CN102219653A - Method for producing low-sulfur methyl tert-butyl ether product - Google Patents
Method for producing low-sulfur methyl tert-butyl ether product Download PDFInfo
- Publication number
- CN102219653A CN102219653A CN2011101084903A CN201110108490A CN102219653A CN 102219653 A CN102219653 A CN 102219653A CN 2011101084903 A CN2011101084903 A CN 2011101084903A CN 201110108490 A CN201110108490 A CN 201110108490A CN 102219653 A CN102219653 A CN 102219653A
- Authority
- CN
- China
- Prior art keywords
- mtbe
- depentanizer
- product
- mixed
- sulfur
- 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
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 title claims abstract description 75
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 11
- 229910052717 sulfur Inorganic materials 0.000 title abstract description 19
- 239000011593 sulfur Substances 0.000 title abstract description 19
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 42
- 238000000034 method Methods 0.000 claims abstract description 36
- 238000010992 reflux Methods 0.000 claims abstract description 21
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 15
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000011084 recovery Methods 0.000 claims abstract description 4
- 239000007791 liquid phase Substances 0.000 claims abstract description 3
- 239000005864 Sulphur Substances 0.000 claims description 30
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 19
- 229910052799 carbon Inorganic materials 0.000 claims description 19
- 241000282326 Felis catus Species 0.000 claims description 9
- 238000004821 distillation Methods 0.000 claims description 7
- 238000007600 charging Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 3
- 238000003908 quality control method Methods 0.000 claims description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 abstract description 12
- 230000008569 process Effects 0.000 abstract description 9
- 239000002994 raw material Substances 0.000 abstract description 9
- 238000007670 refining Methods 0.000 abstract description 3
- 238000010533 azeotropic distillation Methods 0.000 abstract 1
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 abstract 1
- 238000003786 synthesis reaction Methods 0.000 abstract 1
- 239000007788 liquid Substances 0.000 description 20
- 239000007789 gas Substances 0.000 description 17
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 12
- 239000004215 Carbon black (E152) Substances 0.000 description 8
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 8
- 229930195733 hydrocarbon Natural products 0.000 description 8
- 150000002430 hydrocarbons Chemical class 0.000 description 8
- 239000003921 oil Substances 0.000 description 5
- 239000000470 constituent Substances 0.000 description 4
- 238000006477 desulfuration reaction Methods 0.000 description 4
- 238000005194 fractionation Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 239000010779 crude oil Substances 0.000 description 3
- 230000003111 delayed effect Effects 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000001590 oxidative effect Effects 0.000 description 3
- JXPACFZBLKPSRP-UHFFFAOYSA-N pentane;hydrate Chemical compound O.CCCCC JXPACFZBLKPSRP-UHFFFAOYSA-N 0.000 description 3
- CETBSQOFQKLHHZ-UHFFFAOYSA-N Diethyl disulfide Chemical compound CCSSCC CETBSQOFQKLHHZ-UHFFFAOYSA-N 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- QMMFVYPAHWMCMS-UHFFFAOYSA-N Dimethyl sulfide Chemical compound CSC QMMFVYPAHWMCMS-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000004303 calcium sorbate Substances 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- WQOXQRCZOLPYPM-UHFFFAOYSA-N dimethyl disulfide Chemical compound CSSC WQOXQRCZOLPYPM-UHFFFAOYSA-N 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 239000000796 flavoring agent Substances 0.000 description 2
- 235000019634 flavors Nutrition 0.000 description 2
- 230000003993 interaction Effects 0.000 description 2
- 239000004302 potassium sorbate Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- SUVIGLJNEAMWEG-UHFFFAOYSA-N propane-1-thiol Chemical compound CCCS SUVIGLJNEAMWEG-UHFFFAOYSA-N 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 239000003381 stabilizer Substances 0.000 description 2
- 239000004283 Sodium sorbate Substances 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- -1 butyl sulfhydryl Chemical group 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 150000002019 disulfides Chemical class 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000006266 etherification reaction Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
Images
Abstract
The invention relates to the field of petrochemical industry, and discloses a method for producing a low-sulfur methyl tert-butyl ether (MTBE) product. The method is characterized in the following steps that: isobutene-containing mixed C4 is delivered to a middle tray of a pentane removing tower; isobutene-containing mixed C4 is rectified and separated at a temperature of 35 to 45 DEG C, and under a pressure of 0.55 to 0.75Mpa; C4 discharged from the tower top is cooled through a cooler, and is delivered to a reflux accumulator; one part of the C4 is pumped by a reflux pump and is used for liquid phase refluxing, and the other part of the C4 is delivered to a mixed-C4 raw material tank and is used for feeding an MTBE reaction system; through processes of MTBE synthesis, azeotropic distillation, and methanol recovery, the low-sulfur MTBE product is obtained. The low-sulfur MTBE product provided by the present invention assists in solving the problem of high total sulfur content in oil refining MTBE. With the method provided by the present invention, the sulfur content of MTBE product can be reduced to 150ppm or lower.
