CN102604672A - Method for producing low-sulfur gasoline - Google Patents
Method for producing low-sulfur gasoline Download PDFInfo
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- CN102604672A CN102604672A CN2011100225919A CN201110022591A CN102604672A CN 102604672 A CN102604672 A CN 102604672A CN 2011100225919 A CN2011100225919 A CN 2011100225919A CN 201110022591 A CN201110022591 A CN 201110022591A CN 102604672 A CN102604672 A CN 102604672A
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Abstract
The invention discloses a method for producing low-sulfur gasoline. The method comprises the following steps of: (1) cutting gasoline raw materials into light gasoline fractions and heavy gasoline fractions, wherein the cutting temperature of the light gasoline fractions and the heavy gasoline fractions is 50-100 DEG C; (2) carrying out alkali-washing desulfurization on the light gasoline fractions, and obtaining desulfurized light gasoline fractions; (3) under the existence of hydrogen and a catalyst A, carrying out primary desulfurization reaction on the heavy gasoline fractions, and obtaining the hydrogenated and desulfurized heavy gasoline fractions after separation; (4) under the existence of hydrogen or hydrogen-containing gas and a catalyst B, carrying out secondary desulfurization reaction on the hydrogenated and desulfurized heavy gasoline fractions, and obtaining the low-sulfur heavy gasoline fractions after separation; and (5) mixing the light gasoline fractions obtained in the step (2) and the heavy gasoline fractions obtained in the step (4), and obtaining a gasoline product. Compared with the prior art, the gasoline produced by the method is low in sulfur content and low in olefin saturation rate, and has good desulfuration selectivity.
Description
Technical field
The present invention relates to a kind of method of producing low-sulphur oil.
Background technology
Atmospheric pollution is a serious environmental problem, and a large amount of engine emissions is to cause one of air-polluting major reason.In recent years, be the protection environment, countries in the world have proposed more strict restriction to the composition of motor spirit, to reduce emission of harmful substances.
At present, the sulphur of China's gasoline product has 90%～99% from catalytically cracked gasoline, and therefore, reducing sulfur content of catalytic cracking gasoline is the key point that reduces the finished product content of sulfur in gasoline.
Adopting catalytically cracked material hydrogenation pre-treatment (front-end hydrogenation) or catalytic gasoline hydrogenation desulfurization (back end hydrogenation) is two kinds of technical schemes of the sulphur content of alternative reduction catalytically cracked gasoline.Wherein, The catalytically cracked material pre-treatment can significantly reduce the sulphur content of catalytically cracked gasoline, but need all operate under the exacting terms very much at temperature and pressure, simultaneously because unit capacity is big; Cause the hydrogen consumption also bigger, these all will improve the investment or the running cost of device.However, because the heaviness of world's crude oil, increasing CCU begins to handle the inferior raw material that contains normal, vacuum residuum etc., so catalytically cracked material hydrogenation unit amount is also increasing year by year.
Compare front-end hydrogenation, the catalytic gasoline hydrogenation desulfurization all is being lower than the pre-treatment of catalytically cracked material hydrogenation aspect plant investment, production cost and the hydrogen consumption.But conventional catalysts and technology are in hydrogenating desulfurization, and the alkene saturated meeting of hydrogenation significantly causes the product loss of octane number very big.One of effective way that addresses the above problem is exactly to adopt the selective hydrodesulfurization technology that catalytically cracked gasoline is handled.The selective hydrodesulfurization technology is removing sulfide in petrol simultaneously, and gasoline olefin is saturated few, can farthest reduce the product loss of octane number.
Summary of the invention
The technical problem that the present invention will solve provides a kind of working method of new low-sulphur oil.
Contriver of the present invention finds that under study for action in the gasoline hydrodesulfurizationmethod process, alkene wherein and hydrogenation reaction generate H
2S can generate new mercaptan (being called regeneration mercaptan) and remain in the product.For the gasoline fraction oil that is rich in alkene, the gasoline fraction sulphur content is low more behind the hydrogenation, and the mercaptan proportion of wherein regenerating is big more, therefore in order to produce low-sulfur and super low-sulfur oil, must remove the regeneration mercaptan in the gasoline fraction behind the hydrogenation.
The present invention relates to a kind of working method of low-sulphur oil, comprise the following steps:
(1) gasoline stocks is cut into light gasoline fraction, heavy naphtha, wherein, the cut point of light gasoline fraction and heavy naphtha is 50 ℃～100 ℃;
(2) light gasoline fraction is carried out caustic wash desulfuration, obtain the light gasoline fraction after the desulfurization;
(3) in the presence of hydrogen and catalyst A, make heavy naphtha carry out the once desulfurization reaction, through separating the heavy naphtha oil after obtaining hydrogenating desulfurization;
(4) in the presence of hydrogen or hydrogen-containing gas and catalyst B, make the heavy naphtha after the hydrogenating desulfurization carry out the secondary desulphurization reaction, obtain low-sulphur oil through separating;
(5) light gasoline fraction that step (2) is obtained mixes with the heavy naphtha that step (4) obtains and obtains gasoline products;
Wherein, the condition of said once desulfurization reaction comprises: volume space velocity 3h when reaction pressure 0.8MPa-3.2MPa, 200 ℃-320 ℃ of temperature of reaction, feeding liquid
-1-8h
-1, hydrogen and raw oil volume ratio (hydrogen-oil ratio) be 200-600; The condition of said secondary desulphurization reaction comprises: temperature of reaction is 100-350 ℃, and pressure is 0.2-6MPa, and mass space velocity is 1-12h during feeding liquid
-1, hydrogen or hydrogen-containing gas and raw oil volume ratio are 2-200; Said catalyst A contains carrier and is carried on the metal component with hydrogenation-dehydrogenation activity on this carrier, is benchmark in oxide compound and with the catalyzer, and the content with hydrogenation-dehydrogenation activity metal component in the said catalyzer is 5～35 weight %; Said catalyst B contains carrier and has hydrogenation-dehydrogenation activity metal component with being carried on this carrier, is benchmark in oxide compound and with the catalyzer, and the content with hydrogenation-dehydrogenation activity metal component in the said catalyzer is 5～35 weight %.
