CN107754558A - A kind of NHD desulfurization concentrating method - Google Patents
A kind of NHD desulfurization concentrating method Download PDFInfo
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- CN107754558A CN107754558A CN201610689196.9A CN201610689196A CN107754558A CN 107754558 A CN107754558 A CN 107754558A CN 201610689196 A CN201610689196 A CN 201610689196A CN 107754558 A CN107754558 A CN 107754558A
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- gas
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
- B01D2252/2023—Glycols, diols or their derivatives
- B01D2252/2026—Polyethylene glycol, ethers or esters thereof, e.g. Selexol
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Industrial Gases (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of NHD desulfurization concentrating method, it is characterised in that：Using the difference of the parameters such as the operation temperature of absorption tower and concentration tower, pressure and gas liquid ratio, the concentrate of sweetening process is realized, and ensures that concentration of hydrogen sulfide is more than 40% in regeneration acid gas, concentration of hydrogen sulfide is less than 10ppm in tail gas.It solves the problems such as low current NHD sulfur removal technology regeneration gas concentration, Hydrogen Sulfide Tail Gas content overproof, atmosphere pollution is serious, has the advantages that method simplicity, environment-friendly high-efficiency, resource recovery are high.
Description
Technical field
The invention belongs to the refined manufacture field of industrial gasses, is related to a kind of NHD desulfurization concentrating method,
Specifically, using the difference of the operation temperature on concentration tower and absorption tower, pressure and gas liquid ratio, the concentrate of sweetening process is realized,
And ensureing that concentration of hydrogen sulfide is more than 40% in regeneration acid gas, concentration of hydrogen sulfide is less than 10ppm in tail gas.
Background technology
NHD solution is a kind of Physical Absorption solvent, and its main component is the homology of more glycol dimethyl ethers
Thing, the external and country is based respectively on NHD solution and develops Selexol and NHD purification techniques, due to suction
The features such as receipts ability is strong, selectivity is high, steam forces down, non-corrosiveness, is widely used in the mixed gas such as synthesis gas, fuel gas
H2S、CO2With the absorption of the component such as COS.
NHD desulfurization and decarbonization process are similar to traditional absorption technique, mainly including absorption tower, desorption
The equipment such as tower, flash tank, heat exchanger.For in order to meet the requirement of subsequent treatment, process modification is not concentrated mainly on hydrogen sulfide
In concentrate research.
Chinese patent CN101077467 discloses a kind of optimization extracting and concentrating technology of polyethyleneglycol dimethyl ether desulfurizing system.It is logical
Cross and the NHD rich solutions for absorbing hydrogen sulfide are sent into flash tank, the gas pressurized flashed off delivers to regenerator, carrys out concentrate and regenerate
The acid gas come, can solve current NHD same gas raw material and design objective, and various improved flows are developed.For poly-
Glycol dimethyl ether sulfur removal technology,
The problems such as desulphurization system flash process desulfurization degree is low, atmosphere pollution is serious, regenerator heat consumption is higher, there is method simplicity,
The advantages that maximization purpose of achievable environment protection treating, raising cleaning system sulfur recovery rate, implementation Product recycling and the utilization of resources.
Chinese patent CN 101492616 discloses a kind of desulfurization and decarburization integrated absorption process for polyglycol dimethyl ether.Pass through
Absorption tower is transformed, NHD desulfurization and decarburization are completed in an absorption tower, is segmented and is absorbed in absorption tower, together
Mono- concentration tower of Shi Zengshe, the acid gas come out to regeneration overhead concentrate, the H after concentration2S can reach more than 70%.The technique
Have the advantages that system circulation amount is small, running device is few, reasonable energy utilization, easy to operate, reduced investment, suitable for methanol processed,
Synthesize the cleaning system of ammonia or other gas processed.
