 pipelines connect 3# methyl alcohol chiller E3005, recycle methanol cooler E3006 2Rich methanol liquid 34 pipelines at S concentration tower T3003 middle part connect.
The CO of the tube side entrance of described heat exchanger NEW and recycle methanol cooler E3006 2Main absorber portion flow export is communicated with, tube side outlet and the CO of described heat exchanger NEW 2Main absorber portion entrance is communicated with; The shell side entrance of described heat exchanger NEW is communicated with the shell side outlet of 3# poor methanol cooler E3008, and the shell side outlet of described heat exchanger NEW is communicated with the shell side entrance of recycle methanol cooler E3006.
Described H 2S concentration tower T3003 bottom is connected with 2# poor methanol cooler E3009.The heat exchange area of described 2# poor methanol cooler E3009 is increased 990m 2The hot regenerator T3004 of described methyl alcohol bottom is connected with methanol-water cooler E3018.The heat exchange area of the methanol-water cooler E3018 that the hot regenerator T3004 of described methyl alcohol bottom is connected increases 430m 2
It is as follows to carry out the low-temp methanol washing process process by the utility model process unit:
The 5.4MPa that the transformation into itself comes, 40 ℃ conversion gas 1 converge with the circulating air 2 that flashed vapour compressor C3001 sends here, for preventing that conversion gas is cooled to the icing phenomenon of appearance below freezing, spray into the poor methanol liquid 23 of 1303kg/h, be cooled to-20.15 ℃ through unstripped gas heat exchanger E3001 and purified gas 4, carbon dioxide 5, tail gas 6 heat exchange then, after separator V3001 isolated methanol aqueous solution, dry unstripped gas entered methanol wash tower T3001 again.
Methanol wash tower T3001 divides two parts up and down, and lower tower section is mainly used in desulfurization, and upper tower section can be divided into three sections again: push up section and be fine wash sections, absorb a small amount of CO that remains in the gas with-54.99 ℃ poor methanol stream thighs 24 2And H 2S is to guarantee CO in the downstream purification gas 4 2≤ 3%, H 2S≤0.1ppm; Middle two sections is CO 2Absorber portion is used the fine wash sections cleaning solution 31 after recycle methanol cooler E3006 heat exchange, enters CO under-36 ℃ 2Absorber portion absorbs the CO in the gas 2CO 2The outflow liquid 30 of absorber portion enters recycle methanol cooler E3006 after 3# methyl alcohol chiller E3005 is cooled to-24.29 ℃, be cooled to-34.19 ℃ after, enter again among the heat exchanger NEW with from H 2The rich methanol liquid 34 further heat exchange at S concentration tower T3003 middle part are cooled to-35.90 ℃, are back to CO then 2Absorber portion absorbs the CO in the gas 2About 52% methyl alcohol rich solution 25 takes out from last tower bottom tower tray, in methyl alcohol cooler E3017 and purified gas 4 heat exchange, be cooled to-31.65 ℃ through 2# methyl alcohol chiller E3004 again, enter 2# circulating air flash tank V3003 through reducing to 1850kPa, make the most of H that is dissolved in the methanol solution 2Steam.
Only need go up tower during following tower desulfurization and absorb CO 2The part methanol solution, its amount is about 48% of total amount, the methanol solution 26 that comprises whole sulphur after tower washs down flows out from methanol wash tower T3001 tower bottom, respectively in methyl alcohol heat exchanger E3007,1# methyl alcohol chiller E3003 heat exchange cooling, after being decompressed to 1850kPa, enter 1# circulating air flash tank V3002, make to be dissolved in most of H in the methanol solution 2Flash distillation is come out.The H that 1# circulating air flash tank V3002 and 2# circulating air flash tank V3003 flash distillation are come out 2By recycle gas compressor C3001, pressure-raising is cooled to-40 ℃ to the compressed machine water cooler of 5560kPa E3002, sends back to recycling on the unstripped gas pipeline of entrance.
