CN102079993A - Catalytic gasoline alkylation desulfuration method and device - Google Patents
Catalytic gasoline alkylation desulfuration method and device Download PDFInfo
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- CN102079993A CN102079993A CN2010106164149A CN201010616414A CN102079993A CN 102079993 A CN102079993 A CN 102079993A CN 2010106164149 A CN2010106164149 A CN 2010106164149A CN 201010616414 A CN201010616414 A CN 201010616414A CN 102079993 A CN102079993 A CN 102079993A
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Abstract
The invention relates to a catalytic gasoline alkylation desulfuration method and device. The method comprises the following steps: carrying out heat transfer on catalytic gasoline under the pressure of 0.2-1.0 MPa; heating to 50-110 DEG C, and then introducing the catalytic gasoline into an alkylation reaction tower at a liquid hour volume space velocity of 0.5-6.0 hour<-1>; carrying out alkylation reaction in the presence of an alkylation desulfuration catalyst, and introducing the alkylation gasoline after reaction into a fractionating column; fractionating the alkylation gasoline into a low-sulphur light fraction (alkylation desulfuration gasoline) and a sulphur-rich heavy fraction at the temperature of 175-185 DEG C; and recovering the alkylation desulfuration gasoline from the top of the fractionating column, and recovering the heavy fraction from the kettle of the fractionating column. By using the method provided by the invention, the octane value of the gasoline is maintained to be basically unchanged while the sulfide in the gasoline is removed; the method has the advantages of simple flow process, less equipment construction investment, low operation expense, mild operation condition and good desulfuration effect; and the process is easy to control, and the content of the sulphur in the alkylation desulfuration gasoline meets the national standard of motor gasoline.
Description
Technical field
The invention belongs to the alkylation desulfurization of gasoline technical field, be specifically related to the device that a kind of catalytically cracked gasoline desulfurization is produced the method for low-sulfur, stop bracket gasoline and realized this method.
Background technology
Sulfide in the gasoline mainly contains mercaptan, thioether, disulphide, thiophene and derivative thereof, and wherein thiophene and derivative thereof account for more than 80% of total sulfur content.Sulfide in the gasoline is etching apparatus not only, also can make poisoning of catalyst, influences catalyzer work-ing life and the SO in its products of combustion
2Being the main source that causes topsoil, also is the immediate cause that forms acid rain
[2]Therefore, must the strict sulfide content that limits in the motor spirit.At present, developed countries such as America and Europe have all carried out strict qualification to the sulphur content in the gasoline, China has issued that also relevant regulations with the restriction content of sulfur in gasoline, requires from 2010, and the nationwide vehicle gasoline and sulfur content in vehicle gasoline must be reduced to below the 150 μ g/g (state's III standard).
The hydrogenating desulfurization technology is at the industrial feasible and desulfurization technology of being used widely, it is the important means of producing clean fuel oil both at home and abroad, but the operating environment of noble metal catalyst, high-purity hydrogen and High Temperature High Pressure that this Technology Need is special, investment that is brought and process cost are higher thus, and general small-sized refinery is difficult to bear.In addition, some organic sulfides in the petroleum products (as thionaphthene and derivative thereof) are difficult to be removed by hydrogenating desulfurization, and deep hydrogenation can cause a large amount of alkene saturated, also can reduce the oil product octane value when consuming hydrogen.Therefore, many non-hydrodesulfurizationprocess process have appearred in recent years, as: oxidation sweetening, abstraction desulfurization, alkylating desulfurization, adsorption desulfurize etc.But abstraction desulfurization method and oxidation sweetening method have pair sulfide selectivity relatively poor, and yield of gasoline is low; The adsorption desulfurize method exists the sorbent material sulfur capacity low, problems such as regeneration energy consumption height; By contrast, the alkylating desulfurization technology is a kind of non-preferably hydrogenating desulfurization technology.This method utilizes an acidic catalyst to make thiophene sulphur compound and alkene in the catalytically cracked gasoline carry out alkylated reaction, generates the higher alkylthrophene sulfide of boiling point, and the latter can remove by fractionation by distillation, thereby reaches the purpose of desulfurization.Alkylating desulfurization technological operation condition relaxes, sweetening effectiveness is good, the alkene loss less, keep gasoline octane rating, do not consume hydrogen and hydrogenation catalyst, process cost is low, is a kind of very competitive desulfurization technology.