Said once desulfurization reaction is hydrodesulfurization reaction, and preferred reaction conditions comprises: volume space velocity 3h when reaction pressure 1MPa-2.4MPa, 220 ℃-270 ℃ of temperature of reaction, gasoline fraction fluid
-1-6h
-1, hydrogen to oil volume ratio 300-500.
Said secondary desulphurization reaction is a main purpose to remove regeneration mercaptan, be a kind of by mercaptan contain have hydrogenation-catalyst action of dehydrogenation activity metal component decomposes down and the desulphurization reaction of the non-hydro of realization.Preferred reaction conditions comprises: temperature of reaction is 140-240 ℃, and pressure is 0.4-2.5MPa, and mass space velocity is 2-10h during feeding liquid
-1, hydrogen or hydrogen-containing gas and raw oil volume ratio are 5-120.
According to method provided by the invention, described catalyst A and catalyst B can be the same or different, and they can be the combinations that any its composition that prior art provides can satisfy the catalyzer or the catalyzer of aforementioned requirement.In preferred embodiment, said catalyst A is preferably carried out prevulcanized before use, is converted into sulfide so that wherein have hydrogenation-dehydrogenation activity metal component; Catalyst B then need not carried out prevulcanized in use, and promptly preferably having hydrogenation-dehydrogenation activity metal component is oxide compound.
In a kind of embodiment, the carrier of said catalyst A is preferably aluminum oxide or silica-alumina, and said have hydrogenation-dehydrogenation activity metal component and be preferably the metal component that is selected from least a group vib and at least a VIII family.In oxide compound and with the catalyzer is benchmark; Being selected from the vib metal components contents in the preferred said catalyzer is 5～30 heavy %; The content of VIII metal component is 0.5～5 heavy %; Optionally said catalyzer can also contain adjuvant component, for example contains a spot of auxiliary agent that is selected from IA main group, IIA main group or VA subgroup.About the example of this type of catalyzer as, at 200710099304.8,200710099302.9,200710099834.2 disclosed catalyzer respectively, they can be used for the present invention as catalyzer.The carrier of said catalyst B is preferably aluminum oxide, said have hydrogenation-dehydrogenation activity metal component be preferably be selected from least a VIB and with at least a VIII metal component.In oxide compound and with the catalyzer is benchmark, and being selected from the vib metal components contents in the preferred said catalyzer is 4～15 heavy %, and the content of VIII metal component is 1～5 heavy %.
According to method provided by the present invention, wherein said separation, its method and for realizing that the required device of this method is the usual method and apparatus that adopts in this area.For example, adopt that the habitual apparatus and method in this area carry out to generating oil that gas is carried, distillation etc., generate hydrogen sulfide and other the non-gasoline components that contains in the oil to remove.
Be enough to make said charging under the prerequisite that contacts with said catalyzer under the said reaction conditions, the present invention is to the not special restriction of said reactor drum.For example, the said reactor drum that carries out the once desulfurization reaction can be any reactor drum that is suitable for gasoline fraction oil hydrodesulfurization reaction, for example a fixed bed hydrogenation reactor in the prior art.The said reactor drum that carries out the secondary desulphurization reaction can be to comprise various forms of reactor drums such as fixed-bed reactor, fluidized-bed reactor, distillation column reactor or ebullated bed reactor.In preferred embodiment; The said reactor drum that carries out the secondary desulphurization reaction is preferably counter-current reactor, and the gasoline fraction after the promptly said hydrogenating desulfurization flows in reactor drum from top to bottom, said hydrogen or hydrogen-containing gas flow from bottom to top and contact with catalyst B.In counter-current reactor, the gasoline fraction after the hydrogenating desulfurization and hydrogen or hydrogen-containing gas reverse contact in the presence of catalyzer are with the H of reaction generation
2S in time shifts out beds, and hydrogen or hydrogen-containing gas medium are taken reactor drum out of.Described counter-current reactor can be a various forms, for example, can be fixed bed, fluidized-bed, distillation tower or ebullated bed reactor etc., also can in stripping tower that is filled with catalyst B or stabilizer tower, carry out.In the gasoline hydrogenation technology of routine; General all have stripping tower or stabilizer tower in order to remove lighter hydrocarbons and hydrogen sulfide such as the methane in the gasoline, ethane behind the hydrogenation; Utilize stripping tower or stabilizer tower in the existing hydrogenation unit; When removing reacted regeneration mercaptan and lighter hydrocarbons and hydrogen sulfide, can simplify technical process, save facility investment.When the reactor drum of said secondary desulphurization reaction was selected counter-current reactor, said hydrogen or hydrogen-containing gas and raw oil volume ratio further were preferably 5-40.