Description
(1) technical field
The present invention relates to petrochemical industry, particularly a kind of method of producing doctor negative methyl tertbutyl ether product.
(2) background technology
Methyl tertiary butyl ether, english abbreviation is MTBE(methyl tert-butyl ether), molten point-109 ℃, 55.2 ℃ of boiling points, be a kind of colourless, transparent, high-octane liquid, having ethereal odor, is the ideal blending component of producing unleaded, high-octane rating, oxygenated gasoline, generally uses in worldwide as gasoline dope.It can not only effectively improve gasoline octane rating, and can also improve automotive performance, reduces CO content in the exhaust, reduces the gasoline production cost simultaneously.In addition, MTBE still is a kind of important chemical material, as preparing high-purity iso-butylene by cracking.
In recent years, along with the crude oil poor qualityization is serious day by day, the sulphur content of catalytically cracked material, delayed coking raw material has continuous rising trend.The oil refinery liquefied gas hydrogen sulfide content that derives from catalytic cracking and delayed coking unit also is difficult to stable being controlled at below 343 mg/Nm3 usually up to more than the 10000ppm through the liquefied gas total sulfur behind amine method depriving hydrogen sulphide, the Merox extracting and oxidizing method mercaptan removal.Coking liquefied gas for high sulfur-bearing (sulphur content is about 3000ppm), even utilize advanced tunica fibrosa doctor process can only guarantee that also the liquefied gas total sulfur of mercaptan removal is about 100ppm, the total sulfur that causes the mixed c 4 that gas separation unit produces generally about 300ppm, the total sulfur of conventional local refinery mixed c 4 even more than 500ppm.Along with the degree of depth comprehensive utilization of liquefied gas resource, refinery will contain the raw material of the mixed c 4 of iso-butylene as production oil refining type MTBE product usually.In the production process of MTBE product, etherification reaction can take place in mercaptan in the mixed c 4 and iso-butylene, MTBE has higher solvability to sulfide than carbon four components simultaneously, behind carbon four component distillations behind MTBE and the ether, sulfide in the mixed c 4 raw material is almost all residual in the MTBE product, and the sulphur content of conventional MTBE product is sometimes up to more than the 1000ppm.In view of MTBE to sulfide easily dissolve, molecular structure is unstable and self reason such as water-soluble, the sulfide in the MTBE product is difficult to desulfurization, causes the MTBE product to be difficult to satisfy the specification of quality of state's three normal benzene blending components.Therefore, the technology of deep removal gas separation unit stock liquid gasification sulphur content is widely paid close attention to, but be difficult to mostly to realize that sulphur content in the mixed c 4 raw material is stable is lower than 40ppm, cause the refinery of some processing high-sulfur crude oils to be difficult to produce the MTBE product that sulphur content is lower than 150ppm.So, invent a kind of method of producing doctor negative methyl tertbutyl ether product, some refineries that process high-sulfur crude oils there is very strong realistic meaning.
(3) summary of the invention
The present invention is in order to remedy the deficiencies in the prior art, the method of the doctor negative methyl tertbutyl ether product of production of the sulphur content reduction in a kind of MTBE of making product is provided, mixed c 4 of the present invention is meant the mixed c 4 that refinery gas's tripping device is produced, the sulfide that contains higher concentration in these mixed c 4s, sulphur content with the MTBE product of these mixed c 4 productions generally is higher than 200ppm, is not suitable for concocting producing country's three motor spirit.
