CN104436998A - Method for removing acid gas by adopting methanol as absorbent - Google Patents
Method for removing acid gas by adopting methanol as absorbent Download PDFInfo
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- CN104436998A CN104436998A CN201310422443.5A CN201310422443A CN104436998A CN 104436998 A CN104436998 A CN 104436998A CN 201310422443 A CN201310422443 A CN 201310422443A CN 104436998 A CN104436998 A CN 104436998A
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- gas
- methyl alcohol
- methanol
- absorbent
- tower
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Abstract
The present invention belongs to the field of gas processing, and provides a method for removing acid gas by adopting methanol as an absorbent. According to the present invention, the method is mainly characterized in that a pre-washing tower is designed in front of an absorption tower, and pre-washing is performed on raw material gas with a barren solution obtained from the original low temperature methanol washing device and with a temperature of about 30-40 DEG C, such that the raw material gas is dewatered and completely dried, and ammonia naphthalene, benzene and other components carried in the raw material gas are removed; the liquid on the bottom portion of the pre-washing tower enters a methanol water separation tower; and the gas on the top of the pre-washing tower enters a process gas cooler and then enters the absorption tower. With the method of the present invention, the problem of the impurity and the moisture carried by carried raw material gas before entering the absorption tower is solved, wherein the raw material gas is pre-washed, such that the raw material gas is dewatered and dried, and the impurity such as ammonia, naphthalene, benzene and the like are removed so as to make the subsequent treatment system stable.
Description
Technical field
The invention belongs to gas manufacture field, relate to methyl alcohol removes sour gas method as absorbent, particularly adopt methyl alcohol to make the method for absorbent pre-wash unstrpped gas.
Background technology
Low-temp methanol washing process is the 1950's by a kind of Physical Absorption method gas purifying technique of German Linde Co and LURGI's joint development, this technique take low-temp methanol as lyosoption, utilize methyl alcohol at low temperatures to the great characteristic of sour gas solubility, remove the sour gas in unstripped gas.Low-temperature rectisol process for purifying can remove the H in unstripped gas
2s, COS, RSH, CO
2etc. various ingredients, and can dewater and make gas finish-drying; Meanwhile, methyl alcohol chemical stability and better heat stability, methyl alcohol viscosity is less, in operating process, methyl alcohol is non-foaming, pure methyl alcohol does not corrode e-quipment and pipe, so for a long time, methanol cleaning process is widely used in the fields such as synthetic ammonia, synthesizing methanol, coal to SNG, IGCC.
The typical process flow of woods moral low-temperature rectisol process for purifying is described below: the unstripped gas of upstream enters absorption tower through cooling after being separated, for preventing freezing in cooling procedure, first inject a small amount of methyl alcohol before cooling, isolated methyl alcohol and aqueous mixtures send methanol-water separating to be separated.Top, absorption tower adds low-temp methanol and absorbs CO
2, a lower tower part is containing CO
2methanol absorption H
2s and COS, this portion washes liquid accounts for about 52% of whole cleaning solution.Purified gas transports to subsequent handling by tower top.
Solution is at absorption H
2s and CO
2the a part of H of simultaneously stability in process
2with CO, reclaimed by vacuum flashing.CO in flash liquid
2major part is at CO
2desorber or H
2n is used in S concentration tower
2air lift is gone out, and makes H in solution
2s relative concentration improves, for making the CO after desorb
2substantially not sulfur-bearing in emptying end gas after gas product and air lift, at CO
2the top of desorber and stripping tower is with not sulfur-bearing but containing a certain amount of CO
2methanol solution washing.
H is rich in after concentrated
2hot recycling tower is sent thoroughly to regenerate after the low-temperature methanol solution of S and poor methanol heat exchange, the H of hot recycling top of tower
2s, CO
2, methanol steam mixture by a series of cooler, methanol condensed is got off.Liquid enters backflash, H
2s rich gas finally sends battery limit (BL) to sulfur recovery unit in heat exchanger after re-heat.Obtain poor methanol at the bottom of tower, after cooling, deliver to absorption tower top.Supplementary cold needed for device is provided by refrigeration system.