Said hydrogen can be that pure hydrogen gas also can be the refinery gas that is rich in hydrogen, and for example the hydrogen volume percentage composition is the refinery gas more than 70%, and preferred hydrogen volume percentage composition is the refinery gas (comprising circulating hydrogen) more than 80%
Said hydrogen-containing gas be hydrogen with arbitrarily under the secondary desulphurization reaction condition with hydrogenating desulfurization after gasoline fraction be the gas of inert reaction; For example, they can be one or more the mixtures that is selected from nitrogen, carbonic acid gas, carbon monoxide, hydro carbons, water vapour.According to method provided by the invention, wherein the content to hydrogen in the said hydrogen-containing gas has no particular limits, and in concrete embodiment, being preferably hydrogen content is not less than 1 volume % usually.When said hydrogen-containing gas is the gas mixture of hydrogen and hydro carbons; Said hydrogen-containing gas can be the refinery gas that is rich in hydrogen; For example the hydrogen volume percentage composition is the refinery gas more than 70%, and preferred hydrogen volume percentage composition is the refinery gas (comprising circulating hydrogen) more than 80%.
According to method provided by the invention, said gasoline stocks oil can be catalytically cracked gasoline distillate, catalytic cracking gasoline distillate, straight-run spirit distillate, coker oil, pyrolysis gasoline cut fraction is oily and the pressure gasoline distillate in one or more.The boiling range of said gasoline stocks oil is the usual boiling range of gasoline fraction oil, for example: can be 30-220 ℃.
The cut point of said light gasoline fraction and heavy naphtha is preferably 50-75 ℃.In preferred embodiment, be respectively the heavy % in 30 heavy %～60 and the heavy % in 40 heavy %～70 of gasoline stocks through the yield that cuts said light gasoline fraction and heavy naphtha.
According to method provided by the present invention, wherein, the method for said caustic wash desulfuration and operational condition are this area conventional process and condition.For example, the extractive method of alkali cleaning, the extractive operational condition of said alkali cleaning comprises: oily alkali volume ratio 15: 1-1: 1, extraction temperature is less than 40 ℃, extracting pressure 0.1MPa-0.8MPa.Carried out description about these methods 350 pages of " petroleum refining engineering " (volume two) (petroleum industry press, Lin Shixiong work, version in 1988), quoted as a reference here.
According to method provided by the invention, also comprise in said step (3) and to introduce a kind of heavy distillate, the over point of said heavy distillate is greater than the final boiling point of said gasoline stocks oil, volume space velocity during in liquid, the liquid hourly space velocity of introducing heavy distillate is 0.2h
-1-2h
-1
The contriver finds under study for action, when in the once desulfurization reaction, introducing the selectivity that heavy distillate can significantly further improve hydrodesulfurization reaction.
Guarantee to be enough to said heavy distillate introduced and with condition that catalyzer contact under, the present invention does not limit the introducing method of said heavy distillate.For example, can be that said heavy distillate is at first mixed with gasoline fraction oil, introduce reactor drum afterwards and under the gasoline selective hydrodesulfurizationmodification reaction conditions, contact with catalyzer; Also can be that said heavy distillate and gasoline fraction oil raw material are introduced reactor drum respectively.Wherein, Said heavy distillate is selected from diesel oil distillate oil and/or lubricating oil distillate, and the temperature difference of the final boiling point of the over point of said heavy distillate and said gasoline fraction oil is not less than 1 ℃, preferably is not less than 10 ℃; Further preferably be not less than 20 ℃, more preferably be not less than 40 ℃.The liquid hourly space velocity of introducing heavy distillate is preferably 0.4h
-1-1.8h
-1, further be preferably 0.6h
-1.8h
-1Said heavy distillate is derived from one or more in oil, the synthetic oil (for example: be selected from olefin oligomerization synthetic oil, Fischer-Tropsch synthesis oil and biosynthesizing oil).Under reaction conditions according to the invention, wherein said heavy distillate at least partly exists with the form of liquid.
When said step (3) also comprised the step of introducing a kind of heavy distillate, wherein said separation comprises distilled the gained reaction product (comprising the flash distillation distillation) separation steps.The gasoline fraction oil that obtains through fractionation by distillation carries out the secondary desulphurization reaction, and heavy distillate can partly or entirely recycle.
In a preferred embodiment, the inventive method comprises the steps:
(1) gasoline stocks is cut into light gasoline fraction, heavy naphtha, wherein, the cut point of light gasoline fraction and heavy naphtha is 50 ℃～100 ℃;
(2) light gasoline fraction is carried out caustic wash desulfuration, obtain the light gasoline fraction after the desulfurization;
(3) heavy distillate, heavy naphtha and hydrogen are introduced the reactor drum that is filled with catalyst A and carry out hydrodesulfurization reaction one time, the condition of once desulfurization reaction comprises: volume space velocity 3～8h during the liquid of reaction pressure 0.8～3.2MPa, 200～320 ℃ of temperature of reaction, gasoline fraction oil
-1, heavy distillate liquid the time volume space velocity 0.2-2h
-1, hydrogen to oil volume ratio 200～600;
(4) product of step (3) is introduced stripping tower, remove the H in the product through stripping
2Light constituents such as S.