The present invention is achieved through the following technical solutions:
A kind of method of producing doctor negative methyl tertbutyl ether product is characterized in that: comprise the steps:
The mixed c 4 that will contain iso-butylene enters depentanizer middle part tower tray, under 35-45 ℃, 0.55-0.75MPa through rectifying separation, the carbon four that comes out from cat head enters return tank after the water cooler cooling, wherein a part of carbon four is extracted out as liquid-phase reflux by reflux pump, another part is sent to the mixed c 4 head tank to the charging of MTBE reactive system, after synthetic through MTBE then, component distillation, the Methanol Recovery, obtain doctor negative MTBE product.
Described depentanizer is used in particular for removing the higher organosulfur of mixed c 4 mid-boiling point, the quality control index of wherein said depentanizer comprises that carbon five content are 75%-95%(m/m in the control depentanizer tower bottom distillate), the sulphur content of depentanizer overhead fraction is 20ppm-100ppm.
A heavy constituent part of coming out at the bottom of the depentanize Tata heats to tower through bottom reboiler provides gas phase to reflux, and another part is sent pump outside by pentane and extracted the outer tank field of delivering to out after the cooling of pentane water cooler.
The depentanize bottom reboiler by 1.0MPa steam as heating medium.
The present invention is applicable to that with liquid hydrocarbon mixed c 4, industrial methanol be the MTBE product that the raw material production sulphur content is lower than 150ppm.
The present invention is that its main component of sulfide in analysing in depth mixed c 4 is disulphide and causes on the higher basis of MTBE product sulphur content, utilize sulfide or disulphide (as dimethyl disulfide, the first and second basic disulfides, diethyl disulfide, next thiomethyl alcohol, sulfur alcohol, propylmercaptan, butyl sulfhydryl, dimethyl thioether) exist characteristics to propose with the volatility of mixed c 4 hydrocarbon than big-difference, specify the present invention below by the difference of the present invention and traditional method:
A) the traditional method gas that adopts Merox extracting and oxidizing method mercaptan removal or fiber embrane method mercaptan removal to reduce catalytic cracking, delayed coker produces divides the mode of sulphur content in the stock liquid gasification, thereby the sulphur content in the mixed c 4 that the reduction gas separation unit is produced, and then the sulphur content of reduction MTBE product.And the present invention is aspect reduction MTBE product sulphur content, taked to utilize the volatility of sulfide or disulphide and mixed c 4 hydrocarbon to have the method for carrying out fractionation by distillation than the characteristics of big-difference, requirement according to MTBE product sulphur content, fractionation by distillation of the present invention can adopt traditional depentanizer or improved depentanizer, by controlling suitable technic index and quality index, improve the separating power of sulfide or disulphide and mixed c 4 hydrocarbon;
B) mode of the sulphur content of the used reduction MTBE product of traditional method, thereby belong to the method that independent employing catalyzer lye extraction desulfurization alcohol reduces the sulphur content in the mixed c 4, the sulfide in the mixed c 4 or disulphide are influenced the qualified phenomenon of MTBE product sulphur content lack more effective measure.And method of the present invention can make Merox extracting and oxidizing method mercaptan removal or fiber embrane method doctor process gas that process is transferred to divide sulfide or disulphide in the stock liquid gasification, effectively separates with the raw material mixed c 4 of MTBE product with the form of heavy constituent at the bottom of the depentanize Tata;
C) mode of utilizing of the used depentanizer of traditional method is to produce pentane oil and control pentane (carbon five above components) purity more than 95%, and the sulphur content of cat head C-4-fraction is not done requirement, method of the present invention controls then that carbon five content are 75%-95%(m/m in the heavy constituent at the bottom of the depentanizer), can mix with petroleum naphtha and carry out hydrofining and utilize again, and the sulphur content of control depentanizer tops is 20 ppm-100ppm, and carbon five content of depentanizer tops are not done requirement.