US5599441 discloses a kind of alkylating desulfurization method, this method is a catalyzer with the solid acid with Lewis acid site and the solid acid at protonic acid center, make thiophene-type sulfide and alkene in the catalytically cracked gasoline carry out alkylated reaction, the high boiling point alkylthrophene compounds that generates focuses in the heavy constituent by distillation, removes by the hydrogenating desulfurization technology again.But when this method was raw material with full cut, the thiophene transformation efficiency was lower, had the problem of olefinic polymerization simultaneously.
US5863419 discloses the method that a kind of catalytic distillation is used for alkylation desulfurization of gasoline, and alkylated reaction and fractionation are carried out in separation column simultaneously in this method.Can utilize alkene in the gasoline as alkylating agent, also can additionally add alkylating agent,, the part sulfocompound in the gasoline be transferred in the last running as pure and mild alkene.Catalyzer can be the acid material of any energy catalyzed alkene or alcohol and thiophene-type sulfide alkylated reaction, mainly adopts solid acid catalyst.This method temperature of reaction is about 200 ℃, and reaction pressure is more than the 17atm, and operational condition is harsh, and embodiment shows that alkylated reaction has also taken place the part aromatic hydrocarbons in the gasoline.
CN1552705A discloses a kind of ionic-liquid catalyst of thiophene olefin alkylation reaction, and this ionic liquid is made by the hydrochloride of organic nitrogen compound and an alkali metal salt reaction of Lewis acid and boron or phosphorus, can be used for containing the fractional oil desulfurizing of alkene.But still there is environmental issue in acidic ion liquid regeneration difficulty after discarding.
CN101597510A discloses a kind of catalytic distillation method of alkylation desulfurization of gasoline, this method adds high boiling diesel oil distillate in separation column, the boiling point that alkylated reaction is generated is higher than the sulfide of gasoline fraction and transfers in the diesel oil, save the gasoline hydrogenation process, this part diesel oil can mix with other diesel oil, handles together in the diesel fuel desulfurization process.But the reactor used two ends temperature height up and down of this method, medium temperature is low, and thermograde is bigger, and operation is difficult for realizing.
Summary of the invention
The objective of the invention is to deficiency at the existence of abovementioned alkyl sulfur method, the alkylating desulfurization method that develop that a kind of simple to operate, operational condition relaxes, operation is easy to control, sweetening effectiveness is good, keep gasoline octane rating, process cost is low, and the device of this method of realization is provided.
To achieve these goals, the present invention by the following technical solutions: a kind of catalytically cracked gasoline alkylating desulfurization method, this method steps is as follows:
A, earlier in the alkylated reaction tower, load alkylating and desulfurizing catalyst, then with catalytically cracked gasoline under pressure 0.2 ~ 1.0MPa after the interchanger heat exchange is warming up to 50 ~ 110 ℃ volume space velocity 0.5 ~ 6.0h during with liquid
-1Introduce in the alkylated reaction tower, under the effect of alkylating and desulfurizing catalyst, carry out alkylated reaction and generate gasoline alkylate;
B, with gasoline alkylate from the extraction of alkylated reaction column overhead, after being warmed up to 180-185 ℃, the interchanger heat exchange introduces separation column, the last running that fractionation is cut into doctor negative lighting end and is rich in sulphur, described doctor negative lighting end is an alkylating desulfurization gasoline, from fractionator overhead extraction alkylating desulfurization gasoline, the heat exchange cooling is cooled to below 40 ℃ outer defeated; The last running of fractionation Tata still extraction is defeated outward.
Used alkylating and desulfurizing catalyst is a kind of in macropore sulfuric acid resin, molecular sieve, carried heteropoly acid or the ionic liquid.
Gasoline alkylate enters separation column, 175 ~ 185 ℃ of last running of locating to be cut into alkylating desulfurization gasoline and being rich in sulphur.