(5) bottom stream of step (4) is introduced separation column and carry out fractionation by distillation, isolate gasoline fraction and heavy distillate;
(6) gasoline fraction that hydrogen or hydrogen-containing gas and step (5) is obtained is introduced the counter-current reactor that is filled with catalyst B and is carried out the secondary desulphurization reaction; The condition of secondary desulphurization reaction comprises: temperature of reaction is 100-350 ℃; Pressure is 0.2-6MPa, and mass space velocity is 1-12h during feeding liquid
-1, hydrogen or hydrogen-containing gas and raw oil volume ratio are 2-200;
Wherein, Said heavy distillate is selected from diesel oil distillate oil and/or lubricating oil distillate, and the temperature difference of the final boiling point of the over point of said heavy distillate and said gasoline fraction oil is not less than 1 ℃, preferably is not less than 10 ℃; Further preferably be not less than 20 ℃, more preferably be not less than 40 ℃.Said heavy distillate is derived from one or more in oil, the synthetic oil (for example: be selected from olefin oligomerization synthetic oil, Fischer-Tropsch synthesis oil and biosynthesizing oil).Under reaction conditions according to the invention, wherein said heavy distillate at least partly exists with the form of liquid.
The condition of preferred once desulfurization reaction comprises: volume space velocity 3h when reaction pressure 1MPa-2.4MPa, 220 ℃-270 ℃ of temperature of reaction, gasoline fraction fluid
-1-6h
-1, heavy distillate liquid the time volume space velocity be 0.4h
-1-1.8h
-1, further volume space velocity is 0.6h during the liquid of preferred heavy distillate
-1-1.8h
- 1, hydrogen to oil volume ratio 300-500.
The reaction conditions of preferred secondary desulfurization comprises: temperature of reaction is 140-240 ℃, and pressure is 0.4-2.5MPa, and mass space velocity is 2-10h during feeding liquid
-1, hydrogen or hydrogen-containing gas and raw oil volume ratio are 2-200, are preferably 5-120, further are preferably 5-40.
The heavy distillate that obtains through step (5) fractionation by distillation returns step (3) and recycles.In the step (6); Gasoline fraction flows through beds from top to bottom; With hydrogen or the hydrogen-containing gas counter current contact introduced by reactor bottom, the regeneration mercaptan in the said gasoline fraction is decomposed into alkene and hydrogen sulfide on catalyzer, and the hydrogen sulfide in the fluid, lighter hydrocarbons shift out reaction zone with the stripping medium; The stripping medium of sulfide hydrogen and lighter hydrocarbons is discharged on counter-current reactor top, and reactor bottom has obtained removing the gasoline products of mercaptan.
Said catalyst A contains carrier and has hydrogenation-dehydrogenation activity metal component with being carried on the carrier, is benchmark in oxide compound and with the catalyzer, and the content with hydrogenation-dehydrogenation activity metal component in the said catalyzer is 5～35 weight %; Said catalyst B contains carrier and has hydrogenation-dehydrogenation activity metal component with being carried on the carrier, is benchmark in oxide compound and with the catalyzer, and the content with hydrogenation-dehydrogenation activity metal component in the said catalyzer is 5～35 weight %.The carrier of said catalyst A is preferably aluminum oxide or silica-alumina, and said have hydrogenation-dehydrogenation activity metal component and be preferably the metal component that is selected from least a group vib and at least a VIII family.In oxide compound and with the catalyzer is benchmark; Being selected from the vib metal components contents in the preferred said catalyzer is 5～30 heavy %; The content of VIII metal component is 0.5～5 heavy %; Optionally said catalyzer can also contain adjuvant component, for example contains a spot of auxiliary agent that is selected from IA main group, IIA main group, IIIA or VB subgroup.About the example of this type of catalyzer as, at 200710099304.8,200710099302.9,200710099834.2 disclosed catalyzer respectively, they can be used for the present invention as catalyzer.The carrier of said catalyst B is preferably aluminum oxide, said have hydrogenation-dehydrogenation activity metal component be preferably be selected from least a VIB and with at least a VIII metal component.In oxide compound and with the catalyzer is benchmark, and being selected from the vib metal components contents in the preferred said catalyzer is 4～15 heavy %, and the content of VIII metal component is 1～5 heavy %.
In preferred embodiment, said catalyst A is preferably carried out prevulcanized before use, is converted into sulfide so that wherein have hydrogenation-dehydrogenation activity metal component; Catalyst B then need not carried out prevulcanized in use, and promptly preferably having hydrogenation-dehydrogenation activity metal component is oxide compound.
Described counter-current reactor can be a various forms, comprises fixed bed, fluidized-bed, distillation tower or ebullated bed reactor etc., also can in stripping tower that is filled with catalyst B or stabilizer tower, carry out.In the gasoline hydrogenation technology of routine; General all have stripping tower or stabilizer tower in order to remove lighter hydrocarbons and hydrogen sulfide such as the methane in the gasoline, ethane behind the hydrogenation; Utilize stripping tower or stabilizer tower in the existing hydrogenation unit; When removing reacted regeneration mercaptan and lighter hydrocarbons and hydrogen sulfide, can simplify technical process, save facility investment.In counter-current reactor, the gasoline fraction after the hydrogenating desulfurization and hydrogen or hydrogen-containing gas reverse contact in the presence of catalyzer are with the H of reaction generation
2S in time shifts out beds, and is taken out of reactor drum by hydrogen or hydrogen-containing gas medium.When the reactor drum of said secondary desulphurization reaction was selected counter-current reactor, said hydrogen or hydrogen-containing gas and raw oil volume ratio further were preferably 5-40.
