CN203923123U - A kind of device that reduces low-temperature rectisol methane rate of loss - Google Patents
A kind of device that reduces low-temperature rectisol methane rate of loss Download PDFInfo
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- CN203923123U CN203923123U CN201420309957.XU CN201420309957U CN203923123U CN 203923123 U CN203923123 U CN 203923123U CN 201420309957 U CN201420309957 U CN 201420309957U CN 203923123 U CN203923123 U CN 203923123U
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Abstract
The disclosed a kind of device that reduces low-temperature rectisol methane rate of loss of the utility model, is characterized in that, comprises absorption tower and middle pressure flashing tower.It presses flashing tower by pressing flash tank to replace with in one in two of traditional low-temperature rectisols; Utilize the crude synthesis gas after desulfurization to pass into middle pressure flashing tower as gas stripping gas, by CH
4, H
2deng available gas air lift out; Air lift out enters into cycle compressor pressurization containing the gas of methane and enters the rate of recovery that methane is improved on absorption tower; Reduce methane from exhaust emissions amount, alleviate environmental pressure.
Description
Technical field
The utility model relates to low-temperature rectisol and purifies high methane crude synthesis gas processing technology field, be particularly related to a kind ofly by reconfiguring low-temperature rectisol flow process, to reach, increase methane at the device of the minimizing low-temperature rectisol methane rate of loss of the low temperature washing device for methanol rate of recovery.
Background technology
In view of China is a few country of the many gas of coal, at present, it is raw material that most of chemical enterprises all adopt coal.In view of low-temperature rectisol has the features such as suitability is extensive, raw material is cheaply easy to get, nearly all coal chemical industry enterprises is all furnished with low-temperature rectisol workshop section, to remove benzene, toluene, oil, the H in synthetic gas
2s, CO
2etc. component.
Coal is the world saving the widest fossil energy of distribution at most, the age forming according to coal and different region particularities, quality and the kind of coal are diversity, for adapting to different atures of coal, developed different gasification technologies, for example, coal water slurry gasification technology, crushed coal pressure gasifying technology, powdered coal pressuring gasified technology, Hygas gasification technology etc.Yet for the application of low grade coal, generally adopt at present the gasification technologies such as crushed coal pressure gasifying technology, Hygas, coal oil mixture.The above-mentioned type gasification technology is due to features such as its vapor pressure high-temperature are low, and the raw gas of production all contains the more low catenanes gases such as methane.
Low temperature washing device for methanol is mainly to utilize methyl alcohol at low temperatures to have very large solvability to sour gas, yet to H
2, CO solvability less, thereby reach the loss available gas of trying one's best few in decontaminating syngas.In the middle of the crude synthesis gas of producing in above-mentioned gasification, contain about 10～16% methane composition.Yet methane is approximately H in the solubleness of low-temp methanol
2several times～decades of times left and right, therefore, when low temperature washing device for methanol purifies containing the higher synthetic gas of methane, often the rate of loss of methane is also relatively high, has reduced the utilization ratio of raw material.
In the middle of traditional low-temperature rectisol flow process, after being absorbed by methyl alcohol, methane sub-fraction discharges and re-uses by recycle gas compressor in middle pressure flash distillation, and most will be at CO in addition
2product tower and hydrogen sulfide upgrading tower tower top discharge.Not only reduced the utilization ratio of methane, and the methane not being recovered will enter into atmosphere with tail gas.Increased environmental pressure.Therefore in traditional low-temperature rectisol flow process, can not there is high methane recovery.And solving the weak point of above-mentioned flow process, key is in the mode by air lift, CH4 to be separated from low-temp methanol.
Utility model content
Technical problem to be solved in the utility model is to provide a kind of device that reduces low-temperature rectisol methane rate of loss for the weak point of above-mentioned flow process, this device mainly considers that low-temp methanol CH4 has certain solvability, and the methane being absorbed by low-temp methanol will be released in atmosphere in follow-up regenerative section from tail gas.Before the methane being absorbed by low-temp methanol discharges, by the mode of air lift, methane is separated from low-temp methanol to the rate of recovery that not only can improve methane, can also reduce the discharge of methane to atmosphere.