A kind of used alkylating desulfurization device of catalytically cracked gasoline alkylating desulfurization method of implementing, this device comprises stock oil input tube, first interchanger, alkylated reaction tower, second interchanger, separation column, heavy constituent output tube and alkylating desulfurization gasoline output tube, and described stock oil input tube is connected with tube inlet in first interchanger; Pipe exports by pipe connection at the alkylated reaction tower bottom in first interchanger, the alkylated reaction column overhead is connected by the outer tube inlet of the pipeline and second interchanger, the second interchanger outer tube exports by pipe connection at the separation column middle part, the cat head of separation column is connected by the outer tube inlet of the pipeline and first interchanger, the outlet of the first interchanger outer tube is connected with alkylating desulfurization gasoline output tube, is connected with the heavy constituent output tube at the bottom of the tower of separation column.
The present invention has following beneficial effect:
(1) flow process is simple, and operation is easy to control and alkylated reaction tower and distillation tower are combined into a tower, and the plant area area is little, and investment cost is low;
(2) operational condition relaxes, and alkylated reaction can carry out under 50 ~ 110 ℃ of temperature, pressure 0.2 ~ 1.0MPa, and energy consumption is low;
(3) catalytically cracked gasoline is after alkylating desulfurization is handled, the basic free of losses of RON;
(4) sweetening effectiveness is good, and the alkylating desulfurization rate reaches 41.46% ~ 81.10%%, the quality of gasoline yield〉84.64%.
(5) turndown ratio is big, is applicable to the catalytic gasoline of whole fraction desulfurization of sulphur content at 100 ~ 600 μ g/g, keeps gasoline octane rating, and the alkylating desulfurization content of sulfur in gasoline meets " motor spirit " national standard.
Description of drawings
Fig. 1 is the structural representation of alkylating desulfurization device of the present invention.
Among the figure: 1, stock oil input tube, 2, first interchanger, 3, the alkylated reaction tower, 4, second interchanger, 5, separation column, 6, the last running output tube, 7, alkylating desulfurization gasoline output tube.
Concrete embodiment
In order to understand the present invention better, in conjunction with the embodiments the method for the invention is described further.
A kind of catalytically cracked gasoline alkylating desulfurization method, this method steps is as follows:
A, earlier in the alkylated reaction tower, load alkylating and desulfurizing catalyst, then with catalytically cracked gasoline under pressure 0.2 ~ 1.0MPa after the interchanger heat exchange is warming up to 50 ~ 110 ℃ volume space velocity 0.5 ~ 6.0h during with liquid
-1Introduce in the alkylated reaction tower, under the effect of alkylating and desulfurizing catalyst, carry out alkylated reaction and generate gasoline alkylate;
B, with gasoline alkylate from the extraction of alkylated reaction column overhead, after being warmed up to 180-185 ℃, the interchanger heat exchange introduces separation column, heat up in a steamer the last running that is cut into doctor negative lighting end and is rich in sulphur 175 ~ 185 ℃ of punishment, doctor negative lighting end is an alkylating desulfurization gasoline, from fractionator overhead extraction alkylating desulfurization gasoline, the heat exchange cooling is cooled to below 40 ℃ outer defeated; The last running of fractionation Tata still extraction is defeated outward.
Used alkylating and desulfurizing catalyst is a kind of in macropore sulfuric acid resin, molecular sieve, carried heteropoly acid or the ionic liquid.
A kind of used alkylating desulfurization device of catalytically cracked gasoline alkylating desulfurization method of implementing, this device comprises stock oil input tube 1, first interchanger 2, alkylated reaction tower 3, second interchanger 4, separation column 5, heavy constituent output tube 6 and alkylating desulfurization gasoline output tube 7, and described stock oil input tube 1 is connected with tube inlet in first interchanger 2; Pipe exports by pipe connection in alkylated reaction tower 3 bottoms in first interchanger 2, alkylated reaction tower 3 cats head are connected with second interchanger, 4 outer tube inlets by pipeline, second interchanger, 4 outer tubes export by pipe connection at separation column 5 middle parts, the cat head of separation column 5 is connected with first interchanger, 2 outer tube inlets by pipeline, the outlet of first interchanger, 2 outer tubes is connected with alkylating desulfurization gasoline output tube 7, is connected with heavy constituent output tube 6 at the bottom of the tower of separation column 5.
