CN103289754A - Recovery method and apparatus of flash steam - Google Patents
Recovery method and apparatus of flash steam Download PDFInfo
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- CN103289754A CN103289754A CN2013102535656A CN201310253565A CN103289754A CN 103289754 A CN103289754 A CN 103289754A CN 2013102535656 A CN2013102535656 A CN 2013102535656A CN 201310253565 A CN201310253565 A CN 201310253565A CN 103289754 A CN103289754 A CN 103289754A
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- flashed vapour
- methyl alcohol
- spray
- ammonia
- ammoniacal liquor
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- 238000011084 recovery Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 24
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 75
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 37
- 238000001816 cooling Methods 0.000 claims abstract description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 153
- 239000007921 spray Substances 0.000 claims description 43
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 32
- 238000005406 washing Methods 0.000 claims description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 19
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 230000018044 dehydration Effects 0.000 claims description 12
- 238000006297 dehydration reaction Methods 0.000 claims description 12
- 238000002309 gasification Methods 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 claims description 5
- 240000000233 Melia azedarach Species 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 23
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 13
- 239000007788 liquid Substances 0.000 description 11
- 239000005864 Sulphur Substances 0.000 description 9
- 230000008569 process Effects 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 241000196324 Embryophyta Species 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 230000002708 enhancing effect Effects 0.000 description 2
- 238000007710 freezing Methods 0.000 description 2
- 230000008014 freezing Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a recovery method and an apparatus of flash steam. The recovery method comprises following steps: pre-cooling, ammonia removing and dehydrating. The recovery method of flash steam can be used to recycle useful gases in flash stream.
Description
Technical field
The recovery technology field that the present invention relates to drop a hint is in particular to a kind of recovery method and device of flashed vapour.
Background technology
Texaco gasifier is present modal a kind of vapourizing furnace type of furnace, and the mature and reliable that possesses skills, the home-made equipment rate is high and invest characteristics such as little, so be the generally employing of China coal chemical industry enterprises institute.
Existing Inferior of Texaco Gasification Technology and conversion process have a common feature, exactly flashed vapour (gasification high pressure flash gas and conversion high temperature condensate flash gas) are sent to the sulfur recovery burning disposal.Owing to also have effective constituents such as carbon monoxide and hydrogen in the flashed vapour, therefore above-mentioned technical process meeting causes the waste problem of available gas, has caused the wasting of resources.Owing to have carbonic acid gas and water vapour in the above-mentioned flashed vapour, can cause problems such as sulfur recovery sulphur furnace temperature processed is low, burning ammonia is incomplete like this, reduced the sulphur quality.
Summary of the invention
The present invention aims to provide a kind of recovery method and device that can reclaim the flashed vapour of available gas in the flashed vapour.
To achieve these goals, according to an aspect of the present invention, provide a kind of recovery method of flashed vapour, may further comprise the steps: precooling; Except ammonia; And dehydration.
Further, dehydrating step may further comprise the steps: will be except the flashed vapour behind the ammonia and spray methanol mixed, and wherein, spray methyl alcohol mixes the moisture spray methyl alcohol of formation with water in the flashed vapour; Mixed flashed vapour and spray methyl alcohol are carried out deep cooling; With moisture spray methanol stripper to finish the dehydration of flashed vapour.
Further, dehydrating step further may further comprise the steps: the methyl alcohol in the moisture spray methyl alcohol that separates is reclaimed.
Further, further comprising the steps of after dehydrating step: the flashed vapour after will dewatering pressurizes; Flashed vapour after the pressurization is delivered to downstream section.
Further, except in the ammonia step, utilize wash ammoniacal liquor carry out flashed vapour except ammonia, and, to carrying out stripping and wash ammonia in the ammoniacal liquor with acquisition with the ammoniacal liquor of washing after flashed vapour contact.
Further, flashed vapour comprises gasification high pressure flash gas and conversion high temperature condensate flash gas, and gasification high pressure flash gas and conversion high temperature condensate flash gas mix before the precooling step carrying out.
According to a further aspect in the invention, provide a kind of retrieving arrangement of flashed vapour, having comprised: the pre-cooler of Lian Jieing, Ammonic washing tower, chiller and separating tank successively, wherein, the pipeline between Ammonic washing tower and the chiller is provided with the methyl alcohol mouth spray.