According to method provided by the invention, said gasoline stocks oil can be catalytically cracked gasoline distillate, catalytic cracking gasoline distillate, straight-run spirit distillate, coker oil, pyrolysis gasoline cut fraction is oily and the pressure gasoline distillate in one or more.The boiling range of said gasoline stocks oil is the usual boiling range of gasoline fraction oil, for example: can be 30-220 ℃.
Said hydrogen-containing gas be hydrogen with arbitrarily under the secondary desulphurization reaction condition with hydrogenating desulfurization after gasoline fraction be the gas of inert reaction; For example; They can be one or more the mixtures that is selected from nitrogen, carbonic acid gas, carbon monoxide, hydro carbons, water vapour, preferred hydro carbons.According to method provided by the invention, wherein the content to hydrogen in the said hydrogen-containing gas has no particular limits, and in concrete embodiment, being preferably hydrogen content is not less than 1 volume % usually.
Compared with prior art, the sulphur content of the inventive method production gasoline is low, the alkene saturation exponent is low, has good desulfuration selectivity.Particularly; When said secondary desulphurization reaction carries out in counter-current reactor; Hydrogen sulfide in the fluid, lighter hydrocarbons are with shifting out reaction zone on hydrogen or the hydrogen-containing gas, and the stripping medium of sulfide hydrogen and lighter hydrocarbons is discharged on counter-current reactor top, and reactor bottom has obtained removing the gasoline products of mercaptan.Therefore, can the realization response product separation when accomplishing reaction.
Description of drawings
Figure-1 provides a kind of schematic flow sheet of method for the present invention.
Embodiment
The present invention provides a kind of of method preferred embodiment to realize by flow process shown in Figure 1.
According to flow process shown in Figure 1, gasoline stocks gets into separation column 2 through pipeline 3 and is cut into light gasoline fraction, heavy naphtha, and wherein light gasoline fraction gets into soda-wash tower 30 through pipeline 4 and removes mercaptan removal; Heavy naphtha and heavy distillate get into pumps 6 through pipeline 5 to be mixed with hydrogen from pipeline 19; Get into process furnace 8 through pipeline 7, the material after the heating gets into the once desulfurization reactor drum 10 that is filled with catalyst A through pipeline 9 and carries out desulphurization reaction, and hydrogenated oil gets into flashing tower 12 through pipeline 11; Through flash separation is gasoline fraction, heavy distillate; Wherein heavy distillate turns back to process furnace through pipeline 14, recycles, and gasoline fraction gets into HP separator 15 through pipeline 13; The hydrogen-rich gas that comes out from HP separator 15 tops gets into compressor 17 through pipeline 16; Hydrogen-rich gas after the compression mixes through pipeline 18 or with the additional fresh hydrogen from pipeline 1, mixes hydrogen through pipeline 19, with gasoline stocks that comes self-pumping 6 and heavy distillate raw materials mix dereaction.The liquid stream that comes out from separator 15 bottoms gets into the secondary desulphurization reactor 21 that is filled with catalyst B through pipeline 20, and secondary desulphurization reactor 21 is a kind of stripping tower of routine, is catalyst B with the conventional gas stripping column filler that different is wherein.Hydrogen sulfide in the charging, lighter hydrocarbons separate with gasoline fraction in stripping tower.Gasoline flows downward in tower and hydrogen that rises or hydrogen-containing gas (preferred here hydrogen-containing gas; Be the hydrocarbon of the gasification of hydrogen) counter current contact on mercaptan-eliminating catalyst; Liquid flows out from pipeline 26 at the bottom of the tower behind the mercaptan removal; The heavy naphtha of a part after pipeline 29 obtains mercaptan removal mixes with light gasoline fraction behind the mercaptan removal of pipeline 31, must go out device through pipeline 32 by gasoline products.Another part returns in the tower through pipeline 28 after getting into the reboiler vaporization.Part hydrocarbon ils steam, hydrogen sulfide and lighter hydrocarbons distillate from cat head; Get into condensing surface through pipeline 22 and carry out condensation; Get into separator 23 after the condensation; Through pipeline 24 emptyings, the liquid product that comes out from separator 23 bottoms is back in the stripping tower through pipeline 25 lighter hydrocarbons such as hydrogen sulfide that comes out from separator 23 tops and methane, ethane, propane as non-condensable gas.
Above-mentioned flow process is the preferred process of introducing heavy distillate; Do not introducing under the heavy ends oil condition; Reaction still can be carried out in flow process shown in Figure 1, and different is the flashing tower 12 that can save in the flow process, and once desulfurization generates oil to be separated through pipeline 11 entering HP separators 15.
Following embodiment will further explain method provided by the invention, but therefore not limit the present invention.
Comparative Examples and embodiment catalyst system therefor A are numbered RSE-1, are benchmark in oxide compound and with the catalyzer, and RSE-1 consists of: cobalt contents 2.3 weight %, and molybdenum content 14.8 weight %, boron oxide content 3.1 weight %, surplus is an alumina supporter; Catalyst B be numbered RSS-1, be benchmark in oxide compound and with the catalyzer, RSS-1 consists of: nickel content 4.5 weight %, W content 13.6 weight %, surplus is an alumina supporter.