Technical problem to be solved in the utility model can be achieved through the following technical solutions:
A device that reduces low-temperature rectisol methane rate of loss, comprising:
One absorption tower, described absorption tower at least has clean gas outlet, a superposed methyl alcohol lean solution entrance that is positioned at tower top, is positioned at the sulfur-bearing rich methanol taphole containing methane crude synthesis gas entrance and at the bottom of being positioned at tower of bottom, in inside, described absorption tower, is at least provided with from the bottom to top desulfurization section tower reactor, decarbonization section tower reactor and cooling section tower reactor; On the bottom of decarbonization section tower reactor, be also provided with rich CO
2methanol solution outlet; On desulfurization section tower reactor top, be provided with exporting and rich CO containing methane crude synthesis gas after desulfurization
2methanol solution return port; At described methyl alcohol lean solution entrance, connect a methyl alcohol lean solution intake pipeline, on described clean gas outlet, connect a purified gas export pipeline, described purified gas export pipeline is connected to downstream unit, the described methane crude synthesis gas entrance that contains connects a crude synthesis gas intake pipeline, and described crude synthesis gas intake pipeline is connected to upstream changing device;
In one, press flashing tower, described middle pressure flashing tower is divided in upper and lower two sections presses flash distillation tower reactor, presses the top of flash distillation tower reactor to be provided with a rich CO in described epimere
2methanol solution entrance, bottom is provided with air lift gas inlet, and top is provided with air lift gas loop exit, and bottom is provided with the methanol solution outlet after air lift; In described hypomere, press the top of flash distillation tower reactor to be provided with a sulfur-bearing rich methanol solution entrance, bottom is provided with air lift gas loop head, and top is provided with by air lift pneumatic outlet out, and bottom is provided with the methanol solution outlet after air lift;
Being connected with pressing the air lift gas inlet of flash distillation tower reactor in described epimere by air lift gas line of pipes containing the outlet of methane crude synthesis gas after the desulfurization on described desulfurization section tower reactor top; Rich CO on described decarbonization section tower reactor bottom
2the upper rich CO of two-way that connects of methanol solution outlet
2methanol solution line of pipes, the wherein rich CO in a road
2methanol solution line of pipes is connected to the rich CO on desulfurization section tower reactor top
2methanol solution return port, the rich CO in another road
2methanol solution line of pipes is connected to the rich CO that presses flash distillation tower reactor top in described epimere by the first water cooler, the first reducing valve
2methanol solution entrance, presses the air lift gas loop exit at flash distillation tower reactor top by air lift gas recirculation pipework, to be connected to the air lift gas loop head of pressing flash distillation tower reactor bottom in described hypomere in described epimere; The sulfur-bearing rich methanol taphole of bottom, described absorption tower is connected to the sulfur-bearing rich methanol solution entrance of pressing flash distillation tower reactor top in described hypomere by sulfur-bearing rich methanol solution conveyor tube line, the second water cooler, the second reducing valve; In described hypomere, press flash distillation tower reactor top by air lift pneumatic outlet out by by air lift air shooter line, circulator compressor, the 3rd water cooler out, be connected to bottom, described absorption tower containing methane crude synthesis gas entrance; In described upper and lower two sections, press the methanol solution outlet after the air lift of flash distillation tower reactor bottom by the methanol solution line of pipes after first, second air lift, to be connected to methanol solution regenerative section respectively.
Owing to having adopted technical scheme as above, the utility model is by pass into gas stripping gas in middle pressure flashing tower, by CH
4from low-temp methanol, separate, to improve methane recovery.
Feature of the present utility model is:
1, by pressing flash tank to replace with in one in two of traditional low-temperature rectisols, press flashing tower;
2, utilize the crude synthesis gas after desulfurization to pass into middle pressure flashing tower as gas stripping gas, by available gas air lifts such as CH4, H2 out;
3, air lift out enters into cycle compressor pressurization containing the gas of methane and enters the rate of recovery that methane is improved on absorption tower;
4, reduce methane from exhaust emissions amount, alleviate environmental pressure.
Accompanying drawing explanation
Fig. 1 is the apparatus structure schematic diagram of minimizing low-temperature rectisol methane rate of loss of the present utility model.
Embodiment
Referring to Fig. 1, a kind of device that reduces low-temperature rectisol methane rate of loss shown in figure, comprises absorption tower 100 and middle pressure flashing tower 200.
On absorption tower, 100 top is provided with a clean gas outlet 110, and top is provided with a methyl alcohol lean solution entrance 120, and bottom is provided with one containing methane crude synthesis gas entrance 130, is provided with sulfur-bearing rich methanol taphole 140 at the bottom of tower.On absorption tower, 100 inside are at least provided with desulfurization section tower reactor 150, decarbonization section tower reactor 160 and cooling section tower reactor 170 from the bottom to top; In decarbonization section tower reactor 160 and cooling section tower reactor 170, be provided with water cooler 161,171.