The present invention produces the beneficial effect of the method for doctor negative methyl tertbutyl ether product: according to the form and the regularity of distribution of sulfide in the mixed c 4, utilize depentanizer and optimize depentanizer distillation operation condition, solve the high problem of oil refining type MTBE product total sulfur, overcome traditional liquid hydrocarbon deep desulfuration effect and be subjected to behind raw material liquid hydrocarbon sulphur content restriction or the mercaptan removal deficiency of high-content disulphide restriction in the liquid hydrocarbon, the sulphur content of MTBE product is reduced to below the 150ppm, has improved the ability of local refinery producing country three standard low-sulphur oil blending components.
(4) description of drawings
The present invention is further illustrated below in conjunction with accompanying drawing.
Accompanying drawing is technological process of production figure of the present invention.
Among the figure, the C-201 depentanizer, the E-201 water cooler, the E-202 reboiler, E-203 pentane water cooler, the P-201A/B reflux pump, the P-202A/B pentane is sent pump outside, the V-201 return tank.
(5) embodiment
The invention will be further described with embodiment below, and described embodiment just is used to help those skilled in the art to understand the present invention, rather than limits range of application of the present invention.
The present invention produces the method for doctor negative methyl tertbutyl ether product, can be according to the requirement of MTBE product sulphur content, and adopt traditional depentanizer or improved the depentanizer of rectification effect.
The present invention adopts above-mentioned a kind of depentanizer to carry out fractionation by distillation (the sulphur system falls in 30,000 tons of/year MTBE device depentanizes), and embodiment is as follows:
(I) depentanizer system forms
(a) equipment
(b) safety valve
| The place of erection | The medium of releasing | The spring level pressure | Specifications and models | The blowdown temperature |
| The depentanize cat head | C4 | 0.71 | A6R16 | 53.5 |
| Return tank | C4 | 0.68 | CA42Y-16C | 40 |
| The C4 tank deck | C4 | 0.63 | A4P16 | 40 |
(c) control instruments
| Sequence number | Purposes | Setter | Performer | Medium |
| 1 | The depentanizer temperature | Retroaction | Air to open | C4 |
| 2 | The depentanizer inlet amount | Positive interaction | Air to open | The raw material hybrid C 4 |
| 3 | Steam flow | Retroaction | Air to open | Steam |
| 4 | The depentanizer quantity of reflux | Retroaction | Air to close | C4 |
| 5 | Carbon four flows | Retroaction | Air to open | C4 |
| 6 | Liquid level at the bottom of the depentanizer | Positive interaction | Air to open | Carbon five |
| 7 | Liquid level at the bottom of the return tank | Retroaction | Air to open | C4 |
(II) support equipment
Adopt the synthetic and methanol recovery system of traditional MTBE.
(III) technology controlling and process index
| The control project | Controlling index |
| Depentanize inlet amount/th -1 | 10-20 |
| The depentanize feeding temperature/℃ | 40±5 |
| Depentanize cat head temperature/℃ | 53±5 |
| The depentanize column bottom temperature/℃ | 97±5 |
| Depentanize tower top pressure/MPa (gauge pressure) | 0.63±0.1 |
| Return tank pressure/MPa | 0.6±0.1 |
| The depentanizer reflux temperature/℃ | 40±5 |
| Depentanizer reflux ratio (mass ratio) | 1±0.5 |
| Return tank liquid level/% | 20-80 |
| Liquid level/% at the bottom of the depentanize Tata | 20-80 |
| The reboiler temperature/℃ | 97±5 |
(IV) quality control index
| The control project | Controlling index |
| Depentanizer tower bottom distillate carbon five content/% | 75%-95%（m/m） |
| Depentanizer tops sulphur content/ppm | 20-100 |
(V) working method
A. the depentanizer system operation that goes into operation
(1) gets in touch instrument maintenance, chemical examination, start instrument and carry out the chemical examination preparation;
(2) carry out inspection before the pump operation, send preparation work such as electricity;