Produce low-sulphur oil according to flow process shown in Figure 1.
Gasoline stocks oil is catalytic cracking full distillate gasoline, and character is seen table 1.Obtain light gasoline fraction and heavy naphtha through the fractionation cutting, cut point is 65 ℃.Light gasoline fraction and heavy naphtha character are listed in table 1.
Light gasoline fraction is gone into the soda-wash tower mercaptan removal, and operational condition is: 30 ℃ of extraction temperatures, and pressure 0.4MPa,, concentration of lye 15%, oily alkali volume ratio 10: 1.
Heavy naphtha and heavy distillate mixing raw material C go into a hydrodesulphurisatioreactors reactors and carry out desulfurization, and the character of mixing raw material C is listed in table 1.Heavy naphtha is gone into the secondary desulphurization reactor and is carried out desulfurization after the hydrogenating desulfurization.Catalyst A is RSE-1, and catalyst B is RSS-1.
The once desulfurization reaction conditions is: temperature of reaction is 260 ℃, and reaction pressure is 1.6MPa, and the gasoline feeding volume space velocity is 4h
-1, the gasoline feeding hydrogen to oil volume ratio is 400.The character of heavy naphtha is listed in table 2 after the hydrogenating desulfurization.
Secondary desulphurization reaction condition is: pressure is 1.1MPa, and the following beds medial temperature of charging is 200 ℃, charging mass space velocity 3h
-1, (mixed gas of hydrogen and nitrogen consists of hydrogen-containing gas: be 7 with the raw oil volume ratio hydrogen volume per-cent 10%).The character of heavy naphtha is listed in table 3 after the secondary desulfurization.
Light gasoline fraction mixes and obtains gasoline products S1 behind the heavy naphtha of secondary desulfurization and the caustic wash desulfuration, and its character is seen table 4.
Save flashing tower 8 in flow process shown in Figure 1, and produce low-sulphur oil according to this flow process.
Gasoline stocks oil is with embodiment 1, and character is seen table 1.Obtain light gasoline fraction and heavy naphtha through the fractionation cutting, cut point is 65 ℃.Light gasoline fraction and heavy naphtha character are listed in table 1.
Light gasoline fraction is gone into the soda-wash tower mercaptan removal, and operational condition is: 30 ℃ of extraction temperatures, and pressure 0.4MPa,, concentration of lye 15%, oily alkali volume ratio 10: 1.
Heavy naphtha oil is gone into a hydrodesulphurisatioreactors reactors and is carried out hydrodesulfurization reaction, and heavy naphtha oiliness matter is listed in table 1.Heavy naphtha is gone into the secondary desulphurization reactor and is carried out desulfurization after the hydrogenating desulfurization.Catalyst A is RSE-1, and catalyst B is RSS-1.
The once desulfurization reaction conditions is: temperature of reaction is 260 ℃, and reaction pressure is 1.6MPa, and the gasoline feeding volume space velocity is 4h
-1, the gasoline feeding hydrogen to oil volume ratio is 400.The character of gasoline fraction is listed in table 2 after the hydrogenating desulfurization.
Secondary desulphurization reaction condition is: pressure is 1.1MPa, and the following beds medial temperature of charging is 200 ℃, charging mass space velocity 3h
-1, hydrogen-containing gas (pure hydrogen gas, hydrogen content volume percent 99.9%) is 7 with the raw oil volume ratio.The character of gasoline products S2 is listed in table 3.
Produce low-sulphur oil according to flow process shown in Figure 1.
Except that once desulfurization reaction conditions and secondary desulphurization reaction condition and embodiment 1 were different, other were with embodiment 1.
The once desulfurization reaction conditions is: temperature of reaction is 245 ℃, and reaction pressure is 1.6MPa, and the gasoline feeding volume space velocity is 3h
-1, the gasoline feeding hydrogen to oil volume ratio is 400.The character of gasoline fraction is listed in table 2 after the hydrogenating desulfurization.
Secondary desulphurization reaction condition is: pressure is 1.1MPa, and the following beds medial temperature of charging is 210 ℃, charging mass space velocity 3h
-1, (mixed gas of hydrogen and nitrogen consists of hydrogen-containing gas: be 30 with the raw oil volume ratio hydrogen volume per-cent 10%).The character of gasoline products S3 is listed in table 3.
Comparative Examples 1
Flow process according to embodiment 2 is produced gasoline products.Different is that the catalyst B in the reactor drum 14 is replaced by conventional fillers.The stripping tower working pressure is 1.1MPa, charging mass space velocity 3h
-1, (mixed gas of hydrogen and nitrogen consists of hydrogen-containing gas: be 7 with the raw oil volume ratio hydrogen volume per-cent 10%).
The character of gasoline fraction is listed in table 2 after the hydrogenating desulfurization, and the character of gasoline products DB1 is listed in table 3.