Filling H beta-molecular sieve alkylating and desulfurizing catalyst in the alkylated reaction tower, under reaction pressure 0.5MPa, the volume space velocity 0.5h during with liquid with the catalytically cracked gasoline of sulphur content 164 μ g/g
-1Through the input of stock oil input tube, send into the interchanger of alkylated reaction device, the catalytically cracked gasoline temperature is increased to 50 ℃ after heat exchange, carries out alkylated reaction in reaction tower, and reaction generates gasoline alkylate; With gasoline alkylate from the extraction of alkylated reaction column overhead, enter interchanger, after heating up, heat exchange locates to be cut into doctor negative lighting end at 175 ~ 185 ℃---alkylating desulfurization gasoline and the last running of being rich in sulphur, from fractionator overhead extraction alkylating desulfurization gasoline, outer defeated below the heat exchange to 40 ℃, the last running of fractionation Tata still extraction.Recording the alkylating desulfurization content of sulfur in gasoline is 92 μ g/g, desulfurization degree 43.90%, mass yield 89.71%.
With the D002 resin is alkylating and desulfurizing catalyst, and sulphur content is that the catalytically cracked gasoline of 505 μ g/g is a stock oil, presses embodiment 2 described methods 80 ℃ of temperature of reaction, reaction pressure 0.8MPa, volume space velocity 2.5h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 142 μ g/g, mass yield 91.51%, desulfurization degree 71.88%.
Embodiment 3
With ionic liquid Et
2O-AlCl
3Be alkylating and desulfurizing catalyst, sulphur content is that the catalytically cracked gasoline of 505 μ g/g is a stock oil, presses embodiment 2 described methods 50 ℃ of temperature of reaction, reaction pressure 0.2MPa, volume space velocity 4.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 127 μ g/g, mass yield 85.70%, desulfurization degree 74.85%.
With the HMCM-22 molecular sieve is alkylating and desulfurizing catalyst, and sulphur content is that the catalytically cracked gasoline of 505 μ g/g is a stock oil, presses embodiment 2 described methods 110 ℃ of temperature of reaction, reaction pressure 1.0MPa, volume space velocity 1.5h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 148 μ g/g, mass yield 84.64%, desulfurization degree 70.68%.
Embodiment 5
Filling ionic-liquid catalyst Et in reactor
3NHCl-AlCl
3, sulphur content is that the catalytically cracked gasoline of 505 μ g/g is a stock oil, presses embodiment 2 described methods 60 ℃ of temperature of reaction, reaction pressure 0.7MPa, volume space velocity 3.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 107 μ g/g, and desulfurization degree is 78.81%, mass yield 87.90%.
With the NKC-9 resin is alkylating and desulfurizing catalyst, and sulphur content is that the catalytically cracked gasoline of 505 μ g/g is a stock oil, presses embodiment 2 described methods 90 ℃ of temperature of reaction, reaction pressure 0.5MPa, volume space velocity 3.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 145 μ g/g, mass yield 86.51%, and desulfurization degree 71.29%,
With ionic liquid Et
3NHCl-AlCl
3Be alkylating and desulfurizing catalyst, sulphur content is that the catalytically cracked gasoline of 164 μ g/g is a stock oil, presses embodiment 2 described methods 70 ℃ of temperature of reaction, reaction pressure 0.2MPa, volume space velocity 4.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 31 μ g/g, mass yield 85.21%, and desulfurization degree 81.10%,
Embodiment 8
With carried heteropoly acid PW-SiO
2Be alkylating and desulfurizing catalyst, sulphur content is that the catalytically cracked gasoline of 164 μ g/g is a stock oil, presses embodiment 2 described methods 80 ℃ of temperature of reaction, reaction pressure 0.3MPa, volume space velocity 1.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 96 μ g/g, mass yield 88.60%, desulfurization degree 41.46%.
Embodiment 9
With the HMCM-22 molecular sieve is alkylating and desulfurizing catalyst, and sulphur content is that the catalytically cracked gasoline of 315 μ g/g is a stock oil, presses embodiment 2 described methods 60 ℃ of temperature of reaction, reaction pressure 0.8MPa, volume space velocity 2.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 139 μ g/g, mass yield 87.1%, desulfurization degree 55.87%.