But existing NHD sulfur removal technology be although can meet the needs of hydrogen sulfide concentrate, concentration tower, sudden strain of a muscle
The hydrogen sulfide content steamed in the equipment exhausting tail gas such as groove is usually exceeded, can not meet the requirement of discharge standard, this is greatly limited
The popularization of NHD desulfurization technology.
The content of the invention
It is an object of the invention to propose a kind of NHD desulfurization concentrating method, by controlling absorption tower and carrying
Operation temperature, pressure and the gas liquid ratio of dense tower, the concentrate of sweetening process is realized, concentration of hydrogen sulfide exceedes in ensureing to regenerate acid gas
While 40%, hydrogen sulfide content in tail gas is down to below 10ppm, meets the requirement of exhaust emissions.
The NHD desulfurization extracting and concentrating technology of the present invention, its processing step are：（1）Unstripped gas is in raw material air cooling
Through with delivering to absorption tower after the purified gas heat exchange after absorption, counter current contacting being carried out with NHD solution in absorption tower, after desulfurization in device
Purified gas and entrance unstripped gas carry out heat exchange recovery cold to rear system；（2）Enter high pressure after the rich solution decompression at absorption tower bottom
Flash tank, flash off the Gas recovery of part hydrogen and carbon monoxide；（3）The liquid of high pressure flash groove exchanges heat with lean solution
Depressurize again afterwards into concentration tower bottom, carry out counter current contacting with NHD solution in concentration tower, the Hydrogen Sulfide Tail Gas content after concentrate
Below 10ppm is down to, can direct high altitude discharge；（4）The rich solution at concentration tower bottom is pressed into enter into regenerator certainly again after exchanging heat with lean solution
Row solution regenerates, and regenerator uses hot recycling, exports system after sour gas is delivered to after refrigerated separation, concentration of hydrogen sulfide>40%；
（5）The rich solution at regenerator bottom flows through heat exchanger and lean pump successively, is sent to respectively at the top of absorption tower and concentration tower.
Usually, in method provided by the invention, the Stress control of unstripped gas in 1.8 ~ 6.0MPa, temperature control 20 ~
40℃。
In method provided by the invention, absorption tower Stress control is in 1.8 ~ 6.0MPa, and temperature control is at 20 ~ 40 DEG C, gas-liquid
Than controlling 150 ~ 300.
In method provided by the invention, flash tank Stress control is in 0.8 ~ 1.8MPa.
In method provided by the invention, concentration tower Stress control is in 0.4 ~ 0.8MPa, and temperature control is at -10 ~ 20 DEG C, gas-liquid
Than controlling 50 ~ 150.
In method provided by the invention, regeneration column overhead temperatures control is at 100 ~ 110 DEG C.
Method provided by the invention, there is advantages below：
（1）Flow is simple, only comprising equipment such as absorption tower, flash tank, concentration tower, regenerator and heat exchangers, without multistage flash evaporation
Flow is produced with centre, is easy to production operation control；
（2）Can be by concentration of hydrogen sulfide concentrate in regeneration acid gas to more than 40%；
（3）Hydrogen sulfide content in tail gas can be down to below 10ppm, meet the requirement of exhaust emissions.
Brief description of the drawings
Fig. 1 is the process flow diagram of the embodiment of the present invention.
In figure, 1- unstripped gas heat exchanger 2- absorption towers 3- flash tank 4- poor rich liquid heat exchanger I 5- concentration towers
6- poor rich liquid heat exchanger II 7- regenerators 8- regeneration Gas Cooler 9- regeneration gas separating device 10- reflux pumps 11- is again
Boil device 12- lean pump I 13- lean solution cooler 14- lean pump II 15- lean solution coolers II.
Embodiment
With reference to specific embodiment, the invention will be further described.
The technological process of following examples is referring to accompanying drawing 1.
