CN102381945A - Method and device for removing organic sulfur in methyl tertiary butyl ether (MTBE) - Google Patents
Method and device for removing organic sulfur in methyl tertiary butyl ether (MTBE) Download PDFInfo
- Publication number
- CN102381945A CN102381945A CN2011102594316A CN201110259431A CN102381945A CN 102381945 A CN102381945 A CN 102381945A CN 2011102594316 A CN2011102594316 A CN 2011102594316A CN 201110259431 A CN201110259431 A CN 201110259431A CN 102381945 A CN102381945 A CN 102381945A
- Authority
- CN
- China
- Prior art keywords
- mtbe
- interchanger
- extractive distillation
- column
- distillation column
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a method and a device for removing organic sulfur in methyl tertiary butyl ether (MTBE). The method and the device are utilized for high-sulfur content MTBE refinement. The method and the device realize normal-pressure low-temperature extraction rectification desulphurization of a high-sulfur content MTBE product. A technical scheme of the invention comprises the following steps that 1, a sulfur-containing MTBE product is heated by a heat exchanger and then is fed into a rectifying tower from a lower part of the rectifying tower; 2, an extractant is fed into the heat exchanger, is heated and then is fed into the rectifying tower from an upper part of the rectifying tower, wherein a rectifying tower temperature is in a range of 70 to 80 DEG C and the heated sulfur-containing MTBE product and the heated extractant countercurrently contact with each other so that countercurrent contact extraction desulphurization is realized; 3, the desulfurated MTBE product is output from the top of the rectifying tower, is subjected to cooling condensation to form liquid in the heat exchanger and then is output; and 4, the sulfur-containing extractant obtained by the step 2 is output from the bottom of the rectifying tower, is heated by the heat exchanger, is fed into a flash tank, is distilled at a temperature of 80 to 85 DEG C so that the residual desulfurated MTBE product is distilled off, then is fed into an actifier column, and countercurrently contacts with dry air in the actifier column so that countercurrent contact gas stripping regeneration is realized. Through the method and the device, good desulphurization effects are realized; a high product yield is obtained; and an extractant can be regenerated for recycle. The method is convenient for operation, has low costs and low energy consumption, and can be utilized for high-sulfur content MTBE product refinement.
Description
Technical field
The present invention relates to a kind of method and device that is used for the MTBE removal of organic sulfur from of the high sulfur-containing methyl tertbutyl ether of refinery or chemical plant product purification.
Background technology
MTBE; English abbreviation is MTBE (methyl tert-butyl ether); Important blend component as gasoline; Can improve the advantages such as discharging of gasoline octane rating and gasoline combustion efficient, minimizing CO and other objectionable impuritiess (like ozone, benzene, divinyl etc.), applied in China.MTBE also is a kind of important industrial chemicals, as preparing high-purity iso-butylene through cracking, also is used for the production of Methylacrylaldehyde and methylacrylic acid.Iso-butylene is a kind of important chemical material, is widely used in synthetic elastomer, pesticide intermediate and production polyisobutene, TERTIARY BUTYL AMINE, tert.-butylbenzene, butyl rubber etc.Utilize the MTBE cracking to produce high-purity isobutylene, and then produce a series of broad-spectrum high added value derived product.
MTBE (MTBE) is by refining plant C 4 that is rich in iso-butylene and methanol etherification production, and high-purity iso-butylene is produced in the high-octane rating blend component and the cracking that are mainly used in motor spirit.Analysis revealed, the refining plant C 4 raw material sources of synthetic MTBE are in the gas separation unit of catalytic cracking, owing to can not thoroughly remove organosulfur (C wherein
2H
6S
2, COS, RSH, thioether, thiophene), the MTBE sulphur content severe overweight that causes domestic part refinery to be produced.
At present; The report of relevant MTBE desulfurization both at home and abroad is few; In Chinese invention patent " method of a kind of high sulfur-containing methyl tertbutyl ether desulfurization " (publication number CN101643392A),, utilize distillating method that MTBE is carried out desulfurization according to the boiling point difference of MTBE and sulphur.Though this kind method can reach the sweetening effectiveness of expection, service temperature high (90-120 ℃), the production process energy consumption is big; Along with the carrying out that produces, the organosulfur of rectifier bottoms gathers in a large number, causes lower boiling organosulfur to get into the MTBE product; Contain MTBE in the organosulfur of discharging at the bottom of the rectifying tower, cause the yield of desulfurization MTBE product to reduce.