That draws from 2# circulating air flash tank V3003 bottom contains CO 2The methanol solution 32 of sulfur-bearing not, through throttling expansion, pressure drops to 0.29MPa, enters CO 2Analytic Tower T3002 top of tower flashes off most of CO 2Gas, a part is as CO 2The phegma 37 on Analytic Tower T3002 top, a part is as H 2The phegma 36 on S concentration tower T3003 top.
The sulfur-bearing and the CO that draw from 1# circulating air flash tank V3002 bottom 2Methanol solution 33, through throttling expansion, pressure drops to 0.35MPa, enters CO 2The 8th column plate place, Analytic Tower T3002 middle part, at this, portion C O 2And H 2S parses from methanol solution, and methanol solution 38 is sent into H 2S concentration tower T3003 flashes off portion C O 2And H 2S obtains rich methanol liquid 34 by pressure-raising, pass through 3# poor methanol cooler E3008, newly-increased heat exchanger NEW, recycle methanol cooler E3006 successively, after temperature is reduced to-49.69 ℃ ,-47.8 ℃ ,-28.88 ℃ successively by-63.13 ℃, entering methyl alcohol flash tank V3007 separates, liquid part 35 is gone methyl alcohol heat exchanger E3007 heat exchange through pressurization again, and flashed vapour 13, liquid part 35 enter CO simultaneously then 2Tower under the Analytic Tower T3002 tower is raised to-28.88-29 ℃ by-63.13 ℃ because advancing tower methanol solution temperature, along with the rising of temperature, CO 2Solubility in methyl alcohol reduces, at CO 2Tower parses a large amount of CO under the Analytic Tower T3002 2From CO 2The methanol solution 39 of Analytic Tower T3002 bottom enters H 2Behind the S concentration tower T3003 tower middle part, further gone out CO by low-pressure nitrogen 15 air lifts 2, this part CO 2In company with air lift nitrogen and CO 2Analytic Tower T3002 tower overhead gas carbon dioxide 5 reclaims cold through unstripped gas heat exchanger E3001 together.Crouse's hydrogenation tail gas 14 enters H 2S concentration tower T3003.H 2S concentration tower T3003 bottom methanol solution 41 temperature are-43.46 ℃, through pressurization, after going into 2# poor methanol cooler E3009 and 1# poor methanol cooler E3010, with the poor methanol heat exchange after the regeneration, temperature is elevated to 35.43 ℃, 87.4 ℃ successively, enter then on the 26th block of column plate of the hot regenerator T3004 of methyl alcohol, be dissolved in whole sulphur and CO in the methanol solution 2Be reproduced the methanol steam air lift that tower reboiler E3011 heating produces, simultaneously methanol steam 22 air lifts that distilled out by methanol knockout tower T3005 cat head.The sour gas that heating is come out is carried the sour gas/methyl alcohol 16 of part methanol steam secretly and is drawn by cat head, after sour gas water cooler E3012 cooling, most of methanol steam is condensed, isolate methanol condensed liquid 42 as phegma through backflow flow container V3006, send back to the hot regenerator T3004 of methyl alcohol top of tower, leave the rich sulphur steam 17 at backflow flow container V3006 top, at H 2By precooling, further cool off in the hot regenerator sour gas of methyl alcohol chiller E3013 then among the S cut heat exchanger E3014, at this, nearly all methanol steam all is condensed, and separates through sour gas separator V3005 again, and condensate liquid 40 is delivered to H 2S concentration tower T3003 tower bottom is handled, and sour gas 18 parts are circulated to H 2On the 25th block of column plate of S concentration tower T3003, part is through H 2S cut heat exchanger E3014 delivers to out-of-bounds sulfur recovery after reclaiming cold.
