CN106883872A

CN106883872A - Deep gasoline desulfurization device adopting and method

Info

Publication number: CN106883872A
Application number: CN201510931413.6A
Authority: CN
Inventors: 徐新良; 徐亚荣; 张力
Original assignee: China Petroleum and Natural Gas Co Ltd
Current assignee: China Petroleum and Natural Gas Co Ltd
Priority date: 2015-12-15
Filing date: 2015-12-15
Publication date: 2017-06-23
Anticipated expiration: 2035-12-15
Also published as: CN106883872B

Abstract

A kind of deep gasoline desulfurization device adopting, including pre- hydrogasoline Cutting Tap, Etherification of Light FCC Gasoline reactor, catalytic rectifying column, heavy petrol hydrodesulphurisatioreactors reactors；The invention further relates to deep desulfurization of gasoline method：(1) after full distillation gasoline mixes with hydrogen, pre- hydrogenation light petrol Cutting Tap is initially entered, after removing diolefin and mercaptan, completes the cutting of weight component, obtain tower top light petrol and bottom of towe heavy petrol；(2) tower top light petrol enters Etherification of Light FCC Gasoline reactor, and etherification reaction is carried out with methyl alcohol；(3) bottom of towe heavy petrol enters catalytic rectifying column, catalytic rectifying column is equipped with gasoline alkylate sulfur transfer catalyst, there is alkylated reaction in the thiophene-type sulfide in gasoline, obtain middle gasoline, bottom of towe heavy naphtha after tower top desulfurization in the presence of catalyst with light olefin；(4) olefin(e) centent is down to 25% in bottom of towe heavy naphtha, into the heavy petrol hydrodesulphurisatioreactors reactors, obtains heavy petrol after bottom of towe desulfurization.

Description

Deep gasoline desulfurization device adopting and method

Technical field

The present invention relates to a kind of deep desulfurization of gasoline group technology containing alkyl sulfur transfer techniques.

Background technology

With the development and the enhancing of environmental consciousness of national economy, countries in the world are all carried out to the sulfur content of gasoline The developed countries such as considered critical, America and Europe have implemented " sweet gasoline " (gasoline since two thousand nine Sulfur nutrient is not more than 10 μ g/g) new standard, China from 2010 in the whole country gasoline perform The standard of state III (gasoline sulfur nutrient is not more than 150 μ g/g), is determined on January 1st, 2014 for " state Four " (gasoline sulfur nutrient is not more than 50 μ g/g) gasoline standard implements in full the date, " state five " car Will be in issue, transitional period to 2017 before the end of the year 2013 with gasoline standard (sulfur content is not more than 10ppm) The end of the year.

China's gasoline is constituted and (accounts for more than the 80% of China's gasoline product) based on FCC gasoline component, The characteristics of with high-sulfur, alkene high.Hydrogen addition technology is the important means for effectively removing sulphur in FCC gasoline, It is main based on selective hydrodesulfurization technology at present.Wherein, the Prime-G+ technologies of AXENS companies Relatively broad commercial Application production Europe V clean gasoline is obtained.But due to the difference of domestic and international oil property It is different, for treatment China high-sulfur, alkene FCC gasoline high, when ultra-deep hydrodesulfuration is carried out, use Independent hydrodesulfurization technology can bring alkene to be significantly hydrogenated with saturation, cause loss of octane number larger, economy It is poor.At present, it is domestic still to lack the production that mature technology is used for state V standard clean gasoline.