Summary of the invention
The objective of the invention is to: MTBE code name MTBE; In order to overcome the deficiency of existing high sulfur-bearing MTBE product rectifying desulfurization technology; Develop technically a kind of extracting rectifying sulfur method of and atmospheric low-temperature economically, the spy provides a kind of method and device of MTBE removal of organic sulfur from.
In order to achieve the above object; The present invention adopts following technical scheme: a kind of method of MTBE removal of organic sulfur from; It is characterized in that: sulfur-containing methyl tertbutyl ether code name MTBE is heated up through first interchanger 2 from product inlet pipe 16 import in the tower earlier by extractive distillation column 18 bottoms; Keeping working pressure is absolute pressure 0.12-0.15MPa, and tower still temperature is 70-80 ℃, and tower top temperature is 65-75 ℃; Simultaneously the extraction agent in the extraction agent storage tank 15 is heated up, imports in the tower from extractive distillation column 18 tops through the 5th under meter 17 with transferpump 14 inputs the 3rd interchanger 13; Sulfur-bearing MTBE product and extraction agent carry out the counter current contact abstraction desulfurization in extractive distillation column 18; The maintenance reflux ratio is 0.5-3, and the feed volume air speed is 0.5-3 h
-1The output of MTBE product after the desulfurization from extractive distillation column 18 tops, after first flow meter 3 and 2 coolings of first interchanger, the MTBE purified product is condensed into the liquid state below 40 ℃, carries out subsequent operations by 1 output of MTBE products export pipe; The extraction agent that is rich in sulphur output at the bottom of extractive distillation column 18 towers, heating up through second interchanger 12 and the 4th interchanger 19 gets into flash tanks 20; The residence time is 30-60min in flash tank 20; In temperature is to distillate wherein remaining MTBE product under 80-85 ℃, mixes with extractive distillation column 18 top distilled MTBE products after the refined prod pipeline is exported by MTBE products export pipe 1 through second under meter 4 again; The rich sulphur extraction agent of output gets into regenerator column 8 from flash tank 20 bottoms, and regenerator column 8 temperature are 80-85 ℃, and working pressure is that absolute pressure is 0.08-0.10MPa, and dry air is boosted from regenerator column 8 bottoms with 250-350 h through compressor 9 by gas inlet pipe 10
-1Volume space velocity get into, carry out counter current contact gas with the rich sulphur extraction agent that gets into from regenerator column 8 cats head and propose regeneration; The rich sulphur air that gas proposes carries out the condensing and recycling organosulfur or loses the Cross unit recovery sulier it from 7 outputs of regenerator column 8 cat head sulfur-bearing air pipes; The regenerating extracting agent of discharging at the bottom of regenerator column 8 towers gets into extraction agent storage tanks 15 through the 4th under meter 11, second interchanger 12 and 13 coolings of the 3rd interchanger and recycles.
The extraction agent of aforesaid method is a kind of with kerosene, diesel oil, whiteruss, tetramethylene sulfone, N, N-Methyl pyrrolidone, C9 aromatic hydrocarbons or furfural.
A kind of device of MTBE removal of organic sulfur from; Form by interchanger, under meter, return tank, regenerator column, compressor, transferpump, extraction agent storage tank, extractive distillation column and flash tank; It is characterized in that: MTBE product inlet pipe is connected with first interchanger ingress electric welding, and the first heat exchanger exit place connects extractive distillation column lower inlet place with pipeline; Extraction agent storage tank exit connects transferpump, connect the 3rd interchanger and the 5th under meter again with pipeline, and outlet conduit is connected in extractive distillation column upper inlet place; One of extractive distillation column top duct connects the first flow meter and first interchanger, and outlet connects MTBE products export pipe, and another connects second under meter, connects flash drum overhead again; Connect the 3rd under meter and return tank with pipeline in the middle of the extractive distillation column top duct, outlet conduit connects extractive distillation column top; Connect second interchanger and the 4th interchanger of output channel at the bottom of the extracting rectifying Tata, outlet conduit are connected in the flash tank middle part, and flash tank outlet at bottom pipeline connects regenerator column top; The regenerator column lower pipeline connects compressor, connects the gas inlet pipe again; The regenerator column top connects sulfur-bearing air pipe; The regenerator column bottom pipe connects the 4th under meter, connect second interchanger and the 3rd interchanger again, and its outlet conduit is connected in extraction agent storage tank top.