Further, Ammonic washing tower has the ammoniacal liquor of washing import, washes ammoniacal liquor outlet, gas feed and pneumatic outlet, washes on the stripping tower that ammoniacal liquor outlet is connected to the carbon monodixe conversion unit with stripping and the ammonia in the ammoniacal liquor washed after flashed vapour contacts.
Further, retrieving arrangement of the present invention also comprises: the methanol-water knockout tower, be connected with separating tank, and be used for to reclaim the methyl alcohol of moisture spray methyl alcohol, wherein, moisture spray methyl alcohol is to be mixed with water the flashed vapour by the spray methyl alcohol that enters from the methyl alcohol mouth spray to form.
Further, retrieving arrangement of the present invention also comprises: compressor assembly, be connected with separating tank, and be used for improving the pressure of flashed vapour.
Use technical scheme of the present invention, make flashed vapour no longer enter sulphur stove processed and carry out burning disposal, but reclaim by precooling, except the step of ammonia and dehydration.Through after the above-mentioned steps, can remove ammonia and moisture in the flashed vapour, can directly send into downstream (such as the low-temperature rectisol unit) like this and carry out the recovery of available gas in the flashed vapour, improve rate of energy so effectively.Simultaneously, owing to need not flashed vapour is sent to the sulfur recovery burning disposal, thereby reduced to enter the amount of sulphur stove foreign gas processed, so can improve sulphur furnace temperature processed, improved the sulphur quality, also made and burn the environment protecting that the enhancing of ammonia effect has reached reduction of discharging.
Description of drawings
The Figure of description that constitutes the application's a part is used to provide further understanding of the present invention, and illustrative examples of the present invention and explanation thereof are used for explaining the present invention, do not constitute improper restriction of the present invention.In the accompanying drawings:
Fig. 1 shows the schematic flow sheet according to the embodiment of the recovery method of flashed vapour of the present invention;
Fig. 2 shows the dewatering process flow synoptic diagram of recovery method of the flashed vapour of Fig. 1;
Fig. 3 shows the structural representation according to the embodiment of the retrieving arrangement of flashed vapour of the present invention.
Embodiment
Need to prove that under the situation of not conflicting, embodiment and the feature among the embodiment among the application can make up mutually.Describe the present invention below with reference to the accompanying drawings and in conjunction with the embodiments in detail.
As shown in Figure 1, the recovery method of the flashed vapour of present embodiment may further comprise the steps:
Step S10, the precooling of flashed vapour can be finished above-mentioned steps by pre-cooler.Above-mentioned precooling step can guarantee to wash the ammonia effect, washes the ammonia effect in order to improve, and flashed vapour preferably can reach below 40 ℃ through the temperature after the precooling, to separate a large amount of water vapour in the flashed vapour.Recovery method according to the application, the flashed vapour that can reclaim comprises gasification high pressure flash gas and conversion high temperature condensate flash gas, preferably, in order to adapt to pre-cool equipment better, gasification high pressure flash gas and conversion high temperature condensate flash gas mix before the precooling step carrying out.
Step S20, after the precooling flashed vapour except ammonia, can wash ammoniacal liquor by the Ammonic washing tower utilization and finish above-mentioned steps.For can better control drop a hint wash the ammonia effect, in the ammoniacal liquor inlet ductwork flow that ammoniacal liquor is washed in flow valve control is set, the flow of washing ammoniacal liquor is 100～200kg per hour preferably.Preferred scheme requires to wash ammonia content in the flashed vapour behind the ammonia less than 6ppm.Above-mentioned wash ammoniacal liquor and can adopt deaerated water or de-salted water.Preferably, to utilizing carbon monodixe conversion unit existing system to carry out stripping to obtain to wash the ammonia in the ammoniacal liquor with the ammoniacal liquor of washing after flashed vapour contacts.
Step S30 is except the dehydration of flashed vapour behind the ammonia.