The low-temperature rectisol flow process of LURGI is different, but technical characterstic is all similar or identical, all comprises absorption and regenerative system, comprises middle pressure flash distillation and reclaim effective gas, CO
2desorb, N
2air lift, hot recycling tower is separated with methanol/water, but has certain difference on Type of equipment and flowage structure.
Domesticly quite a lotly at present mostly select low-temp methanol washing process at process units such as building large-scale coal synthesis ammonia, ammonia from coal, coal to SNG.
While the factory that low-temperature rectisol technology is raw material with coal, heavy oil, pitch at home obtains extensive application, in production, also expose some problems, as total sulfur in purified gas exceed standard, the problem such as system water content is high, ammonia content is high in system corrosion, system.
Summary of the invention
The object of the invention is to solve unstripped gas enter absorption tower before the impurity carried and moisture problem, namely pre-wash carried out to unstripped gas, unstripped gas dehydrated and by the impurity such as removing such as ammonia, naphthalene, system just can be more stable in subsequent treatment for such unstripped gas, and impurity also can not have an impact to purified gas degree of purification.
Main technical schemes of the present invention is: before absorption tower, increase prewashing column, the lean solution of about 30-40 DEG C that obtains from former low temperature washing device for methanol carries out pre-wash to unstripped gas, unstripped gas is dewatered fully dry, remove the component such as ammonia naphthalene, benzene of carrying in unstripped gas; Liquid bottom prewashing column enters methanol-water separating; Absorption tower is entered after the gas of prewashing column tower top enters process gas cooler.
The inventive method solves the shortcoming containing impurity and water in unstripped gas, for the stable operation of low-temperature rectisol purification method creates condition.
For achieving the above object, the present invention takes following technical scheme usually:
(1) lean solution used is from former lean solution pipeline, carries with original pump;
(2) prewashing column is plate column or packed tower;
(3) methyl alcohol entering prewashing column is the poor methanol after heat exchange, and temperature is 30 ~ 40 DEG C;
(4) solution at the bottom of prewashing column enters methanol-water separating and reclaims methyl alcohol;
(5) gas of pre-wash tower top enters absorption tower after entering process gas cooler;
(6) after process gas cooler, methanol-water knockout drum need not be set.
Effect of the present invention and feature thoroughly eliminate the impurity such as ammonia, naphthalene, benzene contained in unstripped gas.
Accompanying drawing explanation
Accompanying drawing 1 is low-temperature rectisol technology typical production general flow chart (absorption portion); Accompanying drawing 2 is embodiment of the present invention method process flow diagrams.
In figure, 1-process gas cooler; 2-methanol-water knockout drum; 3-absorption tower; 4-prewashing column.
Detailed description of the invention
The specific embodiment of the present invention is described in detail below in conjunction with technical scheme and accompanying drawing.
Accompanying drawing 1 is existing techniqueflow, the temperature 40 DEG C that shift conversion step comes, and pressure is 5.4MPaA, containing H
253.76%, CO
244.77%, H
2s+COS 0.22%, N
20.3%, CO 0.77%, H
2the unstripped gas of O 0.18% first contacts with spray methyl alcohol before entering process gas cooler 1 heat exchange, prevent from freezing, unstripped gas enters in methanol-water knockout drum 2 after cooling in process gas cooler 1 and carries out gas-liquid separation, and gas phase enters absorption tower 3 and carries out mass transfer absorption, and tower top is purified gas.Liquid phase enters methanol-water separating and reclaims methyl alcohol.The deficiency of this flow process is that the impurity such as ammonia, naphthalene contained in conversion gas cannot effectively remove, and builds up, affect the quality of purified gas in low-temperature rectisol lean solution, stablizing of influential system.
Embodiment: accompanying drawing 2 is the techniqueflow of embodiment.
The temperature 40 DEG C that shift conversion step comes, pressure is 5.4MPaA, containing H
253.76%, CO
244.77%, H
2s+COS 0.22%, N
20.3%, CO 0.77%, H
2the unstripped gas of O 0.18% is introduced into bottom prewashing column 4, and the methyl alcohol counter current contacting of 30 ~ 40 DEG C that spray with tower top, removes the impurity in unstripped gas and moisture.The gas of prewashing top of tower, after process gas cooler 1 is cooled to-13 DEG C, enters absorption tower 3.After this, process by rectisol method.The solution of prewashing column 4 tower bottom enters methanol-water separating as charging.After the method process, the impurity such as the ammonia contained in unstripped gas, naphthalene, benzene can not be accumulated in systems in which, eliminate the impact of impurity on rectisol system.