Embodiment 10
With the CT-175 resin is alkylating and desulfurizing catalyst, and sulphur content is that the catalytically cracked gasoline of 505 μ g/g is a stock oil, presses embodiment 2 described methods 80 ℃ of temperature of reaction, reaction pressure 0.4MPa, volume space velocity 3.5h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 126 μ g/g, mass yield 86.30%, desulfurization degree 75.05%.
Embodiment 11
With carried heteropoly acid PW-NKC9 is alkylating and desulfurizing catalyst, and sulphur content is that the catalytically cracked gasoline of 164 μ g/g is a stock oil, presses embodiment 2 described methods 100 ℃ of temperature of reaction, reaction pressure 0.3MPa, volume space velocity 1.5h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 81 μ g/g, mass yield 88.00%, desulfurization degree 50.61%.
Embodiment 12
With the NKC-9 resin is alkylating and desulfurizing catalyst, and sulphur content is that the catalytically cracked gasoline of 315 μ g/g is a stock oil, presses embodiment 2 described methods 80 ℃ of temperature of reaction, reaction pressure 0.4MPa, volume space velocity 2.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 92 μ g/g, mass yield 84.72%, desulfurization degree 70.79%.
Embodiment 13
With ionic liquid Et
2O-AlCl
3Be alkylating and desulfurizing catalyst, sulphur content is that the catalytically cracked gasoline of 315 μ g/g is a stock oil, presses embodiment 2 described methods 50 ℃ of temperature of reaction, reaction pressure 0.2MPa, volume space velocity 5.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 94 μ g/g, mass yield 86.31%, desulfurization degree 70.16%.
Embodiment 14
With carried heteropoly acid AC-SiW is alkylating and desulfurizing catalyst, and sulphur content is that the catalytically cracked gasoline of 164 μ g/g is a stock oil, presses embodiment 2 described methods 100 ℃ of temperature of reaction, reaction pressure 0.6MPa, volume space velocity 4.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 75 μ g/g, mass yield 88.34%, desulfurization degree 54.27%.
With the solid phosphoric acid is alkylating and desulfurizing catalyst, and sulphur content is that the catalytically cracked gasoline of 315 μ g/g is a stock oil, presses embodiment 2 described methods 105 ℃ of temperature of reaction, reaction pressure 0.7MPa, volume space velocity 6.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 82 μ g/g, mass yield 85.43%, desulfurization degree 73.97%.
Embodiment 16
With ionic liquid [BMIM] Cl-FeCl
3Be alkylating and desulfurizing catalyst, sulphur content is that the catalytically cracked gasoline of 315 μ g/g is a stock oil, presses embodiment 2 described methods 50 ℃ of temperature of reaction, reaction pressure 0.9MPa, volume space velocity 1.0h during liquid
-1Condition under alkylated reaction, other step is identical with step among the embodiment 2.Recording the alkylating desulfurization content of sulfur in gasoline is 43 μ g/g, mass yield 89.40%, desulfurization degree 73.78%.
Claims (4)
1. catalytically cracked gasoline alkylating desulfurization method is characterized in that this method steps is as follows:
A, earlier in the alkylated reaction tower, load alkylating and desulfurizing catalyst, then with catalytically cracked gasoline under pressure 0.2 ~ 1.0MPa after the interchanger heat exchange is warming up to 50 ~ 110 ℃ volume space velocity 0.5 ~ 6.0h during with liquid
-1Introduce in the alkylated reaction tower, under the effect of alkylating and desulfurizing catalyst, carry out alkylated reaction and generate gasoline alkylate;
B, with gasoline alkylate from the extraction of alkylated reaction column overhead, after being warmed up to 180-185 ℃, the interchanger heat exchange introduces separation column, the last running that fractionation is cut into doctor negative lighting end and is rich in sulphur, described doctor negative lighting end is an alkylating desulfurization gasoline, from fractionator overhead extraction alkylating desulfurization gasoline, the heat exchange cooling is cooled to below 40 ℃ outer defeated; The last running of fractionation Tata still extraction is defeated outward.
2. a kind of catalytically cracked gasoline alkylating desulfurization method according to claim 1 is characterized in that: used alkylating and desulfurizing catalyst is a kind of in macropore sulfuric acid resin, molecular sieve, carried heteropoly acid or the ionic liquid.