Through after the above-mentioned steps, can remove ammonia and moisture in the flashed vapour, through the pressurization back or directly send into downstream units (such as sending into the low-temperature rectisol unit after the pressurization) and carry out the recovery of available gas in the flashed vapour, improve rate of energy so effectively.Simultaneously, owing to need not flashed vapour is sent to the sulfur recovery burning disposal, thereby reduced to enter the amount of sulphur stove foreign gas processed, so can improve sulphur furnace temperature processed, improved the sulphur quality, also made and burn the environment protecting that the enhancing of ammonia effect has reached reduction of discharging.
Preferably, as shown in Figure 2, this dehydration preferably includes following steps:
Step S31 will be except the flashed vapour behind the ammonia and spray methanol mixed, and wherein, spray methyl alcohol mixes the moisture spray methyl alcohol of formation with water in the flashed vapour.Pipeline in the ammonia removal equipment downstream arranges the methyl alcohol mouth spray to realize the mixing of spray methyl alcohol and flashed vapour, and the spray step can reduce the freezing point of water in the flashed vapour.Preferably, spray per hour 4～6kg of methyl alcohol.
Step S32 carries out deep cooling with mixed described flashed vapour and spray methyl alcohol.Can finish above-mentioned deep cooling step by chiller.Preferably, the temperature of the flashed vapour after the chiller cooling is preferably in-30～-36 ℃.
Step S33, with moisture spray methanol stripper to finish the dehydration of flashed vapour.Can realize the step that removes of above-mentioned moisture spray methyl alcohol by separating tank.
Step S34 reclaims the methyl alcohol in the moisture spray methyl alcohol that separates.Can pass through low-temperature rectisol unit existing system, carry out the recovery of above-mentioned methyl alcohol such as the methanol-water knockout tower.
Preferably, further comprising the steps of after dehydrating step:
Step S40 pressurizes the flashed vapour after the dehydration, can realize by independent compression system, preferably pressurizes by the recycle gas compressor system of low-temperature rectisol unit.Like this, the recovery technology of present embodiment can effectively integrate the resource between each chemical plant installations, to realize low input, the purpose of high benefit.Because present embodiment produces washes ammoniacal liquor and moisture spray methyl alcohol can utilize existing process system to recycle, simultaneously can utilize the recycle gas compressor system of low-temperature rectisol unit that flashed vapour is carried out pressure treatment, therefore can realize the plant factor maximization, minimumization of investment working cost, economic environmental benefit optimization.
Step S50 delivers to downstream section with the flashed vapour after the pressurization.Obtain required product through flashed vapour being processed as raw material after the above-mentioned steps.
As shown in Figure 3, comprise according to the embodiment of the retrieving arrangement of flashed vapour of the present invention: the pre-cooler E01 of Lian Jieing, Ammonic washing tower T01, chiller E02 and separating tank V01 successively, wherein, the pipeline between Ammonic washing tower T01 and the chiller E02 is provided with the methyl alcohol mouth spray.About 10～the 13bar of this flow operations pressure ,-33 ℃ approximately of separating tank V01 flashed vapour temperature outs.Pre-cooler E01 utilizes recirculated water to be the precooling medium, Ammonic washing tower T01 utilizes the ammonia in the de-salted water washing flashed vapour, chiller E02 utilizes liquefied ammonia or propylene to the flashed vapour deep dehydration of lowering the temperature, and containing a large amount of aqueous methanol in the flashed vapour after the cooling need separate in separating tank V01.
Preferably, the retrieving arrangement of present embodiment also comprises 3 liquid level valves and 2 flow valves.Be respectively liquid level valve LV01, liquid level valve LV02, liquid level valve LV03, flow valve FV01 and flow valve FV02.The liquid level of liquid level valve LV01 control Ammonic washing tower T01, liquid level valve LV02 controlled chilling device E02 liquid level, the liquid level of liquid level valve LV03 control separating tank V01.The amount that ammoniacal liquor is washed in flow valve FV01 control, the amount of flow valve FV02 control spray methyl alcohol.
Preferably, Ammonic washing tower T01 has the ammoniacal liquor of washing import, washes ammoniacal liquor outlet, gas feed and pneumatic outlet, washes on the stripping tower that ammoniacal liquor outlet is connected to the carbon monodixe conversion unit with stripping and the ammonia in the ammoniacal liquor washed after flashed vapour contacts.In Ammonic washing tower T01, feed and wash ammoniacal liquor and contact with flashed vapour, will with after flashed vapour contacts wash ammoniacal liquor deliver to the carbon monodixe conversion unit the stripping tower stripping wash ammonia in the ammoniacal liquor.