Embodiment 1
The method of the present embodiment has steps of：
（1）Unstripped gas（Sulfide hydrogen 1.2%, temperature 50 C, pressure 3.32MPa）In feed gas chiller with it is net after absorption
Absorption tower is delivered to after changing gas heat exchange, carries out counter current contacting with NHD solution in absorption tower, control absorption tower top lean solution enters material temperature
Spend for 40 DEG C, absorption tower top pressure is 3.01MPa, and absorption tower gas liquid ratio is 200, and the purified gas after desulfurization is entered with entrance unstripped gas
Row heat exchange reclaims cold to rear system；
（2）The rich solution at absorption tower bottom enters high pressure flash groove after being decompressed to 1.0MPa, flashes off part hydrogen and carbon monoxide
Gas be back to absorption tower porch；
（3）The liquid of high pressure flash groove enters concentration tower bottom with being decompressed to 0.6MPa again after lean solution heat exchange, in concentration tower and
NHD solution carries out counter current contacting, and the feeding temperature for controlling concentrate tower top lean solution is 10 DEG C, and concentrate tower top pressure is 0.4MPa, is carried
Dense tower gas liquid ratio is 80；
（4）The rich solution at concentration tower bottom carries out solution regeneration with being pressed into certainly again after lean solution heat exchange into regenerator, and regenerator uses heat again
It is raw, regenerator tower top pressure 0.13MPa is controlled, regenerates 103 DEG C of column overhead temperatures, regeneration overhead regeneration gas cooler outlet temperature
40℃；
（5）The rich solution at regenerator bottom flows through heat exchanger and lean pump successively, respectively with 40 DEG C, 3.7MPa and 10 DEG C, 1.0MPa
Condition is sent at the top of absorption tower and concentration tower.
Sampling analysis result：Purified gas hydrogen sulfide content 2.2ppm, Hydrogen Sulfide Tail Gas content 8.6ppm, regeneration acid gas vulcanization
Hydrogen content 45.3v%.
Embodiment 2
The method of the present embodiment has steps of：
（1）Unstripped gas（Sulfide hydrogen 0.9%, temperature 50 C, pressure 4.12MPa）In feed gas chiller with it is net after absorption
Absorption tower is delivered to after changing gas heat exchange, carries out counter current contacting with NHD solution in absorption tower, control absorption tower top lean solution enters material temperature
Spend for 40 DEG C, absorption tower top pressure is 3.81MPa, and absorption tower gas liquid ratio is 250, and the purified gas after desulfurization is entered with entrance unstripped gas
Row heat exchange reclaims cold to rear system；
（2）The rich solution at absorption tower bottom enters high pressure flash groove after being decompressed to 1.2MPa, flashes off part hydrogen and carbon monoxide
Gas be back to absorption tower porch；
（3）The liquid of high pressure flash groove enters concentration tower bottom with being decompressed to 0.7MPa again after lean solution heat exchange, in concentration tower and
NHD solution carries out counter current contacting, and the feeding temperature for control concentrate tower top lean solution is 0 DEG C, and concentrate tower top pressure is 0.5MPa, concentrate
Tower gas liquid ratio is 100；
（4）The rich solution at concentration tower bottom carries out solution regeneration with being pressed into certainly again after lean solution heat exchange into regenerator, and regenerator uses heat again
It is raw, regenerator tower top pressure 0.13MPa is controlled, regenerates 106 DEG C of column overhead temperatures, regeneration overhead regeneration gas cooler outlet temperature
40℃；
（5）The rich solution at regenerator bottom flows through heat exchanger and lean pump successively, respectively with 40 DEG C, 4.2MPa and 0 DEG C, 1.0MPa bar
Part is sent at the top of absorption tower and concentration tower.
Sampling analysis result：Purified gas hydrogen sulfide content 1.8ppm, Hydrogen Sulfide Tail Gas content 4.5ppm, regeneration acid gas vulcanization
Hydrogen content 41.2v%.