(3) the mixed c 4 liquid hydrocarbon is sent in contact liquefied gas tank field, to depentanizer C-201 charging, enables the charging variable valve simultaneously, and feed rate is little when just beginning, and progressively increases to normal discharge later on;
(4) open depentanizer top blow-off valve, close after the gas flavor is dense;
(5) at the bottom of the tower and each condensate drain point cut water;
(6) after liquid level reaches 50% at the bottom of the depentanizer, enable depentanize bottom reboiler E-202;
(7) depentanizer heats up with 20 ℃ of-30 ℃/h, progressively is raised to about 97.5 ℃, heats up and enables depentanize cat head aftercooler and thermal bypass simultaneously;
(8) contact chemical examination sampling analysis carbon five purity;
(9) according to liquid level at the bottom of the depentanizer, enable liquid level valve group at the bottom of the depentanizer, pentane goes out device through pentane water cooler E-203;
When (10) depentanize cat head overhead product advances depentanizer return tank V-201, open the emptying of tank deck blow-off valve, close after gas flavor is dense, and the condensate drain valve is cut water at the bottom of opening jar;
(11) enable depentanizer voltage-controlled valve control tower pressure, after depentanizer return tank V-201 liquid level reaches 60%, enable after reflux pump P-201A/B(emptying sees liquefied gas) in tower, return stream;
(12) enable depentanizer reverse flow valve group control quantity of reflux and return tank liquid level;
(13) adjust depentanizer pressure, cat head and column bottom temperature, quantity of reflux and liquid level, make it steadily normal;
(14) at the bottom of the sampling analysis tower, overhead product quality;
(15) when the overhead product sulphur content be 20ppm-100ppm, bottom product carbon five content are 75%-95%(m/m), it is up-to-standard to be considered as overhead product, the beginning to four jars of chargings of MTBE material carbon;
B. depentanizer mass of system control
(1) under normal load, the treatment process that the overhead product sulphur content is high
A. heavy constituent content is pressed as can suitably improve tower in the technic index scope at the bottom of the tower;
B. normal as the tower positive pressure, can suitably reduce the top temperature;
C. suitably reduce feeding temperature or opening for feed is moved down increase rectifying section stage number;
(2) under normal load, contain the many treatment processs of C4 at the bottom of the tower:
A. reduce inlet amount, the load of stabilizer tower;
B. by adjusting the steady tower top pressures of method such as reflux temperature, quantity of reflux in index;
C. reduce quantity of reflux, the control quantity of reflux is in the index request scope;
D. regulate quantity of reflux, reboiler steam amount, temperature is in the technic index span of control at the bottom of the stripper
E. do the stable operation of tower well, suitably reduce inlet amount or increase output, the control liquid level is in indication range;
F. reduce inlet amount, quantity of reflux, the operation of stabilizer tower.
The invention effect:
1, reduce MTBE product sulfur content: when mixing carbon four sulfur contents of gas fractionation unit production were lower than 600ppm, carbon four sulfur contents that the depentanize cat head distillates can drop to below the 25ppm, and corresponding MTBE product total sulfur can drop to below the 50ppm;
2, comprehensive utilization of resources: the restructuring branch that distillates at the bottom of the depentanizer can be stored up naphtha or the similar gasoline component tank of need hydrofinishing desulfurization, further recycles.
Claims (2)
1. a method of producing doctor negative methyl tertbutyl ether product is characterized in that: comprise the steps:
The mixed c 4 that will contain iso-butylene enters depentanizer middle part tower tray, under 35-45 ℃, 0.55-0.75MPa through rectifying separation, the carbon four that comes out from cat head enters return tank after the water cooler cooling, wherein a part of carbon four is extracted out as liquid-phase reflux by reflux pump, another part is sent to the mixed c 4 head tank to the charging of MTBE reactive system, after synthetic through MTBE then, component distillation, the Methanol Recovery, obtain doctor negative MTBE product.