Preferably, the retrieving arrangement of this enforcement also comprises: the methanol-water knockout tower, be connected with separating tank, and be used for to reclaim the methyl alcohol of moisture spray methyl alcohol, wherein, moisture spray methyl alcohol is to be mixed with water the flashed vapour by the spray methyl alcohol that enters from the methyl alcohol mouth spray to form.Preferably, the retrieving arrangement of this enforcement also comprises: compressor assembly, be connected with separating tank, and be used for improving the pressure of flashed vapour.Wherein compressor assembly utilizes the low-temperature rectisol unit to have compressor now, also can design compressor assembly separately.
Make detailed introduction according to the working process of the retrieving arrangement of the present embodiment of Fig. 3 below:
Gasification high pressure flash gas 1 and conversion high temperature condensate flash gas 2 converge before entering pre-cooler E01, and pre-cooler E01 adopts the recirculated water refrigeration, and water 12 is 30 ℃ on the recirculated water, and recirculated water backwater 13 is 40 ℃.Flashed vapour 3 after the precooling enters Ammonic washing tower T01, controls the flow of washing ammoniacal liquor 6 by flow valve FV01, washs the stripping tower stripping ammonia wherein that ammoniacal liquor 5 is sent to conversion of washing after dropping a hint.Flashed vapour 4 mixes with spray methyl alcohol 7 after going out Ammonic washing tower T01, and the freezing point of the water vapour that contains in the flashed vapour is down to below-40 ℃, guarantees water vapour in the flashed vapour obstruction heat-exchanging tube bundle that can not freeze in chiller E02.Chiller E02 utilizes propylene or ammonia to be refrigeration agent, and 11a is propylene liquid or liquid ammonia, and 11b is propylene steam or gaseous ammonia.Be reduced to through flashed vapour 8 temperature of chiller E02 cooling and enter separating tank V01 after-33 ℃ and separate the moisture spray methyl alcohol that cools down.The methanol-water knockout tower that the moisture spray methyl alcohol 9 that separates is sent to the low-temperature rectisol unit carries out Methanol Recovery.Through the recycle gas compressor system that is sent to the low-temperature rectisol unit except the flashed vapour 10 behind the ammonia, cooling, the dehydration recovery of pressurizeing.Flashed vapour after the pressurization is sent into process system (such as the low-temperature rectisol unit) with middle pressure flashed vapour and is reclaimed.
The above is the preferred embodiments of the present invention only, is not limited to the present invention, and for a person skilled in the art, the present invention can have various changes and variation.Within the spirit and principles in the present invention all, any modification of doing, be equal to replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (10)
1. the recovery method of a flashed vapour is characterized in that, may further comprise the steps:
Precooling;
Except ammonia; And
Dehydration.
2. recovery method according to claim 1 is characterized in that, described dehydrating step may further comprise the steps:
Will be except the described flashed vapour behind the ammonia and spray methanol mixed, wherein, described spray methyl alcohol mixes the moisture spray methyl alcohol of formation with water in the described flashed vapour;
Mixed described flashed vapour and described spray methyl alcohol are carried out deep cooling;
With described moisture spray methanol stripper to finish the dehydration of described flashed vapour.
3. recovery method according to claim 2 is characterized in that, described dehydrating step further may further comprise the steps: the methyl alcohol in the described moisture spray methyl alcohol that separates is reclaimed.
4. recovery method according to claim 1 is characterized in that, and is further comprising the steps of after described dehydrating step:
Described flashed vapour after the dehydration is pressurizeed;
Described flashed vapour after the pressurization is delivered to downstream section.
5. recovery method according to claim 1 is characterized in that, and is described except in the ammonia step, utilize wash ammoniacal liquor carry out described flashed vapour except ammonia, and, to carrying out stripping to obtain the described ammonia of washing in the ammoniacal liquor with the ammoniacal liquor of washing after described flashed vapour contacts.