Claims (6)
1. a kind of NHD desulfurization concentrating method, it is characterized in that：Comprise the following steps：（1）Unstripped gas is in unstripped gas
Through with delivering to absorption tower after the purified gas heat exchange after absorption, carrying out counter current contacting with NHD solution in absorption tower, taking off in cooler
Purified gas after sulphur carries out heat exchange recovery cold to rear system with entrance unstripped gas；（2）Enter after the rich solution decompression at absorption tower bottom
High pressure flash groove, flash off the Gas recovery of part hydrogen and carbon monoxide；（3）The liquid and lean solution of high pressure flash groove
Depressurized again after heat exchange into concentration tower bottom, carry out counter current contacting with NHD solution in concentration tower, the Hydrogen Sulfide Tail Gas after concentrate
Content is down to below 10ppm, direct high altitude discharge；（4）The rich solution at concentration tower bottom with being pressed into regenerator certainly again after lean solution heat exchange
Solution regeneration is carried out, regenerator uses hot recycling, exports system after sour gas is delivered to after refrigerated separation, concentration of hydrogen sulfide>
40%；（5）The rich solution at regenerator bottom flows through heat exchanger and lean pump successively, is sent to respectively at the top of absorption tower and concentration tower.
2. NHD desulfurization concentrating method according to claim 1, it is characterized in that：The Stress control of unstripped gas
In 1.8 ~ 6.0MPa, temperature control is at 20 ~ 40 DEG C.
3. NHD desulfurization concentrating method according to claim 1, it is characterized in that：Absorption tower Stress control exists
1.8 ~ 6.0MPa, at 20 ~ 40 DEG C, gas liquid ratio controls 150 ~ 300 temperature control.
4. NHD desulfurization concentrating method according to claim 1, it is characterized in that：High pressure flash groove pressure control
System is in 0.8 ~ 1.8MPa.
5. NHD desulfurization concentrating method according to claim 1, it is characterized in that：Concentration tower Stress control exists
0.4 ~ 0.8MPa, at -20 ~ 20 DEG C, gas liquid ratio controls 50 ~ 150 temperature control.
6. NHD desulfurization concentrating method according to claim 1, it is characterized in that, regenerate column overhead temperatures control
System is at 100 ~ 110 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610689196.9A CN107754558B (en) | 2016-08-19 | 2016-08-19 | Desulfurization and concentration method of polyethylene glycol dimethyl ether |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610689196.9A CN107754558B (en) | 2016-08-19 | 2016-08-19 | Desulfurization and concentration method of polyethylene glycol dimethyl ether |
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| Publication Number | Publication Date |
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| CN107754558A true CN107754558A (en) | 2018-03-06 |
| CN107754558B CN107754558B (en) | 2020-10-20 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112609334A (en) * | 2020-11-30 | 2021-04-06 | 浙江青昀新材料科技有限公司 | Flash evaporation non-woven fabric and preparation method thereof |
| CN114797385A (en) * | 2022-05-25 | 2022-07-29 | 光大环境科技（中国）有限公司 | Deacidifying and carbon capturing integrated system and using method thereof |
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| US20150361364A1 (en) * | 2013-02-21 | 2015-12-17 | Mitsubishi Heavy Industries, Ltd. | System and method for recovering gas containing co2 and h2s |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112609334A (en) * | 2020-11-30 | 2021-04-06 | 浙江青昀新材料科技有限公司 | Flash evaporation non-woven fabric and preparation method thereof |
| CN114797385A (en) * | 2022-05-25 | 2022-07-29 | 光大环境科技（中国）有限公司 | Deacidifying and carbon capturing integrated system and using method thereof |
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| CN107754558B (en) | 2020-10-20 |
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Address after: Liuhe District of Nanjing City, Jiangsu province 210048 geguan Road No. 699 Patentee after: China Petroleum & Chemical Corp. Patentee after: SINOPEC NANJING CHEMICAL RESEARCH INSTITUTE Co.,Ltd. Address before: Liuhe District of Nanjing City, Jiangsu province 210048 geguan Road No. 699 Patentee before: China Petroleum & Chemical Corp. Patentee before: Nanhua Group Research Institute |