The present invention and prior art relatively have following useful result: (1) MTBE extraction removal of organic sulfur from belongs to physical separating process, and technical process is simple, invests low; (2) do not use strong oxidizer and atmospheric oxidation, production process safety is prone to control, three-waste free discharge; (3) extraction agent can recycle in holomorphosis; (4) process is operated under the atmospheric low-temperature condition, and energy consumption is low; (5) MTBE extracting rectifying removal of organic sulfur from technology; MTBE yield and desulfurization degree are high; Final sulphur content can be reduced to below the 10-50 μ g/g, reaches the harsh requirement that high-purity iso-butylene sulphur content is produced in MTBE mediation motor spirit or cracking, is applied to high sulfur-bearing MTBE product purification.
Description of drawings
Fig. 1 is the structural representation of the device of MTBE removal of organic sulfur from of the present invention.
Among the figure: 1.MTBE products export pipe; 2. first interchanger; 3. first flow meter; 4. second under meter; 5. the 3rd under meter; 6. return tank; 7. sulfur-bearing air pipe; 8. regenerator column; 9. compressor; 10. gas inlet pipe; 11. the 4th under meter; 12. second interchanger; 13. the 3rd interchanger; 14. transferpump; 15. extraction agent storage tank; 16.MTBE product inlet pipe; 17. the 5th under meter; 18. extractive distillation column; 19. the 4th interchanger; 20. flash tank.
Embodiment
Define two notions:
Desulfurization degree: sulphur content * 100% of (sulphur content after sulphur content-desulfurization of raw material MTBE)/raw material MTBE
Mass yield: actual quality product/raw materials quality * 100% that obtains.
Instance 1
The MTBE feed sulphur content is 125 μ g/g, and extraction agent is used whiteruss, feed volume air speed 0.5h
-1, 70 ℃ of column bottom temperatures, 65 ℃ of tower top temperatures, extractive distillation column 18 working pressure 0.12MPa; Extractive distillation column 18 reflux ratios 0.5,80 ℃ of flash tank 20 temperature, 20 residence time of flash tank 30min; 80 ℃ of regenerator column 8 temperature, regenerator column 8 working pressure 0.08MPa, regenerator column 8 volume of air air speed 250h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 2 μ g/g, desulfurization degree is 98.40%, mass yield is 99.97%.
Instance 2
The MTBE feed sulphur content is 149 μ g/g, and extraction agent is used whiteruss, feed volume air speed 0.5h
-1, 80 ℃ of column bottom temperatures, 73 ℃ of tower top temperatures, extractive distillation column 18 working pressure 0.13MPa; Extractive distillation column 18 reflux ratios 1.0,80 ℃ of flash tank 20 temperature, 20 residence time of flash tank 40min; 80 ℃ of regenerator column 8 temperature, regenerator column 8 working pressure 0.08MPa, regenerator column 8 volume of air air speed 280h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 7 μ g/g, desulfurization degree is 95.30%, mass yield is 99.98%.
Instance 3
The MTBE feed sulphur content is 197 μ g/g, and extraction agent is used tetramethylene sulfone, feed volume air speed 0.8h
-1, 80 ℃ of column bottom temperatures, 70 ℃ of tower top temperatures, extractive distillation column 18 working pressure 0.13MPa; Extractive distillation column 18 reflux ratios 1.5,85 ℃ of flash tank 20 temperature, 20 residence time of flash tank 30min; 85 ℃ of regenerator column 8 temperature, regenerator column 8 working pressure 0.09MPa, regenerator column 8 volume of air air speed 250h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 4 μ g/g, desulfurization degree is 97.97%, mass yield is 99.95 %.