Table 1
Table 2
Table 3
Table 4
Claims (26)
1. a method of producing low-sulphur oil comprises the following steps:
(1) gasoline stocks is cut into light gasoline fraction, heavy naphtha, wherein, the cut point of light gasoline fraction and heavy naphtha is 50 ℃～100 ℃;
(2) light gasoline fraction is carried out caustic wash desulfuration, obtain the light gasoline fraction after the desulfurization;
(3) in the presence of hydrogen and catalyst A, heavy naphtha is carried out the once desulfurization reaction, through separating the heavy naphtha oil after obtaining hydrogenating desulfurization;
(4) in the presence of hydrogen or hydrogen-containing gas and catalyst B, the heavy naphtha after the hydrogenating desulfurization is carried out the secondary desulphurization reaction, obtain the low-sulfur heavy naphtha through separating;
(5) light gasoline fraction that step (2) is obtained mixes with the heavy naphtha that step (4) obtains and obtains gasoline products;
Wherein, the condition of said once desulfurization reaction comprises: reaction pressure 0.8-3.2MPa, temperature of reaction 200-320 ℃, volume space velocity 3-8h during feeding liquid
-1, hydrogen to oil volume ratio is 200-600; The condition of said secondary desulphurization reaction comprises: temperature of reaction is 100-350 ℃, and pressure is 0.2-6MPa, and mass space velocity is 1-12h during feeding liquid
-1, hydrogen or hydrogen-containing gas and raw oil volume ratio are 2-200; Said catalyst A contains carrier and is carried on the metal component with hydrogenation-dehydrogenation activity on this carrier, is benchmark in oxide compound and with the catalyzer, and the content with hydrogenation-dehydrogenation activity metal component in the said catalyzer is 5～35 weight %; Said catalyst B contains carrier and has hydrogenation-dehydrogenation activity metal component with being carried on this carrier, is benchmark in oxide compound and with the catalyzer, and the content with hydrogenation-dehydrogenation activity metal component in the said catalyzer is 5～35 weight %.
2. method according to claim 1 is characterized in that, the reaction conditions of said once desulfurization reaction comprises: reaction pressure 1-2.4MPa, temperature of reaction 220-270 ℃, volume space velocity 3-6h during gasoline fraction fluid
-1, hydrogen to oil volume ratio 300-500; The reaction conditions of said secondary desulphurization reaction comprises: pressure is 0.4-2.5MPa, and temperature of reaction is 140-240 ℃, and mass space velocity is 2-10h during feeding liquid
-1, hydrogen or hydrogen-containing gas and raw oil volume ratio are 5-120.
3. method according to claim 1; It is characterized in that; The carrier of said catalyst A is aluminum oxide or silica-alumina, and said have a metal component that hydrogenation-dehydrogenation activity metal component is selected from least a group vib and at least a VIII family, is benchmark in oxide compound and with the catalyzer; Being selected from the vib metal components contents in the said catalyzer is 5～30 heavy %, and the content of VIII metal component is 0.5～5 heavy %; The carrier of said catalyst B is an aluminum oxide; Said metal component with hydrogenation-dehydrogenation activity is selected from the metal component of at least a group vib and at least a VIII family; In oxide compound and with the catalyzer is benchmark; Being selected from the vib metal components contents in the said catalyzer is 4～15 heavy %, and the content of VIII metal component is 1～5 heavy %.
4. according to claim 1 or 3 described methods, it is characterized in that said catalyst A is carried out prevulcanized before use.
5. method according to claim 1 is characterized in that, the reactor drum of said secondary desulphurization reaction is a countercurrent reactor.
6. method according to claim 1 is characterized in that, said hydrogen-containing gas be hydrogen with arbitrarily under the secondary desulphurization reaction condition with hydrogenating desulfurization after gasoline fraction be the gas of inert reaction.
7. method according to claim 6 is characterized in that, said rare gas element is selected from one or more mixture of nitrogen, carbonic acid gas, carbon monoxide, hydro carbons, water vapour.
8. method according to claim 1; It is characterized in that; Also comprise a kind of heavy distillate of introducing in said step (3); Said heavy distillate is the distillate of a kind of over point greater than the final boiling point of said gasoline stocks oil, volume space velocity during in liquid, and the liquid hourly space velocity of introducing heavy distillate is 0.2-2h
-1
9. method according to claim 8; It is characterized in that; Said heavy distillate is selected from diesel oil distillate oil and/or lubricating oil distillate, and the temperature difference of the final boiling point of the over point of said heavy distillate and said gasoline fraction oil is not less than 1 ℃, and the liquid hourly space velocity of introducing heavy distillate is 0.4-1.8h
-1
10. method according to claim 9 is characterized in that, the temperature difference of the final boiling point of the over point of said heavy distillate and said gasoline fraction oil is not less than 10 ℃, and the liquid hourly space velocity of introducing heavy distillate is 0.6-1.8h
-1
11. according to Claim 8,9 or 10 described methods, it is characterized in that the temperature difference of the final boiling point of the over point of said heavy distillate and said gasoline fraction oil is not less than 20 ℃.
12. method according to claim 11 is characterized in that, the temperature difference of the final boiling point of the over point of said heavy distillate and said gasoline fraction oil is not less than 40 ℃.
13. according to Claim 8 or 9 described methods, it is characterized in that said heavy distillate is derived from one or more in oil, the synthetic oil.
14. method according to claim 13 is characterized in that, said synthetic oil is selected from olefin oligomerization synthetic oil, Fischer-Tropsch synthesis oil and biosynthesizing oil.