US6,692635 describe a kind of low-sulphur oil production technology, are characterized in that full cut catalytic gasoline is former Material selectively removing alkadienes first in selective hydrogenation reactor (first reactor), olefinic double bonds are different Structure, mercaptan is converted into higher boiling sulfur compound.Then, selective hydrogenation product is fractionated in a fractionating column It is light fraction and heavy distillat.Heavy distillat is first in the first reaction zone of hydrogenation reactor (second reactor) MoO₃-CoO/Al₂O₃It is hydrogenated with catalyst, by unsaturated sulfide (such as thiophene and its alkylated substituted thiazoline Fen) saturation sulfide (such as thiophane or mercaptan) is converted into, then, in second reaction zone NiO/Al₂O₃It is hydrogenated with catalyst, saturation sulfide is converted into H₂S.The desulfurization degree of the patented method leads to Often it is 80.0%~92.0%, product sulfur content is generally 96 μ g/g~240 μ g/g, research octane number (RON) (RON) 1.4~3.0 units are lost.It has the disadvantage to can not meet oil refining enterprise's production clean gasoline sulphur The technical need of content ≯ 10 μ g/g.

CN101270301A discloses a kind of Etherification of Light FCC Gasoline technique and the catalytically cracked gasoline containing the technique Method for modifying, is by the alkadienes and mercaptan sulfur in FCC gasoline selective hydrogenation and removing gasoline, after hydrogenation By full distillation gasoline cut into gently, weigh two components.Substantial amounts of Tertiary olefin has been concentrated in light petrol, through with first Alcohol is etherified into ether compound, the hydrogenated desulfurization drop alkene of heavy petrol in the presence of catalyst for etherification through two sections Hydrocarbon, after removing sulfide and reduction olefin(e) centent, the aromatic hydrocarbons in heavy petrol after hydrogenation is more, can be through taking out Aromatic hydrocarbons is carried, gasoline component of the heavy petrol rich in alkane after extracting aromatic hydrocarbons can make the raw material of steam cracking ethene, Also it is clean gasoline product that can be reconciled with etherified benzine.The technology light petrol cut point is 60 DEG C, weight vapour After oily hydrodesulfurization, sulfur content in 100 μ g/g, can not meet oil refining enterprise's production clean gasoline sulfur content ≯ The technical need of 10 μ g/g.

CN201310256949.3 discloses a kind of method for modifying of catalytic gasoline of whole fraction.Full cut Catalytically cracked gasoline raw material enters pre- hydroprocessing unit and removes alkadienes.Effluent is de- into selective hydrogenation It is and pungent into octane value recovering reactor after sulphuring treatment reactor, with Hydrobon catalyst haptoreaction Alkane value recovers catalyst haptoreaction, and effluent obtains the upgraded products of low sulfur-bearing after gas-liquid separation.The hair The bright catalytic gasoline of whole fraction by total sulfur content less than 400ppm carries out hydrodesulfurization and octane Value recovery treatment, below 50ppm is down to by upgraded products sulfur content, while loss of octane number is less than one Unit.

The A of CN 104650975 disclose a kind of method of deep desulfurization of gasoline；Gasoline stocks initially enter One reactor removes alkadienes mercaptan heaviness simultaneously, and light, heavy petrol is fractionated into subsequently into fractionating column cutting, After heavy petrol enters the most sulfide of second reactor removing, product enters back into the 3rd reactor and enters Traveling one-step desulfurization, the heavy petrol hydrodesulfurization product for obtaining is mixed to get qualified gasoline and produces with light petrol Product；This method is realizing further deep desulfuration by after second reactor, increasing by the 3rd reactor Meanwhile, second reactor reaction severity is significantly reduced, realize loss of octane number and hydrogen consumption is optimized.

CN 103184071A disclose a kind of method of gasoline desulfurization：Gasoline comprising a small amount of diesel component evaporates Divide and hydrogen is mixed into pre-hydrogenator；Pre- hydrogenation products are fractionated into fractionating column, from fractionating column Tower top light component out enters directly as low-sulphur oil blend component from Fractionator Bottom heavy constituent out Water scrubber removes basic nitrogen compound, enters back into during the alkene thiophene alkylation reactor of one group of series connection makes heavy petrol Exposure fen class sulfide weightening, enter catalytic distillation tower from alkylation reactor gasoline component out, urging Changing in the presence of destilling tower top alkene exposes alkylated phenothiazine catalyst makes remaining exposure fen class sulfide increase weight, together When by gasoline be cut into gently, weigh two components；Light component is directly as low-sulphur oil blend component, heavy constituent It is then the diesel component for being enriched sulfide；The method of the present invention, can be greatly reduced the sulphur in gasoline Content, while reducing the loss of octane number that sweetening process is brought.