Instance 4
The MTBE feed sulphur content is 197 μ g/g, and extraction agent is used N, feed volume air speed 0.8h
-1, 80 ℃ of column bottom temperatures, 70 ℃ of tower top temperatures, extractive distillation column 18 working pressure 0.13MPa; Extractive distillation column 18 reflux ratios 1.2,80 ℃ of flash tank 20 temperature, 20 residence time of flash tank 50min; 85 ℃ of regenerator column 8 temperature, regenerator column 8 working pressure 0.09MPa, regenerator column 8 volume of air air speed 250h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 2 μ g/g, desulfurization degree is 98.98%, mass yield is 99.96%.
Instance 5
The MTBE feed sulphur content is 337 μ g/g, and extraction agent is used N-Methyl pyrrolidone, feed volume air speed 1.0h
-1, 80 ℃ of column bottom temperatures, 75 ℃ of tower top temperatures, extractive distillation column 18 working pressure 0.15MPa; Extractive distillation column 18 reflux ratios 1.0,80 ℃ of flash tank 20 temperature, 20 residence time of flash tank 50min; 85 ℃ of regenerator column 8 temperature, regenerator column 8 working pressure 0.08MPa, regenerator column 8 volume of air air speed 250h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 11 μ g/g, desulfurization degree is 96.74%, mass yield is 99.95%.
Instance 6
The MTBE feed sulphur content is 454 μ g/g, and extraction agent is used kerosene, feed volume air speed 1.5h
-1, 80 ℃ of column bottom temperatures, 75 ℃ of tower top temperatures, extractive distillation column 18 working pressure 0.15MPa; Extractive distillation column 18 reflux ratios 2.0,80 ℃ of flash tank 20 temperature, 20 residence time of flash tank 40min; 85 ℃ of regenerator column 8 temperature, regenerator column 8 working pressure 0.10MPa, regenerator column 8 volume of air air speed 300h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 15 μ g/g, desulfurization degree is 96.70%, mass yield is 99.92%.
Instance 7
The MTBE feed sulphur content is 125 μ g/g, and extraction agent is used furfural, feed volume air speed 2.0h
-1, 70 ℃ of column bottom temperatures, 65 ℃ of tower top temperatures, extractive distillation column 18 working pressure 0.12MPa; Extractive distillation column 18 reflux ratios 2.0,80 ℃ of flash tank 20 temperature, 20 residence time of flash tank 30min; 85 ℃ of regenerator column 8 temperature, regenerator column 8 working pressure 0.09MPa, regenerator column 8 volume of air air speed 260h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 1 μ g/g, desulfurization degree is 99.20%, mass yield is 99.98%.
Instance 8
The MTBE feed sulphur content is 125 μ g/g, and extraction agent is used diesel oil, feed volume air speed 2.0h
-1, 70 ℃ of column bottom temperatures, 65 ℃ of tower top temperatures, extractive distillation column 18 working pressure 0.13MPa; Extractive distillation column 18 reflux ratios 0.5,80 ℃ of flash tank 20 temperature, 20 residence time of flash tank 50min; 82 ℃ of regenerator column 8 temperature, regenerator column 8 working pressure 0.09MPa, regenerator column 8 volume of air air speed 280h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 4 μ g/g, desulfurization degree is 96.80%, mass yield is 99.98%.
Instance 9
The MTBE feed sulphur content is 523 μ g/g, and extraction agent is used C9 aromatic hydrocarbons, feed volume air speed 2.5h
-1, 70 ℃ of column bottom temperatures, 65 ℃ of tower top temperatures; Extractive distillation column 18 working pressure 0.13MPa, extractive distillation column 18 reflux ratios 2.0,80 ℃ of flash tank 20 temperature; 20 residence time of flash tank 40min; 85 ℃ of regenerator column 8 temperature, the working pressure 0.10MPa of regenerator column 8, regenerator column 8 volume of air air speed 300h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 10 μ g/g, desulfurization degree is 98.09%, mass yield is 99.92%.