2. the method for the doctor negative methyl tertbutyl ether product of production according to claim 1, it is characterized in that: the quality control index of depentanizer comprises that carbon five content are 75%-95% in the control depentanizer tower bottom distillate, and the sulphur content of depentanizer overhead fraction is 20ppm-100ppm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110108490 CN102219653B (en) | 2011-04-28 | 2011-04-28 | Method for producing low-sulfur methyl tert-butyl ether product |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110108490 CN102219653B (en) | 2011-04-28 | 2011-04-28 | Method for producing low-sulfur methyl tert-butyl ether product |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102219653A true CN102219653A (en) | 2011-10-19 |
| CN102219653B CN102219653B (en) | 2013-06-12 |
Family
ID=44776387
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110108490 Active CN102219653B (en) | 2011-04-28 | 2011-04-28 | Method for producing low-sulfur methyl tert-butyl ether product |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102219653B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104262116A (en) * | 2014-06-23 | 2015-01-07 | 贺立明 | MTBE deep desulfurization device and method thereof |
| CN104341278A (en) * | 2013-08-09 | 2015-02-11 | 中国石油天然气股份有限公司 | Method for recycling disulfide during production of low-sulfur MTBE (methyl tert-butyl ether) product |
| CN105457328A (en) * | 2016-01-16 | 2016-04-06 | 山东东方宏业化工有限公司 | Azeotropic rectifying tower device capable of saving energy, reducing consumption and being used for producing MTBE and adjusting method |
| CN109748781A (en) * | 2018-12-20 | 2019-05-14 | 惠州宇新化工有限责任公司 | Method for treating high-sulfur-carbon four-raw material and co-producing low-sulfur MTBE product |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4391677A (en) * | 1979-03-21 | 1983-07-05 | Davy Mckee (Oil & Chemicals) Limited | Process for producing substantially sulphur-free butene-1 |
| US5569788A (en) * | 1995-03-20 | 1996-10-29 | Uop | Process for removal of impurities from etherification feedstocks |
| CN1193991A (en) * | 1995-08-28 | 1998-09-23 | 化学研究及许可证公司 | Gasoline desulfurization process |
| CN101544532A (en) * | 2009-04-30 | 2009-09-30 | 中国石油兰州石油化工公司 | Method for producing butylene-1 by utilizing catalytic cracking by-product C4 hydrocarbons and ethylene cracking by-product C4 hydrocarbons as raw materials |
-
2011
- 2011-04-28 CN CN 201110108490 patent/CN102219653B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4391677A (en) * | 1979-03-21 | 1983-07-05 | Davy Mckee (Oil & Chemicals) Limited | Process for producing substantially sulphur-free butene-1 |
| US5569788A (en) * | 1995-03-20 | 1996-10-29 | Uop | Process for removal of impurities from etherification feedstocks |
| CN1193991A (en) * | 1995-08-28 | 1998-09-23 | 化学研究及许可证公司 | Gasoline desulfurization process |
| CN101544532A (en) * | 2009-04-30 | 2009-09-30 | 中国石油兰州石油化工公司 | Method for producing butylene-1 by utilizing catalytic cracking by-product C4 hydrocarbons and ethylene cracking by-product C4 hydrocarbons as raw materials |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104341278A (en) * | 2013-08-09 | 2015-02-11 | 中国石油天然气股份有限公司 | Method for recycling disulfide during production of low-sulfur MTBE (methyl tert-butyl ether) product |
| CN104341278B (en) * | 2013-08-09 | 2016-05-11 | 中国石油天然气股份有限公司 | A kind of method of producing low-sulfur MTBE product recovery disulphide |
| CN104262116A (en) * | 2014-06-23 | 2015-01-07 | 贺立明 | MTBE deep desulfurization device and method thereof |
| CN105457328A (en) * | 2016-01-16 | 2016-04-06 | 山东东方宏业化工有限公司 | Azeotropic rectifying tower device capable of saving energy, reducing consumption and being used for producing MTBE and adjusting method |
| CN109748781A (en) * | 2018-12-20 | 2019-05-14 | 惠州宇新化工有限责任公司 | Method for treating high-sulfur-carbon four-raw material and co-producing low-sulfur MTBE product |
| CN109748781B (en) * | 2018-12-20 | 2022-05-13 | 惠州宇新化工有限责任公司 | Method for treating high-sulfur-carbon four-raw material and co-producing low-sulfur MTBE product |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102219653B (en) | 2013-06-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2815621C (en) | Process for the refining of crude oil | |
| CN103146426B (en) | Method of converting fischer-tropsch synthesis products into naphtha, diesel and liquefied petroleum gas | |
| CN103975045A (en) | Process for the production of gasoline by using butanol in the gasoline pool | |
| CA2916163C (en) | Process for the refining of crude oil | |