Take out regenerated methanol 43 from the hot regenerator T3004 of methyl alcohol bottom, deliver to methyl alcohol collecting tank V3004 after in 1# poor methanol cooler E3010, being cooled to 44.14 ℃, be pressurized to 6.5MPa then, after methanol-water cooler E3018 cooling, except a small amount of conduct spray methyl alcohol, all the other deliver to methanol wash tower T3001 top of tower as the fine wash sections cleaning solution after 2# poor methanol cooler E3009,3# poor methanol cooler E3008 are cooled to-54.99 ℃.
The methanol of coming from separator V3001 27 among methanol knockout tower feed heater E3016 with by methyl alcohol at the bottom of the hot regenerator T3004 tower through cooled poor methanol 45 heat exchange, temperature rises to 60.80 ℃ through entering behind the methanol knockout tower charging separator V3008 on the 21st block of column plate of methanol knockout tower T3005 tower, simultaneously, after washings 51 pressurizations behind the washing tail gas, in water-to-water heat exchanger E3019, heat up and deliver on the 13rd block of column plate of methanol knockout tower T3005 tower, the distillation of their fellowships, tower bottom steam is produced by methanol knockout tower reboiler E3015 heat exchange, methanol steam is directly sent into the hot regenerator T3004 of methyl alcohol after 51 column plate distillations, and delivers to methanol-water knockout tower T3005 top as phegma by the cooled poor methanol 45 of methanol-water/knockout tower feed heater E3016.Waste water 49 at the bottom of the tower is disposed to Waste Water Treatment reclaim heat in water-to-water heat exchanger E3019 after.
Applicant's statement, the utility model illustrates detailed construction feature of the present utility model and low-temp methanol washing process by above-described embodiment, but the utility model is not limited to above-mentioned detailed construction feature and process, does not mean that namely the utility model must rely on above-mentioned detailed construction feature and process could be implemented.The person of ordinary skill in the field should understand; to any improvement of the present utility model; to the increase of the equivalence replacement of the selected parts of the utility model and accessory, the selection of concrete mode etc., all drop within protection domain of the present utility model and the open scope.
Public work consumption contrast before and after table 1 is optimized
The public work type Quality Existing energy consumption/kw Optimize energy consumption/kw Energy-saving potential/%
Cold public work ? 11652.7 ? ?
Ammonia refrigeration -38℃/-38℃ 4920.62 4419.92 10.2
Cooling water 28℃/40℃ 6732.1 8261.9 22.73
Hot public work ? 9035.67 ? ?
Low-pressure steam 1.27MPa 1809.21 ? ?
Low-pressure steam 0.30MPa 7226.46 ? ?
In the technological process after optimizing as can be seen from Table 1, though the consumption of cooling water increases by 22.73%, the colod-application amount of ammonia saves 10.2%.Because the Costco Wholesale of cooling water is cold far below ammonia, so the utility model scheme can significantly reduce the enterprise operation cost.The utility model increases two heat exchangers by newly-increased heat exchanger, can reach existing energy-saving effect.
Table 2 is optimized forward part heat exchanger information
Figure BDA00002657969900131
Table 2 is optimized rear section heat exchanger information
Figure BDA00002657969900141

Claims (7)

1. low-temp methanol washing process device, described device comprises methanol wash tower (T3001), H 2S concentration tower (T3003), the hot regenerator of methyl alcohol (T3004) is characterized in that described methanol wash tower (T3001) is followed successively by fine wash sections, CO from top to bottom 2Main absorber portion and desulfurization section, described CO 2The outflow liquid (30) of main absorber portion recycle methanol cooler (E3006) inflow heat exchanger (NEW) of flowing through makes CO 2Outflow liquid (30) and the H of main absorber portion 2Rich methanol liquid (34) heat exchange at S concentration tower (T3003) middle part.
2. device as claimed in claim 1 is characterized in that, described CO 2The outflow liquid (30) of main absorber portion is at the recycle methanol cooler (E3006) of the flowing through 3# methyl alcohol chiller (E3005) of flowing through earlier before.