Instance 10
The MTBE feed sulphur content is 445 μ g/g, and extraction agent is used N-Methyl pyrrolidone, feed volume air speed 3.0h
-1, 80 ℃ of column bottom temperatures, 75 ℃ of tower top temperatures, extractive distillation column 18 working pressure 0.14MPa; Extractive distillation column 18 reflux ratios 3.0,80 ℃ of flash tank 20 temperature, 20 residence time of flash tank 60min; 83 ℃ of regenerator column 8 temperature, regenerator column 8 working pressure 0.10MPa, regenerator column 8 volume of air air speed 350h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 7 μ g/g, desulfurization degree is 98.43%, mass yield is 99.94%.
Instance 11
The MTBE feed sulphur content is 523 μ g/g, and extraction agent is used N, feed volume air speed 2.0h
-1, 80 ℃ of column bottom temperatures, 75 ℃ of tower top temperatures, extractive distillation column 18 working pressure 0.15MPa; Extractive distillation column 18 reflux ratios 3.0,80 ℃ of flash tank 20 temperature, 20 residence time of flash tank 50min; 85 ℃ of regenerator column 8 temperature, regenerator column 8 working pressure 0.10MPa, regenerator column 8 volume of air air speed 350h
-1Condition under, in the accompanying drawing shown device, carry out desulfurization operations, the MTBE sulphur content after refining reaches 9 μ g/g, desulfurization degree is 98.28%, mass yield is 99.90%.
Claims (3)
1. the method for a MTBE removal of organic sulfur from; It is characterized in that: earlier with sulfur-containing methyl tertbutyl ether code name MTBE; Import in the tower by extractive distillation column (18) bottom through first interchanger (2) intensification from MTBE product inlet pipe (16); Keeping working pressure is absolute pressure 0.12-0.15MPa, and tower still temperature is 70-80 ℃, and tower top temperature is 65-75 ℃; Simultaneously the extraction agent in the extraction agent storage tank (15) is heated up, imports in the tower from extractive distillation column (18) top through the 5th under meter (17) with transferpump (14) input the 3rd interchanger (13); Sulfur-bearing MTBE product and extraction agent carry out the counter current contact abstraction desulfurization in extractive distillation column (18); The maintenance reflux ratio is 0.5-3, and the feed volume air speed is 0.5-3 h
-1The output of MTBE product after the desulfurization from extractive distillation column (18) top, after first flow meter (3) and first interchanger (2) cooling, the MTBE purified product is condensed into the liquid state below 40 ℃, is exported by MTBE products export pipe (1); The extraction agent that is rich in sulphur is exported at the bottom of extractive distillation column (18) tower; Get into flash tank (20) through second interchanger (12) and the 4th interchanger (19) intensification; The residence time is 30-60min in flash tank (20); In temperature is to distillate wherein remaining MTBE product under 80-85 ℃, flows into the refined prod pipeline through second under meter (4) again and is exported by MTBE products export pipe (1); Get into regenerator column (8) from the rich sulphur extraction agent of flash tank (20) bottom output; Regenerator column (8) temperature is 80-85 ℃; Working pressure is that absolute pressure is 0.08-0.10MPa, dry air by gas inlet pipe (10) after compressor (9) boosts from regenerator column (8) bottom with 250-350 h
-1Volume space velocity get into, the rich sulphur extraction agent that gets into cat head carries out counter current contact gas and proposes regeneration; The rich sulphur air that gas proposes is from regenerator column (8) cat head sulfur-bearing air pipe (7) output, to its condensing and recycling organosulfur or lose the Cross unit recovery sulier; The regenerating extracting agent of discharging at the bottom of regenerator column (8) tower entering extraction agent storage tank (15) after the 4th under meter (11), second interchanger (12) and the 3rd interchanger (13) are lowered the temperature recycles.
2. according to the method for the said removal of organic sulfur from of claim 1, it is characterized in that: described extraction agent is a kind of with kerosene, diesel oil, whiteruss, tetramethylene sulfone, N, N-Methyl pyrrolidone, C9 aromatic hydrocarbons or furfural.