3. according to the described a kind of catalytically cracked gasoline alkylating desulfurization method of claim 1, it is characterized in that: gasoline alkylate enters separation column, 175 ~ 185 ℃ of last running of locating to be cut into alkylating desulfurization gasoline and being rich in sulphur.
4. implement the used alkylating desulfurization device of the described a kind of catalytically cracked gasoline alkylating desulfurization method of claim 1 for one kind, this device comprises stock oil input tube (1), first interchanger (2), alkylated reaction tower (3), second interchanger (4), separation column (5), heavy constituent output tube (6) and alkylating desulfurization gasoline output tube (7), it is characterized in that: described stock oil input tube (1) is connected with the interior tube inlet of first interchanger (2); Pipe exports by pipe connection in alkylated reaction tower (3) bottom in first interchanger (2), alkylated reaction tower (3) cat head is connected with the outer tube inlet of second interchanger (4) by pipeline, second interchanger (4) outer tube exports by pipe connection at separation column (5) middle part, the cat head of separation column (5) is connected with the outer tube inlet of first interchanger (2) by pipeline, the outlet of first interchanger (2) outer tube is connected with alkylating desulfurization gasoline output tube (7), is connected with heavy constituent output tube (6) at the bottom of the tower of separation column (5).
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102876361A (en) * | 2012-09-28 | 2013-01-16 | 西南石油大学 | Naphtha dearomatization and automotive fuel oil desulfurization coupling technology |
| CN105861030A (en) * | 2014-12-24 | 2016-08-17 | 神华集团有限责任公司 | Gasoline alkylating and desulfurizing method based on modified heteropolyacid catalyst and product thereof |
| CN108192665A (en) * | 2018-02-05 | 2018-06-22 | 山东星火科学技术研究院 | A kind of gasoline desulfating method |
| CN116396139A (en) * | 2023-06-08 | 2023-07-07 | 新疆天利石化股份有限公司 | Method for catalytic removal of thiophene aromatic heterocyclic sulfur compounds in styrene in fixed bed reactor |
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| CN1453335A (en) * | 2002-04-26 | 2003-11-05 | 中国石油化工股份有限公司 | Petroleum fraction alkyl sulfur transferring method |
| CN101007965A (en) * | 2006-01-27 | 2007-08-01 | 中国石油化工股份有限公司 | Gasoline alkylation desulfuration method |
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- 2010-12-31 CN CN2010106164149A patent/CN102079993A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1453335A (en) * | 2002-04-26 | 2003-11-05 | 中国石油化工股份有限公司 | Petroleum fraction alkyl sulfur transferring method |
| CN101007965A (en) * | 2006-01-27 | 2007-08-01 | 中国石油化工股份有限公司 | Gasoline alkylation desulfuration method |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102876361A (en) * | 2012-09-28 | 2013-01-16 | 西南石油大学 | Naphtha dearomatization and automotive fuel oil desulfurization coupling technology |
| CN102876361B (en) * | 2012-09-28 | 2015-08-26 | 西南石油大学 | A kind of coupling method of petroleum naphtha Porous deproteinized bone-vehicle fuel oil desulfurization |
| CN105861030A (en) * | 2014-12-24 | 2016-08-17 | 神华集团有限责任公司 | Gasoline alkylating and desulfurizing method based on modified heteropolyacid catalyst and product thereof |
| CN105861030B (en) * | 2014-12-24 | 2018-04-13 | 神华集团有限责任公司 | Gasoline alkylation desulfuration method based on modified heteropolyacid catalyst and products thereof |
| CN108192665A (en) * | 2018-02-05 | 2018-06-22 | 山东星火科学技术研究院 | A kind of gasoline desulfating method |
| CN116396139A (en) * | 2023-06-08 | 2023-07-07 | 新疆天利石化股份有限公司 | Method for catalytic removal of thiophene aromatic heterocyclic sulfur compounds in styrene in fixed bed reactor |
| CN116396139B (en) * | 2023-06-08 | 2023-08-18 | 新疆天利石化股份有限公司 | Method for catalytic removal of thiophene aromatic heterocyclic sulfur compounds in styrene in fixed bed reactor |
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Application publication date: 20110601 |