CN85105457A - Remove the method for acidic components in the air-flow - Google Patents
Remove the method for acidic components in the air-flow Download PDFInfo
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- CN85105457A CN85105457A CN 85105457 CN85105457A CN85105457A CN 85105457 A CN85105457 A CN 85105457A CN 85105457 CN85105457 CN 85105457 CN 85105457 A CN85105457 A CN 85105457A CN 85105457 A CN85105457 A CN 85105457A
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- solvent
- gas
- desulfurization
- flow
- acidic components
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Abstract
The present invention is a kind of method that removes acidic components in the air-flow.It is used in and adds the selection of depressing such as lightweight oil, sulfide and carbonic acid gas in Sweet natural gas, synthetic gas, the town gas and remove, or removes simultaneously.Removing of acidic components of the present invention is to adopt trivalent alcohol, propylene carbonate and weak polyvalent mineral acid, the efficient physical lyosorption that N methyldiethanol amine is formed to realize under corresponding device thereof and processing condition.This technology than other purifying method have that flow process is simple, energy consumption is little, the day-to-day operation expense is low, solvent is easy to get, cheaply, characteristics such as no burn into is nontoxic.
Description
The present invention is a kind of method that removes acidic components in the air-flow.Specifically, the present invention is that the employing physical solvent is that absorption agent selects to remove the CO in the acid gas stream
2, H
2The method of S and multiple organic sulfide.The air-flow of indication of the present invention can be Sweet natural gas, synthetic gas and pressurization town gas or the like.
The physical solvent absorption agent can be depressed adding, and removes the acidic components in the air-flow more economically.Multiple different physical solvent process is developed, and has applied for patent by the inventor.Certain methods demonstrates gratifying in various degree result by application feature separately, as Rectisol method, Fluor method and Selexol method etc.In these methods, the need that have could show bigger benefit at low temperatures, the technical process complexity that is complementary with it simultaneously, and cost of equipment is big, management and operative technique difficulty are higher, and solvent is toxic; Have then to H
2It is bad that S absorbs selectivity; The solvent that some adopted costs an arm and a leg, thereby its application is restricted.
Task of the present invention be provide that a kind of solvent is easy to get, solvent low price, chemistry and thermal stability be good, steam forces down, it is nontoxic not have burn into, to sour gas H particularly
2The S absorptive capacity is big, degree of purification height, H
2S can reach 0.1ppm, and technical process is simple, and the low method that removes acidic components consumes energy.
The pure carbon acid propylene ester solvent that is adopted in United States Patent (USP) 2926751-3 is made absorption agent, is referred to as the Fluor method.Recently it is applied in Large Scale Synthetic Ammonia Plants and removes CO
2In the process, the low potential energy heat of saving as ammonia absorption refrigeration, be it is said to make synthetic ammonia ton ammonia energy consumption reduce about 10%.But the Fluor method removes H
2The S ability is little, at CO
2Exist down H
2S selects receptivity poor.Can not satisfy higher concentration H
2S removes requirement.
The solvent that the present invention uses is by trivalent alcohol such as glycerol 2-85%; Weak polyvalent mineral acid is as phosphoric acid 0.2-4%; N methyldiethanol amine 0.5-8%, all the other are propylene carbonate, the solvent of being formed removes the acidic components in the air-flow.
The present invention depresses adding, and the acidic components in the air-flow is removed.It takes off the process of releasing and follows Henry's law substantially, and pressure is higher, and temperature is low, more helps the absorption of sour gas, disengages from solvent otherwise then help sour gas.
In order more clearly to describe this processing method, provide following accompanying drawing to be illustrated: by pipe 1 enter thionizer 2 bottoms greater than 8 atmospheric unstripped gass, and by the solvent of cat head spray counter current contact in packing layer at normal temperatures, with H
2S is from 5-7 gram/mark rice
3Be removed to 1-20 milligram/mark rice
3Decarbonizing tower 14 bottoms are sent into by pipe 3 in the back.Sulfide and a small amount of CO have been absorbed
2Solvent, by discharging at the bottom of the thionizer, enter 5 vacuum flashings of intermediate flash device through managing 4, will be dissolved in that most of valuable gases discharges after press 6 is delivered to pipe 1 in the solvent.Solvent after the flash distillation is after the desulfurization lean solution heat exchange of interchanger 12 and heat, heater via 7 is heated to 80-120 ℃ and enters stripping tower 8 tops again, with the rare gas element that well heater 10 is heated to 80-120 ℃ that passes through that enters by the stripping tower bottom, counter current contact in packing layer, the sour gas that makes it to be dissolved in the solvent thoroughly discharges, and solvent is regenerated.The sour gas that discharges enters the stripping tower middle part along with rare gas element is discharged by the stripping cat head together after condensation separator 9 reclaims solvent, gas then is discharged processing.Solvent behind the stripping enters interchanger 12 successively after lean pump 11 pressurizations and water cooler 13 is squeezed into thionizer 2 tops, makes it solvent cycle and uses.The gas of the pre-desulfurization of warp enters decarbonizing tower 14 and removes CO
2With smart desulfurization.When decarburization pressure greater than 18 normal atmosphere, adopt normal temperature and CO during with the air stripping
2Can take off to 0.5% H
2S can reach 0.1PPm.Be product gas from the decarbonizing tower expellant gas, carry by managing 17.Rich solution is gone into 15 vacuum flashings of intermediate flash device by the decarbonizing tower underflow, and flashed vapour is sent into pipe 3 by press 16, and the solvent after the flash distillation enters normal pressure Jie haustorium 18, discharges a large amount of high concentration COs
2, to discharge by pipe 22, solvent then enters stripping tower 19 by U type pipe.If need the more CO of recovery
2, then can be earlier through vacuum Jie sucking-off CO
2After, again solvent is sent into stripping tower top and used by pipe 20 air and in packing layer, carry out stripping, make solvent be able to thoroughly the regeneration back and squeeze into decarbonizing tower 14 by pump 21 and recycle.