3. device of using of the method for removal of organic sulfur from according to claim 1; Form by interchanger, under meter, return tank, regenerator column, compressor, transferpump, extraction agent storage tank, extractive distillation column and flash tank; It is characterized in that: MTBE product inlet pipe (16) is connected with first interchanger (2) ingress electric welding, and first interchanger (2) exit connects extractive distillation column (18) lower inlet place with pipeline; Extraction agent storage tank (15) outlet line connects transferpump (14), connect the 3rd interchanger (13) and the 5th under meter (17) again, and outlet conduit is connected in extractive distillation column (18) upper inlet place; Extractive distillation column (18) top duct one small transfer line connects first flow meter (3) and first interchanger (2), and outlet connection MTBE products export pipe (1), another small transfer line connect second under meter (4), connect flash tank (20) top again; Connect the 3rd under meter (5) and return tank (6) with pipeline in the middle of extractive distillation column (18) top duct, its outlet conduit connects extractive distillation column (18) top; Connect second interchanger (12) and the 4th interchanger (19) of output channel at the bottom of extractive distillation column (18) tower, outlet conduit are connected in flash tank (20) middle part, and flash tank (20) outlet at bottom pipeline connects regenerator column (8) top; Regenerator column (8) lower pipeline connects compressor (9), connects gas inlet pipe (10) again; Regenerator column (8) top attachment sulfur-bearing air pipe (7), regenerator column (8) bottom pipe connect the 4th under meter (11), connect second interchanger (12) and the 3rd interchanger (13) again, and its outlet conduit is connected in extraction agent storage tank (15) top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110259431 CN102381945B (en) | 2011-09-05 | 2011-09-05 | Method and device for removing organic sulfur in methyl tertiary butyl ether (MTBE) |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110259431 CN102381945B (en) | 2011-09-05 | 2011-09-05 | Method and device for removing organic sulfur in methyl tertiary butyl ether (MTBE) |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102381945A true CN102381945A (en) | 2012-03-21 |
| CN102381945B CN102381945B (en) | 2013-10-09 |
Family
ID=45821842
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110259431 Expired - Fee Related CN102381945B (en) | 2011-09-05 | 2011-09-05 | Method and device for removing organic sulfur in methyl tertiary butyl ether (MTBE) |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102381945B (en) |
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102898286A (en) * | 2012-08-21 | 2013-01-30 | 九江齐鑫化工有限公司 | Method for removing sulfides in MTBE by adsorptive distillation |
| CN103193603A (en) * | 2013-04-24 | 2013-07-10 | 北京石油化工学院 | Regeneration method of MTBE (methyl tert-butyl ether) adsorbent desulfurization solvent |
| CN103880605A (en) * | 2012-12-21 | 2014-06-25 | 中国石油天然气股份有限公司 | Method for removing sulfides with high boiling points in methyl tert-butyl ether |
| CN103922900A (en) * | 2014-04-03 | 2014-07-16 | 西南石油大学 | Method for removing sulfide in methyl tertiary butyl ether through double-solvent extractive distillation |
| CN105712848A (en) * | 2016-03-23 | 2016-06-29 | 陆明全 | Methyl tertiary butyl ether desulfurizing agent and application method thereof |
| CN105777500A (en) * | 2016-05-25 | 2016-07-20 | 郝天臻 | Extraction anti-gum agent for MTBE desulfurization |
| CN105837408A (en) * | 2015-01-16 | 2016-08-10 | 宁波章甫能源科技有限公司 | Desulfurizer composition for removal of sulfides in MTBE |
| CN106045825A (en) * | 2016-05-29 | 2016-10-26 | 孟红琳 | Method for desulfurizing methyl tertiary butyl ether based on coupled hydrolysis and extraction technology |
| CN106278834A (en) * | 2016-08-12 | 2017-01-04 | 丹东明珠特种树脂有限公司 | A kind of green MTBE deep desulfuration purification agent and the application of sulfide in removing methyl tertiary butyl ether(MTBE) thereof |