On the bottom of decarbonization section tower reactor 160, be also provided with in addition rich CO
2methanol solution outlet 162; On desulfurization section tower reactor 150 tops, be provided with after desulfurization containing methane crude synthesis gas outlet 151 and rich CO
2methanol solution return port 152.
At methyl alcohol lean solution entrance 120, connect a methyl alcohol lean solution intake pipeline 121, this methyl alcohol lean solution intake pipeline 121 connects Mathanol regenerating workshop section.
On clean gas outlet 110, connect a purified gas export pipeline 111, purified gas export pipeline 111 is connected to downstream unit.
Containing methane crude synthesis gas entrance 130, connect a crude synthesis gas intake pipeline 131, crude synthesis gas intake pipeline 131 is connected to upstream changing device.
Middle pressure flashing tower 200 is divided in upper and lower two sections presses flash distillation tower reactor 210,220, presses the top of flash distillation tower reactor 210 to be provided with a rich CO in epimere
2methanol solution entrance 211, bottom is provided with air lift gas inlet 212, and top is provided with air lift gas loop exit 213, and bottom is provided with the methanol solution outlet 214 after air lift.
In hypomere, press the top of flash distillation tower reactor 220 to be provided with a sulfur-bearing rich methanol solution entrance 221, bottom is provided with air lift gas loop head 222, and top is provided with by air lift pneumatic outlet 223 out, and bottom is provided with the methanol solution outlet 224 after air lift.
After the desulfurization on desulfurization section tower reactor 150 tops on absorption tower 100, containing methane crude synthesis gas outlet 151, in the epimere by air lift gas line of pipes 310 and middle pressure flashing tower 200, press the air lift gas inlet 212 of flash distillation tower reactor 210 to be connected.
Rich CO on decarbonization section tower reactor 160 bottoms
2in methanol solution outlet 162, connect the rich CO of two-way
2methanol solution line of pipes 320,330, the wherein rich CO in a road
2methanol solution line of pipes 320 is connected to the rich CO on desulfurization section tower reactor 150 tops
2methanol solution return port 152, the rich CO in another road
2methanol solution line of pipes 330 is connected to the rich CO that presses flash distillation tower reactor 210 tops in the epimere of middle pressure flashing tower 200 by water cooler 331, reducing valve 332
2methanol solution entrance 211.
In the epimere of middle pressure flashing tower 200, press the air lift gas loop exit 213 at flash distillation tower reactor 210 tops by air lift gas recirculation pipework 340, to be connected to the air lift gas loop head 222 of pressing flash distillation tower reactor 220 bottoms in the hypomere of middle pressure flashing tower 200.
The sulfur-bearing rich methanol taphole 140 of 100 bottoms, absorption tower is connected to the sulfur-bearing rich methanol solution entrance 221 of pressing flash distillation tower reactor 220 tops in the hypomere of middle pressure flashing tower 200 by sulfur-bearing rich methanol solution conveyor tube line 350, water cooler 351, reducing valve 352.
In the hypomere of middle pressure flashing tower 200, press flash distillation tower reactor 220 tops by air lift pneumatic outlet 223 out by by air lift air shooter line 360, circulator compressor 361, water cooler 362 out, be connected to 100 bottoms, absorption tower containing methane crude synthesis gas entrance 130.
In upper and lower two sections, press the methanol solution outlet 214,224 after the air lift of flash distillation tower reactor 210,220 bottoms by the methanol solution line of pipes 370,380 after air lift, to be connected to methanol solution regenerative section respectively.
Principle of work of the present utility model is as follows:
From upstream changing device outlet containing methane crude synthesis gas by crude synthesis gas intake pipeline 131, the decarbonization section tower reactor 160, the desulfurization section tower reactor 150 that enter in the absorption tower 100 of low-temperature rectisol remove CO
2, H
2after S, the clean gas outlet 110 through the cooled purified gas of cooling section tower reactor 170 100 tower tops from absorption tower flows out and enters downstream unit through purified gas export pipeline 111 again.
The rich CO of the decarbonization section tower reactor 160 in absorption tower 100
2methanol solution outlet 162 rich co2 methanol solution out contains absorbed methane.This rich CO
2methanol solution is divided into two strands: one is by rich CO
2the rich CO on methanol solution line of pipes 320 and desulfurization section tower reactor 150 tops
2methanol solution return port 152 flows in the desulfurization section tower reactor 150 of desulfurization section tower reactor 150, as the washing methyl alcohol of desulfurization section tower reactor 150, absorbs the H in crude synthesis gas
2s.One is through rich CO in addition
2after methanol solution line of pipes 330, water cooler 331 are cooling, through reducing valve 332, be decompressed to 10barG left and right again, in the epimere by middle pressure flashing tower 200, press the rich CO on flash distillation tower reactor 210 tops
2methanol solution entrance 211 enters to press in epimere and in flash distillation tower reactor 210, carries out air lift.