Claims (7)
1. a methyl alcohol removes the method for sour gas as absorbent, it is characterized in that: before absorption tower, increase prewashing column, the lean solution of 30 ~ 40 DEG C that obtain from former low temperature washing device for methanol carries out pre-wash to unstripped gas, unstripped gas is dewatered fully dry, and remove ammonia, naphthalene, the benzene component of carrying in unstripped gas; Liquid bottom prewashing column enters methanol-water separating; Absorption tower is entered after the gas of prewashing column tower top enters process gas cooler.
2. the methyl alcohol according to claims 1 removes the method for sour gas as absorbent, it is characterized in that lean solution used is from former lean solution pipeline, carries with original pump.
3. the methyl alcohol according to claims 1 removes the method for sour gas as absorbent, it is characterized in that prewashing column is plate column or packed tower.
4. the methyl alcohol according to claims 1 removes the method for sour gas as absorbent, and the methyl alcohol that it is characterized in that entering prewashing column is the poor methanol after heat exchange, and temperature is 30 ~ 40 DEG C.
5. the methyl alcohol according to claims 1 removes the method for sour gas as absorbent, it is characterized in that the solution at the bottom of prewashing column enters methanol-water separating recovery methyl alcohol.
6. the methyl alcohol according to claims 1 removes the method for sour gas as absorbent, it is characterized in that the gas of pre-wash tower top enters absorption tower after entering process gas cooler.
7. the methyl alcohol according to claims 1 removes the method for sour gas as absorbent, does not arrange methanol-water knockout drum after it is characterized in that process gas cooler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310422443.5A CN104436998A (en) | 2013-09-17 | 2013-09-17 | Method for removing acid gas by adopting methanol as absorbent |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310422443.5A CN104436998A (en) | 2013-09-17 | 2013-09-17 | Method for removing acid gas by adopting methanol as absorbent |
Publications (1)
| Publication Number | Publication Date |
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| CN104436998A true CN104436998A (en) | 2015-03-25 |
Family
ID=52884214
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| CN201310422443.5A Pending CN104436998A (en) | 2013-09-17 | 2013-09-17 | Method for removing acid gas by adopting methanol as absorbent |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN105861027A (en) * | 2016-05-27 | 2016-08-17 | 无锡市湖晨石化设备有限公司 | Process system for recycling HCl and gasoline blending components from light hydrocarbon gas |
| CN106039762A (en) * | 2016-07-06 | 2016-10-26 | 山西潞安煤基合成油有限公司 | Method and device for improving extraction effect of prewashed methanol during low-temperature methanol washing |
| CN107754558A (en) * | 2016-08-19 | 2018-03-06 | 中国石油化工股份有限公司 | A kind of NHD desulfurization concentrating method |
| 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 |
| CN114471088A (en) * | 2021-12-30 | 2022-05-13 | 浙江中控技术股份有限公司 | Low-temperature methanol washing process CO2Concentration control method and system |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN105861027A (en) * | 2016-05-27 | 2016-08-17 | 无锡市湖晨石化设备有限公司 | Process system for recycling HCl and gasoline blending components from light hydrocarbon gas |
| CN106039762A (en) * | 2016-07-06 | 2016-10-26 | 山西潞安煤基合成油有限公司 | Method and device for improving extraction effect of prewashed methanol during low-temperature methanol washing |
| CN107754558A (en) * | 2016-08-19 | 2018-03-06 | 中国石油化工股份有限公司 | A kind of NHD desulfurization concentrating method |
| CN107754558B (en) * | 2016-08-19 | 2020-10-20 | 中国石油化工股份有限公司 | Desulfurization and concentration method of polyethylene glycol dimethyl ether |
| 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 |
| CN114471088A (en) * | 2021-12-30 | 2022-05-13 | 浙江中控技术股份有限公司 | Low-temperature methanol washing process CO2Concentration control method and system |
| CN114471088B (en) * | 2021-12-30 | 2023-01-10 | 浙江中控技术股份有限公司 | Low-temperature methanol washing process CO 2 Concentration control method and system |
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Application publication date: 20150325 |
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