| CN106316801A (en) * | 2015-07-09 | 2017-01-11 | 上海纳科助剂有限公司 | Methyl tertiary butyl ether desulfurizing agent and use method thereof |
| CN106554807A (en) * | 2015-09-30 | 2017-04-05 | 中国石油化工股份有限公司 | The high-octane rating etherified benzine production technology of low sulfur, low olefin |
| CN106554813A (en) * | 2015-09-30 | 2017-04-05 | 中国石油化工股份有限公司 | The high-knock rating gasoline production technology of low sulfur, low olefin |
| CN107473938A (en) * | 2017-09-19 | 2017-12-15 | 中建安装工程有限公司 | Utilize the device and method of sulfide in dividing plate extractive distillation column methanol removal |
| CN115400448A (en) * | 2022-08-30 | 2022-11-29 | 华东理工大学 | Application of No. 5 industrial white oil as MTBE (methyl tert-butyl ether) extraction anti-coking agent and MTBE desulfurization method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1740123A (en) * | 2004-08-26 | 2006-03-01 | 西南化工研究设计院 | Alkane desulfurizing process |
| CN101643392A (en) * | 2009-08-31 | 2010-02-10 | 山东玉皇化工有限公司 | Method for desulphurizing methyl tertiary butyl ether with high sulphur content |
| CN102166428A (en) * | 2011-03-02 | 2011-08-31 | 天津凯赛特科技有限公司 | Extractive distillation system for sulfur-containing toluene and refining method thereof |
-
2011
- 2011-09-05 CN CN 201110259431 patent/CN102381945B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1740123A (en) * | 2004-08-26 | 2006-03-01 | 西南化工研究设计院 | Alkane desulfurizing process |
| CN101643392A (en) * | 2009-08-31 | 2010-02-10 | 山东玉皇化工有限公司 | Method for desulphurizing methyl tertiary butyl ether with high sulphur content |
| CN102166428A (en) * | 2011-03-02 | 2011-08-31 | 天津凯赛特科技有限公司 | Extractive distillation system for sulfur-containing toluene and refining method thereof |
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102898286A (en) * | 2012-08-21 | 2013-01-30 | 九江齐鑫化工有限公司 | Method for removing sulfides in MTBE by adsorptive distillation |
| CN103880605A (en) * | 2012-12-21 | 2014-06-25 | 中国石油天然气股份有限公司 | Method for removing sulfides with high boiling points in methyl tert-butyl ether |
| CN103880605B (en) * | 2012-12-21 | 2016-08-10 | 中国石油天然气股份有限公司 | A kind of remove the method for higher boiling sulfur compound in methyl tertiary butyl ether(MTBE) |
| CN103193603B (en) * | 2013-04-24 | 2017-07-04 | 北京石油化工学院 | MTBE adsorbs the renovation process of desulfurization solvent |
| CN103193603A (en) * | 2013-04-24 | 2013-07-10 | 北京石油化工学院 | Regeneration method of MTBE (methyl tert-butyl ether) adsorbent desulfurization solvent |
| CN103922900A (en) * | 2014-04-03 | 2014-07-16 | 西南石油大学 | Method for removing sulfide in methyl tertiary butyl ether through double-solvent extractive distillation |
| CN105837408A (en) * | 2015-01-16 | 2016-08-10 | 宁波章甫能源科技有限公司 | Desulfurizer composition for removal of sulfides in MTBE |
| CN106316801A (en) * | 2015-07-09 | 2017-01-11 | 上海纳科助剂有限公司 | Methyl tertiary butyl ether desulfurizing agent and use method thereof |
| CN106554813B (en) * | 2015-09-30 | 2018-09-21 | 中国石油化工股份有限公司 | The high-knock rating gasoline production technology of low sulfur, low olefin |
| CN106554807B (en) * | 2015-09-30 | 2018-09-21 | 中国石油化工股份有限公司 | The high-octane rating etherified benzine production technology of low sulfur, low olefin |
| CN106554807A (en) * | 2015-09-30 | 2017-04-05 | 中国石油化工股份有限公司 | The high-octane rating etherified benzine production technology of low sulfur, low olefin |
| CN106554813A (en) * | 2015-09-30 | 2017-04-05 | 中国石油化工股份有限公司 | The high-knock rating gasoline production technology of low sulfur, low olefin |
| CN105712848A (en) * | 2016-03-23 | 2016-06-29 | 陆明全 | Methyl tertiary butyl ether desulfurizing agent and application method thereof |
| CN105777500A (en) * | 2016-05-25 | 2016-07-20 | 郝天臻 | Extraction anti-gum agent for MTBE desulfurization |
| CN105777500B (en) * | 2016-05-25 | 2018-03-06 | 郝天臻 | A kind of extraction antigum inhibitor for MTBE desulfurization |