Through the desulfurization section tower reactor 150 in absorption tower 100, absorb H
2s and part CO
2rear formation sulfur-bearing rich methanol solution, from desulfurization section tower reactor 150, flow out, and send through sulfur-bearing rich methanol taphole 140, the sulfur-bearing rich methanol solution conveyor tube line 350 of 100 bottoms, absorption tower, the sulfur-bearing rich methanol solution of sending is decompressed to about 10barG through reducing valve 332 again after supercooler 331 is cooling, then in hypomere, presses the sulfur-bearing rich methanol solution entrance 221 on flash distillation tower reactor 220 tops to send into press in hypomere and in flash distillation tower reactor 220, carry out air lift.
Crude synthesis gas one desulfurization sending containing methane crude synthesis gas outlet 151 after by the desulfurization at desulfurization section tower reactor 150 tops extracted at desulfurization section tower reactor 150 tops in absorption tower 100 out, then to entering, presses the rich CO in flash distillation tower reactor 210 through pressing the air lift gas inlet 212 of flash distillation tower reactor 210 to enter at the bottom of the tower of pressing flash distillation tower reactor 210 in epimere in air lift gas line of pipes 310 and epimere in epimere
2methanol solution carries out air lift.Due to gas stripping, rich CO
2methane, CO2 in methanol solution separate from solution.
The air lift gas loop exit 213 of pressing flash distillation tower reactor 210 in section being pressed in flash distillation tower reactor 220 by pressing the air lift gas loop head 222 of flash distillation tower reactor 220 bottoms to enter into hypomere in air lift gas recirculation pipework 340 and hypomere by air lift gas out out, air lift enters and in hypomere, presses methane, the CO in the interior sulfur-bearing rich methanol solution of flash distillation tower reactor 220 again
2.In hypomere, press gas after flash distillation tower reactor 220 air lifts by hypomere, press flash distillation tower reactor 220 tops by pneumatic outlet 223 out of air lift and by air lift air shooter line 360 out, delivered to circulator compressor 361 and compress, after cooling by water cooler 362 after compression, by 100 bottoms, absorption tower containing methane crude synthesis gas entrance 130 with from upstream changing device outlet, contain methane crude synthesis gas and mix and together enter absorption tower 100 towers at the bottom of.
In upper and lower two sections, pressing methanol solution after methanol solution outlet 214,224 after the air lift of flash distillation tower reactor 210,220 bottoms air lift out by the methanol solution line of pipes 370,380 after air lift, to deliver to methanol solution regenerative section respectively regenerates.
By above-mentioned measure, to reach, improve methane in the rate of recovery of low temperature washing device for methanol.
Claims (1)
1. a device that reduces low-temperature rectisol methane rate of loss, is characterized in that, comprising:
One absorption tower, described absorption tower at least has clean gas outlet, a superposed methyl alcohol lean solution entrance that is positioned at tower top, is positioned at the sulfur-bearing rich methanol taphole containing methane crude synthesis gas entrance and at the bottom of being positioned at tower of bottom, in inside, described absorption tower, is at least provided with from the bottom to top desulfurization section tower reactor, decarbonization section tower reactor and cooling section tower reactor; On the bottom of decarbonization section tower reactor, be also provided with rich CO
2methanol solution outlet; On desulfurization section tower reactor top, be provided with exporting and rich CO containing methane crude synthesis gas after desulfurization
2methanol solution return port; At described methyl alcohol lean solution entrance, connect a methyl alcohol lean solution intake pipeline, on described clean gas outlet, connect a purified gas export pipeline, described purified gas export pipeline is connected to downstream unit, the described methane crude synthesis gas entrance that contains connects a crude synthesis gas intake pipeline, and described crude synthesis gas intake pipeline is connected to upstream changing device;
In one, press flashing tower, described middle pressure flashing tower is divided in upper and lower two sections presses flash distillation tower reactor, presses the top of flash distillation tower reactor to be provided with a rich CO in described epimere