Present method also can remove the lightweight oil in the lurgi gas effectively under not influencing desulfurization, decarburization efficient, and need not to add extra oil product and separate and extraction plant, and the only employing that separates of oil and solvent is simply come down in torrents and got final product; H in flow of process air
2S content≤3.0 gram/marks rice
3, or H
2S concentration is higher, but does not need essence to take off, and can need not to heat steam stripping regeneration.
The present invention is to H
2It is big approximately more than 50% than the Fluor solvent method that S removes ability, and solvent saturation steam pressure ratio Fluor solvent reduces 30-80%, and this law is specially adapted to remove the H in the gas
2S or remove CO simultaneously
2Occasion, and can obtain best economical effectiveness.
Table 1. is and Fluor solvent contrast information slip:
| Method name | CO 2Solubleness | H 2S solubleness | The solvent price | Solvent loss |
| Fluor | 1.0 | 1.0 | 1 | 1 |
| Present method | ～1.0 | 1.5-3.0 | 0.9-1.05 | 0.2-0.7 |
Further specify process of the present invention below
Example: table 2 is the relevant physicochemical data of present method solvent of being prepared in above-mentioned compositing range:
Density (grams per milliliter) 1.200
Viscosity (centipoise) 4.86
Specific heat (card/gram ℃) 0.4
Surface tension (dynes per centimeter) 41.75
Saturated vapor pressure (mmhg) 0.034
CO
2(the mark rice of equilibrium solubility in solvent
3/ rice
3) 3.35
H
2S is balance solubility (mark rice in solvent
3/ rice
3) under 40 ℃ of 760 mmhg 12.3
Except that the temperature of indicating, pressure, be 25 ℃, 760 mmhg in the table 2.
Adopt the solvent of being formed in the example, utilize and generally once remove flow process H in the synthetic-ammonia transformation gas
2S, CO
2Removing the result with sulfide in the Sweet natural gas is listed as table 3:
Table 3.
Claims (4)
1, this patent is a kind of processing method that removes acidic components in the air-flow, it is characterized in that the solvent that uses is by trivalent alcohol such as glycerol 2-85%; Weak polyvalent mineral acid is as phosphoric acid 0.2-4%; N methyldiethanol amine 0.5-8%; A kind of special physical solvent that all the other are formed for propylene carbonate.
2, according to the solvent that is adopted in the claim 1, the present invention can be at normal temperatures, absorption pressure 〉=8 normal atmosphere, and in the steam stripped mode of rare gas element, by pre-desulfurization, the flow process of decarburization again can be with H in the unstripped gas under 80-120 ℃ for desulfurization regeneration
2S is from 6-7 gram/mark rice
3Be removed to 0.1-0.5ppm; Adopt the once desulfurization flow process,, when absorbing vapour-liquid ratio 180-200, can make H in the unstripped gas at 20 normal atmosphere
2S is from 6.4 gram/marks rice
3Be removed to 1 milligram/mark rice
3, mercaptan is from 150 milligrams/mark rice
3Be removed to 1 milligram/mark rice
3Below.
3, the present invention can remove lightweight oil in the coal gas in pre-desulfurization simultaneously, adopts simple decantation the strippings in the solvent can be separated, and the solvent that dissolves a small amount of light oil is had no effect to desulfurization performance.
4, according to the corresponding viscosity of the solvent that claim 1 adopted, severe, specific heat, saturated vapor pressure, surface tension and sour gas data such as equilibrium solubility in solvent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 85105457 CN85105457A (en) | 1985-07-15 | 1985-07-15 | Remove the method for acidic components in the air-flow |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 85105457 CN85105457A (en) | 1985-07-15 | 1985-07-15 | Remove the method for acidic components in the air-flow |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN85105457A true CN85105457A (en) | 1987-01-21 |
Family
ID=4794489
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 85105457 Pending CN85105457A (en) | 1985-07-15 | 1985-07-15 | Remove the method for acidic components in the air-flow |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN85105457A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102657998A (en) * | 2012-04-25 | 2012-09-12 | 中国石油化工股份有限公司 | Mixed solvent for removing acid gas |
-
1985
- 1985-07-15 CN CN 85105457 patent/CN85105457A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102657998A (en) * | 2012-04-25 | 2012-09-12 | 中国石油化工股份有限公司 | Mixed solvent for removing acid gas |
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