| CN106045825A (en) * | 2016-05-29 | 2016-10-26 | 孟红琳 | Method for desulfurizing methyl tertiary butyl ether based on coupled hydrolysis and extraction technology |
| CN106278834B (en) * | 2016-08-12 | 2018-09-18 | 丹东明珠特种树脂有限公司 | A kind of green MTBE deep desulfuration purifications agent and its in removing methyl tertiary butyl ether(MTBE) sulfide application |
| CN106278834A (en) * | 2016-08-12 | 2017-01-04 | 丹东明珠特种树脂有限公司 | A kind of green MTBE deep desulfuration purification agent and the application of sulfide in removing methyl tertiary butyl ether(MTBE) thereof |
| CN107473938A (en) * | 2017-09-19 | 2017-12-15 | 中建安装工程有限公司 | Utilize the device and method of sulfide in dividing plate extractive distillation column methanol removal |
| CN107473938B (en) * | 2017-09-19 | 2023-10-10 | 中建安装集团有限公司 | Device and method for removing sulfides in methanol by using partition plate extraction rectifying tower |
| CN115400448A (en) * | 2022-08-30 | 2022-11-29 | 华东理工大学 | Application of No. 5 industrial white oil as MTBE (methyl tert-butyl ether) extraction anti-coking agent and MTBE desulfurization method |
| CN115400448B (en) * | 2022-08-30 | 2024-06-21 | 华东理工大学 | Application of No. 5 industrial white oil as MTBE (methyl tert-butyl ether) extraction scorch retarder and MTBE desulfurization method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102381945B (en) | 2013-10-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102381945B (en) | Method and device for removing organic sulfur in methyl tertiary butyl ether (MTBE) | |
| CN203923054U (en) | A kind of device of being produced benzene, toluene and dimethylbenzene by crude benzol | |
| CN102958877A (en) | Process for removing one or more sulfur compounds from stream | |
| CN103468307A (en) | Method and device for desulfurizing catalytically cracked gasoline | |
| CN103922900A (en) | Method for removing sulfide in methyl tertiary butyl ether through double-solvent extractive distillation | |
| US4406868A (en) | Process and apparatus for removing H2 S from gas streams | |
| CN101250079A (en) | Heat-exchange network device for refining crude benzene and method of operation | |
| CN108129254A (en) | A kind of device and method of the carbon dioxide removal from ethane gas | |
| CN107365241A (en) | A kind of crude benzole hydrogenation process for refining | |
| CN102174333A (en) | Combination process method for denitrification and prerefining of coking diesel oil | |
| CN107473938B (en) | Device and method for removing sulfides in methanol by using partition plate extraction rectifying tower | |
| CN103184071A (en) | Gasoline desulfurization method | |
| CN114989856A (en) | Method and device for separating aromatic hydrocarbon or sulfur-containing compound from gasoline fraction | |
| CN105949026A (en) | Mixed pentane precise separation device | |
| CN204369817U (en) | A kind of gasoline hydrogenation system | |
| CN203238197U (en) | Production device of MTBE (methyl tert-butyl ether) with low sulfur content | |
| CN216320054U (en) | Coking crude benzol fractionation device for desulfurization treatment | |
| CN101941877B (en) | For removing the method and apparatus of pollutent from selective aromatics solvent | |
| CN102079993A (en) | Catalytic gasoline alkylation desulfuration method and device | |
| CN204385135U (en) | Full cut catalytic gasoline selective hydrodesulfurization device | |
| CN203095914U (en) | Device for removing high-boiling-point sulphide in methyl tertiary butyl ethers | |
| CN1030070A (en) | Single tower debenzolizing process and novel debenzolizing tower | |
| CN203916122U (en) | A kind of dimethylbenzene separator | |
| CN101870882B (en) | Shale oil condensation recycling water-washing process system and operation method | |
| CN110013751B (en) | Device and method for removing non-mercaptan sulfur and mercaptan in liquefied gas by wet method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20131009 Termination date: 20140905 |
|
| EXPY | Termination of patent right or utility model |