3. device as claimed in claim 2 is characterized in that, the CO of the tube side entrance of described heat exchanger (NEW) and recycle methanol cooler (E3006) 2Main absorber portion flow export is communicated with, tube side outlet and the CO of described heat exchanger (NEW) 2Main absorber portion entrance is communicated with; The shell side entrance of described heat exchanger (NEW) is communicated with the shell side outlet of 3# poor methanol cooler (E3008), and the shell side outlet of described heat exchanger (NEW) is communicated with the shell side entrance of recycle methanol cooler (E3006).
4. device as claimed in claim 1 is characterized in that, described H 2S concentration tower (T3003) bottom is connected with 2# poor methanol cooler (E3009).
5. device as claimed in claim 4 is characterized in that, with the heat exchange area increase 16.58% of described 2# poor methanol cooler (E3009).
6. device as claimed in claim 1 is characterized in that, the hot regenerator of described methyl alcohol (T3004) bottom is connected with methanol-water cooler (E3018).
7. device as claimed in claim 6 is characterized in that, with the heat exchange area increase 58.74% of described methanol-water cooler (E3018).
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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
CN104293398A (en) * 2014-10-27 2015-01-21 上海国际化建工程咨询公司 Energy-saving and production-increasing method and device adopting low temperature methanol cleaning technology
CN105233628A (en) * 2015-09-21 2016-01-13 七台河宝泰隆煤化工股份有限公司 Shift gas gas-water separation method
CN106422672A (en) * 2016-10-26 2017-02-22 中石化宁波工程有限公司 Method for preventing low-temperature methanol washing heat regeneration system from being corroded
CN106608618A (en) * 2015-10-21 2017-05-03 中国石油化工股份有限公司 Acid gas purification process
CN109627187A (en) * 2019-01-03 2019-04-16 灵谷化工有限公司 A kind of bypass adjustment type washing device for methanol and its technique
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CN113532191A (en) * 2021-07-22 2021-10-22 华亭煤业集团有限责任公司 Optimized heat exchange network of low-temperature methanol washing system
CN113599978A (en) * 2021-09-02 2021-11-05 河南心连心化学工业集团股份有限公司 Anhydrous low-temperature methanol washing device and production method
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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
CN104140852B (en) * 2013-11-22 2016-02-24 上海国际化建工程咨询公司 A kind of devices and methods therefor processing low-temperature rectisol crystalline ammonium and purification lean solution methyl alcohol
CN104293398A (en) * 2014-10-27 2015-01-21 上海国际化建工程咨询公司 Energy-saving and production-increasing method and device adopting low temperature methanol cleaning technology
CN105233628A (en) * 2015-09-21 2016-01-13 七台河宝泰隆煤化工股份有限公司 Shift gas gas-water separation method
CN106608618A (en) * 2015-10-21 2017-05-03 中国石油化工股份有限公司 Acid gas purification process
CN106422672A (en) * 2016-10-26 2017-02-22 中石化宁波工程有限公司 Method for preventing low-temperature methanol washing heat regeneration system from being corroded
CN109627187A (en) * 2019-01-03 2019-04-16 灵谷化工有限公司 A kind of bypass adjustment type washing device for methanol and its technique
CN109627187B (en) * 2019-01-03 2021-05-11 灵谷化工集团有限公司 Bypass adjustment balance type methanol washing device and process thereof
CN111848399A (en) * 2020-07-14 2020-10-30 上海交通大学 Method for separating dimethyl oxalate and dimethyl carbonate with low energy consumption
CN114788983A (en) * 2021-01-26 2022-07-26 大连佳纯气体净化技术开发有限公司 Low-temperature methanol cleaning method and device
CN114788983B (en) * 2021-01-26 2023-09-08 大连佳纯气体净化技术开发有限公司 Low-temperature methanol cleaning method and device
CN113532191A (en) * 2021-07-22 2021-10-22 华亭煤业集团有限责任公司 Optimized heat exchange network of low-temperature methanol washing system
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