15. method according to claim 1 is characterized in that, one or more in said gasoline fraction grease separation catalytic cracking gasoline, catalytic cracking gasoline, straight-run spirit, coker gasoline, pyrolysis gasoline and the pressure gasoline.
16. method according to claim 15 is characterized in that, the boiling range of said gasoline fraction oil is 30-220 ℃.
17. a method of producing low-sulphur oil comprises the following steps:
(1) gasoline stocks is cut into light gasoline fraction, heavy naphtha, wherein, the cut point of light gasoline fraction and heavy naphtha is 50 ℃～100 ℃;
(2) light gasoline fraction is carried out caustic wash desulfuration, obtain the light gasoline fraction after the desulfurization;
(3) heavy distillate, heavy naphtha and hydrogen are introduced the reactor drum that is filled with catalyst A and carry out hydrodesulfurization reaction one time, the condition of once desulfurization reaction comprises: volume space velocity 3～8h during the liquid of reaction pressure 0.8～3.2MPa, 200～320 ℃ of temperature of reaction, gasoline fraction oil
-1, heavy distillate liquid the time volume space velocity 0.2-2h
-1, hydrogen to oil volume ratio 200～600;
(4) product of step (3) is introduced stripping tower, remove the H in the product through stripping
2Light constituents such as S.
(5) bottom stream of step (4) is introduced separation column and carry out fractionation by distillation, isolate gasoline fraction and heavy distillate;
(6) gasoline fraction that hydrogen or hydrogen-containing gas and step (5) is obtained is introduced the counter-current reactor that is filled with catalyst B and is carried out the secondary desulphurization reaction; The condition of secondary desulphurization reaction comprises: temperature of reaction is 100-350 ℃; Pressure is 0.2-6MPa, and mass space velocity is 1-12h during feeding liquid
-1, hydrogen or hydrogen-containing gas and raw oil volume ratio are 2-200;
Wherein, said catalyst A contains carrier and is carried on the metal component with hydrogenation-dehydrogenation activity on this carrier, is benchmark in oxide compound and with the catalyzer, and the content with hydrogenation-dehydrogenation activity metal component in the said catalyzer is 5～35 weight %; Said catalyst B contains carrier and has hydrogenation-dehydrogenation activity metal component with being carried on this carrier, is benchmark in oxide compound and with the catalyzer, and the content with hydrogenation-dehydrogenation activity metal component in the said catalyzer is 5～35 weight %; Said heavy distillate is the distillate of a kind of over point greater than the final boiling point of said gasoline stocks oil.
18. method according to claim 17 is characterized in that, the reaction conditions of said once desulfurization reaction comprises: reaction pressure 1-2.4MPa, temperature of reaction 220-270 ℃, volume space velocity 3-6h during gasoline fraction fluid
-1, hydrogen to oil volume ratio 300-500; Said heavy distillate is selected from diesel oil distillate oil and/or lubricating oil distillate; The temperature difference of the final boiling point of the over point of said heavy distillate and said gasoline fraction oil is not less than 1 ℃, and the liquid hourly space velocity of introducing heavy distillate is 0.4-1.8h
-1The reaction conditions of said secondary desulphurization reaction comprises: pressure is 0.4-2.5MPa, and temperature of reaction is 140-240 ℃, and mass space velocity is 2-10h during feeding liquid
-1, hydrogen or hydrogen-containing gas and raw oil volume ratio are 5-40.
19. method according to claim 18 is characterized in that, the temperature difference of the final boiling point of the over point of said heavy distillate and said gasoline fraction oil is not less than 10 ℃, and the liquid hourly space velocity of introducing heavy distillate is 0.6-1.8h
-1
20. method according to claim 19 is characterized in that, the temperature difference of the final boiling point of the over point of said heavy distillate and said gasoline fraction oil is not less than 20 ℃.
21. method according to claim 20 is characterized in that, the temperature difference of the final boiling point of the over point of said heavy distillate and said gasoline fraction oil is not less than 40 ℃.
22. method according to claim 17 is characterized in that, said heavy distillate is derived from one or more in oil, the synthetic oil.
23. method according to claim 22 is characterized in that, said synthetic oil is selected from olefin oligomerization synthetic oil, Fischer-Tropsch synthesis oil and biosynthesizing oil.
24. method according to claim 17; It is characterized in that; The carrier of said catalyst A is aluminum oxide or silica-alumina, and said have a metal component that hydrogenation-dehydrogenation activity metal component is selected from least a group vib and at least a VIII family, is benchmark in oxide compound and with the catalyzer; Being selected from the vib metal components contents in the said catalyzer is 5～30 heavy %, and the content of VIII metal component is 0.5～5 heavy %; The carrier of said catalyst B is an aluminum oxide; Said metal component with hydrogenation-dehydrogenation activity is selected from the metal component of at least a group vib and at least a VIII family; In oxide compound and with the catalyzer is benchmark; Being selected from the vib metal components contents in the said catalyzer is 4～15 heavy %, and the content of VIII metal component is 1～5 heavy %.
25. according to claim 17 or 18 described methods, it is characterized in that, said hydrogen-containing gas be hydrogen with arbitrarily under the secondary desulphurization reaction condition with hydrogenating desulfurization after gasoline fraction be the gas of inert reaction.
26. method according to claim 25 is characterized in that, said rare gas element is selected from one or more mixture of nitrogen, carbonic acid gas, carbon monoxide, hydro carbons, water vapour.
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