6. recovery method according to claim 1, it is characterized in that, described flashed vapour comprises gasification high pressure flash gas and conversion high temperature condensate flash gas, and described gasification high pressure flash gas and described conversion high temperature condensate flash gas mix before the described precooling step carrying out.
7. the retrieving arrangement of a flashed vapour is characterized in that, comprising:
The pre-cooler of Lian Jieing (E01), Ammonic washing tower (T01), chiller (E02) and separating tank (V01) successively, wherein, the pipeline between described Ammonic washing tower (T01) and the described chiller (E02) is provided with the methyl alcohol mouth spray.
8. retrieving arrangement according to claim 7, it is characterized in that, described Ammonic washing tower (T01) has the ammoniacal liquor of washing import, washes ammoniacal liquor outlet, gas feed and pneumatic outlet, described washing on the stripping tower that ammoniacal liquor outlet is connected to the carbon monodixe conversion unit with stripping and the ammonia in the ammoniacal liquor washed after described flashed vapour contacts.
9. retrieving arrangement according to claim 7, it is characterized in that, also comprise: the methanol-water knockout tower, be connected with described separating tank, be used for reclaiming the methyl alcohol of moisture spray methyl alcohol, wherein, described moisture spray methyl alcohol is to be mixed with water the described flashed vapour by the spray methyl alcohol that enters from described methyl alcohol mouth spray to form.
10. retrieving arrangement according to claim 7 is characterized in that, also comprises: compressor assembly, be connected with described separating tank, and be used for improving the pressure of described flashed vapour.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2013102535656A CN103289754A (en) | 2013-06-24 | 2013-06-24 | Recovery method and apparatus of flash steam |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2013102535656A CN103289754A (en) | 2013-06-24 | 2013-06-24 | Recovery method and apparatus of flash steam |
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| CN2013102535656A Pending CN103289754A (en) | 2013-06-24 | 2013-06-24 | Recovery method and apparatus of flash steam |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105330571A (en) * | 2015-06-19 | 2016-02-17 | 上海珈叶实业有限公司 | Preparation method of hydroxyethylurea crystal or aqueous solution |
| CN106957213A (en) * | 2015-12-18 | 2017-07-18 | 乔治·克劳德方法的研究开发空气股份有限公司 | Recover the technique and device of methanol |
| CN108277050A (en) * | 2018-03-10 | 2018-07-13 | 河南晋煤天庆煤化工有限责任公司 | A kind of low-temp methanol washes two sections of flashed vapour recycling systems of flash column |
| CN112520808A (en) * | 2020-11-26 | 2021-03-19 | 中国天辰工程有限公司 | CO conversion condensate refining process system and method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1264316A (en) * | 1997-06-06 | 2000-08-23 | 德士古发展公司 | Black water flash and vapor recovery system |
| CN102489120A (en) * | 2011-12-07 | 2012-06-13 | 中国华能集团清洁能源技术研究院有限公司 | Low temperature methanol wash method and equipment |
-
2013
- 2013-06-24 CN CN2013102535656A patent/CN103289754A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1264316A (en) * | 1997-06-06 | 2000-08-23 | 德士古发展公司 | Black water flash and vapor recovery system |
| CN102489120A (en) * | 2011-12-07 | 2012-06-13 | 中国华能集团清洁能源技术研究院有限公司 | Low temperature methanol wash method and equipment |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105330571A (en) * | 2015-06-19 | 2016-02-17 | 上海珈叶实业有限公司 | Preparation method of hydroxyethylurea crystal or aqueous solution |
| CN106957213A (en) * | 2015-12-18 | 2017-07-18 | 乔治·克劳德方法的研究开发空气股份有限公司 | Recover the technique and device of methanol |
| CN108277050A (en) * | 2018-03-10 | 2018-07-13 | 河南晋煤天庆煤化工有限责任公司 | A kind of low-temp methanol washes two sections of flashed vapour recycling systems of flash column |
| CN108277050B (en) * | 2018-03-10 | 2023-11-24 | 河南晋控天庆煤化工有限责任公司 | Two-stage flash gas recycling system of low-temperature methanol washing flash tower |
| CN112520808A (en) * | 2020-11-26 | 2021-03-19 | 中国天辰工程有限公司 | CO conversion condensate refining process system and method |
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Application publication date: 20130911 |