| CN102219653B (en) | Method for producing low-sulfur methyl tert-butyl ether product | |
| CN104711019A (en) | System and method for producing diesel oil and jet fuel by utilizing Fischer-Tropsch synthetic oil | |
| CN201186917Y (en) | System for preparing high-quality petrol | |
| CN102557888B (en) | Method for deeply desulfurizing methyl tertiary butyl ether | |
| CN102382678B (en) | Method for producing aromatic hydrocarbon from coked gasoline | |
| CN102443432B (en) | Method for producing low-sulfur gasoline by non-hydroforming sulfur and alcohol removal | |
| CN104098448B (en) | A kind of method of methyl tertiary butyl ether(MTBE) lossless rectification desulfurization | |
| CN102443433B (en) | Method for producing low-sulfur gasoline | |
| WO2012174860A1 (en) | Device and method for low-cost production of low-sulphur, high-octane gasoline | |
| CN204723789U (en) | A kind of MTBE deep desulfuration device | |
| CN201144229Y (en) | System for preparing high-quality petrol by recombination of catalytic hydrocarbon | |
| CN201154954Y (en) | System for preparing high quality gasoline by catalytic hydrocarbon recombination | |
| CN101429442B (en) | System and method for catalyzing hydrocarbon for recombinant production of high-quality gasoline | |
| CA2853924A1 (en) | Pretreatment of fcc naphthas and selective hydrotreating | |
| CN101328421B (en) | Method for enhancing diesel/gasoline ratio in oil refining process | |
| CN105950214B (en) | A kind of production method of low-sulphur oil | |
| CN105038843B (en) | A kind of diesel oil vapor-phase hydrodesulfurization process | |
| CN103087770A (en) | Clean gasoline production method through selective hydrogenation and desulfurization of catalytic gasoline | |
| CN201144230Y (en) | System for preparing high-quality petrol by recombination of catalytic hydrocarbon | |
| WO2009067885A1 (en) | A system and process for producing high quality gasoline by catalytic hydrocarbon recombination | |
| CN103756721A (en) | Extraction-washing-hydrogenation combined process for producing low-sulfur gasoline |
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 | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170712 Address after: 274500 No. 27, the Yellow River Road, Dongming County, Heze, Shandong Patentee after: Dongming Hengchang Chemical Co.,Ltd. Address before: 274500, No. 27, petrochemical Avenue, Dongming County, Shandong, Heze Patentee before: SHANDONG DONGMING PETROLEUM & CHEMICAL GROUP CO.,LTD. |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180627 Address after: 274513 Industrial Park, vegetable garden town, Dongming, Heze, Shandong Patentee after: DONGMING QIANHAI CHEMICAL Co.,Ltd. Address before: 274500 the Yellow River Road, Dongming County, Heze, Shandong Province, No. 27 Patentee before: Dongming Hengchang Chemical Co.,Ltd. |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20211214 Address after: 274500 the Yellow River Road, Dongming County, Heze, Shandong Province, No. 27 Patentee after: SHANDONG DONGMING PETROLEUM & CHEMICAL GROUP CO.,LTD. Address before: 274513 Industrial Park, vegetable garden town, Dongming, Heze, Shandong Patentee before: DONGMING QIANHAI CHEMICAL Co.,Ltd. |
|
| TR01 | Transfer of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Method for producing low sulfur methyl tert butyl ether product Effective date of registration: 20211221 Granted publication date: 20130612 Pledgee: Industrial and Commercial Bank of China Limited Dongming sub branch Pledgor: SHANDONG DONGMING PETROLEUM & CHEMICAL GROUP CO.,LTD. Registration number: Y2021980015749 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20220419 Granted publication date: 20130612 Pledgee: Industrial and Commercial Bank of China Limited Dongming sub branch Pledgor: SHANDONG DONGMING PETROLEUM & CHEMICAL GROUP CO.,LTD. Registration number: Y2021980015749 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: A method for producing low sulfur methyl tert butyl ether Effective date of registration: 20221222 Granted publication date: 20130612 Pledgee: Industrial and Commercial Bank of China Limited Dongming sub branch Pledgor: SHANDONG DONGMING PETROLEUM & CHEMICAL GROUP CO.,LTD. Registration number: Y2022980028541 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20231228 Granted publication date: 20130612 Pledgee: Industrial and Commercial Bank of China Limited Dongming sub branch Pledgor: SHANDONG DONGMING PETROLEUM & CHEMICAL GROUP CO.,LTD. Registration number: Y2022980028541 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right |