2methanol solution entrance, bottom is provided with air lift gas inlet, and top is provided with air lift gas loop exit, and bottom is provided with the methanol solution outlet after air lift; In described hypomere, press the top of flash distillation tower reactor to be provided with a sulfur-bearing rich methanol solution entrance, bottom is provided with air lift gas loop head, and top is provided with by air lift pneumatic outlet out, and bottom is provided with the methanol solution outlet after air lift;
Being connected with pressing the air lift gas inlet of flash distillation tower reactor in described epimere by air lift gas line of pipes containing the outlet of methane crude synthesis gas after the desulfurization on described desulfurization section tower reactor top; Rich CO on described decarbonization section tower reactor bottom
2the upper rich CO of two-way that connects of methanol solution outlet
2methanol solution line of pipes, the wherein rich CO in a road
2methanol solution line of pipes is connected to the rich CO on desulfurization section tower reactor top
2methanol solution return port, the rich CO in another road
2methanol solution line of pipes is connected to the rich CO that presses flash distillation tower reactor top in described epimere by the first water cooler, the first reducing valve
2methanol solution entrance, presses the air lift gas loop exit at flash distillation tower reactor top by air lift gas recirculation pipework, to be connected to the air lift gas loop head of pressing flash distillation tower reactor bottom in described hypomere in described epimere; The sulfur-bearing rich methanol taphole of bottom, described absorption tower is connected to the sulfur-bearing rich methanol solution entrance of pressing flash distillation tower reactor top in described hypomere by sulfur-bearing rich methanol solution conveyor tube line, the second water cooler, the second reducing valve; In described hypomere, press flash distillation tower reactor top by air lift pneumatic outlet out by by air lift air shooter line, circulator compressor, the 3rd water cooler out, be connected to bottom, described absorption tower containing methane crude synthesis gas entrance; In described upper and lower two sections, press the methanol solution outlet after the air lift of flash distillation tower reactor bottom by the methanol solution line of pipes after first, second air lift, to be connected to methanol solution regenerative section respectively.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104437004A (en) * | 2014-11-25 | 2015-03-25 | 赛鼎工程有限公司 | Method suitable for controlling concentration of hydrogen sulfide tail gas in low-temperature methanol washing process |
| CN104857817A (en) * | 2015-05-12 | 2015-08-26 | 湖北双环科技股份有限公司 | Low temperature methanol washing gas stripping regeneration methyl alcohol equipment and utilization method thereof |
| CN107011950A (en) * | 2016-01-28 | 2017-08-04 | 惠生工程（中国）有限公司 | A kind of method for gas purification for coal base synthesis of natural device of air |
| CN109999617A (en) * | 2019-03-15 | 2019-07-12 | 中国天辰工程有限公司 | The technique of CO concentration in a kind of reduction low-temperature methanol washing tail-gas |
| CN111004082A (en) * | 2018-10-08 | 2020-04-14 | 中国石油化工股份有限公司 | System and method for removing carbon dioxide from C2 fraction |
| CN112625761A (en) * | 2020-12-01 | 2021-04-09 | 中国五环工程有限公司 | Process for removing low-partial pressure acid gas in low-pressure feed gas by using low-temperature methanol |
-
2014
- 2014-06-11 CN CN201420309957.XU patent/CN203923123U/en active Active
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104437004A (en) * | 2014-11-25 | 2015-03-25 | 赛鼎工程有限公司 | Method suitable for controlling concentration of hydrogen sulfide tail gas in low-temperature methanol washing process |
| CN104437004B (en) * | 2014-11-25 | 2016-04-06 | 赛鼎工程有限公司 | The method of hydrogen sulfide tail gas concentration is controlled in a kind of applicable low-temperature rectisol process |
| CN104857817A (en) * | 2015-05-12 | 2015-08-26 | 湖北双环科技股份有限公司 | Low temperature methanol washing gas stripping regeneration methyl alcohol equipment and utilization method thereof |
| CN107011950A (en) * | 2016-01-28 | 2017-08-04 | 惠生工程（中国）有限公司 | A kind of method for gas purification for coal base synthesis of natural device of air |
| CN107011950B (en) * | 2016-01-28 | 2019-12-27 | 惠生工程（中国）有限公司 | Gas purification method for coal-based natural gas synthesis device |
| CN111004082A (en) * | 2018-10-08 | 2020-04-14 | 中国石油化工股份有限公司 | System and method for removing carbon dioxide from C2 fraction |
| CN109999617A (en) * | 2019-03-15 | 2019-07-12 | 中国天辰工程有限公司 | The technique of CO concentration in a kind of reduction low-temperature methanol washing tail-gas |
| CN112625761A (en) * | 2020-12-01 | 2021-04-09 | 中国五环工程有限公司 | Process for removing low-partial pressure acid gas in low-pressure feed gas by using low-temperature methanol |
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