The A of CN 102994148 provide a kind of method of deep desulfurization of gasoline, and gasoline stocks and hydrogen are mixed into It is monoolefine to enter pre-hydrogenator by the diene hydrogenation in catalytic gasoline；Pre- hydrogenation products enter a water Wash tower to be washed, the partial alkaline nitride in abjection gasoline, subsequently into a catalytic rectifying tower, Vulcanize the part thiophene-based in gasoline in the presence of the alkene thiophene alkylation catalyst of catalytic rectifying tower top Thing increases weight, while gasoline is cut into light petrol, heavy petrol, three components of light diesel fuel；Heavy gasoline components enter Selectable hydrogenation reactor carries out deep desulfuration, after the hydrogen sulfide that desulfurization product is produced in elimination reaction with Light petrol is mixed to get the gasoline products of deep desulfuration；The light diesel fuel of bottom of towe as hydrodesulfurization raw material, or Make the mediation of low-coagulation diesel oil blend component to dispatch from the factory.

In sum, from terms of the retrieval of patent document, more full fraction hydrogenating gasoline is studied and applied at present Desulfurization technology and weight gasoline selective hydrodesulfurizationmodification technology, in producing country's V normal benzines, gasoline depth Degree desulfurization requirement equipment material is high, while there is alkene degree of saturation greatly, octane number loses big problem. Therefore, further removing product in sulphur, reduce product loss of octane number be current technological development difficult point and Focus.

The content of the invention

Present in prior art while catalytic gasoline deep desulfuration, the loss of octane number of gasoline is larger to ask Topic, it is de- it is an object of the invention to provide a kind of gasoline deep of the transfer reaction of sulphur containing gasoline alkylate distillation technology Sulphur group technology, gasoline alkylate sulphur transfer reaction distillation technology and Etherification of Light FCC Gasoline and heavy petrol hydrogenation are taken off Sulphur is combined, the method with technological process flexibly, reduced investment, gasoline octane while deep desulfuration Value loss is few, it is also possible to be combined with the existing gasoline desulfurization in refinery and raising octane number device.

The present invention provides a kind of deep gasoline desulfurization device adopting, wherein, including pre- hydrogasoline Cutting Tap, light vapour Oily methyltertiarvbutyl ether reactor, catalytic rectifying column, heavy petrol hydrodesulphurisatioreactors reactors；

The pre- hydrogasoline Cutting Tap is provided with the outlet of tower top light petrol, the outlet of bottom of towe heavy petrol and full cut Gasoline entrance；

The Etherification of Light FCC Gasoline reactor is provided with pre- etherified benzine entrance and the outlet of bottom of towe etherified benzine；

The catalytic rectifying column is provided with fuel dispensing outlet in tower top, the outlet of bottom of towe heavy naphtha and urges in advance Change oil product of gasoline entrance；

The heavy petrol hydrodesulphurisatioreactors reactors are provided with tower top and are hydrogenated with sweet oil product entrance, and bottom of towe desulfurization in advance Heavy petrol outlet afterwards；

After full distillation gasoline pipeline is connected with hydrogen gas lines, then with the full distillation gasoline entrance by pipe Line is connected；After tower top light petrol outlet is connected by pipeline with toluene pipeline, then with the pre- ether Change light petrol entrance to be connected by pipeline；The bottom of towe heavy petrol outlet enters with the pre- catalytic gasoline oil product Mouth is connected by pipeline；The bottom of towe heavy naphtha outlet is connected by pipeline with the hydrogen gas lines After, then be hydrogenated with sweet oil product entrance in advance with the tower top and be connected by pipeline.

The present invention also provides a kind of deep desulfurization of gasoline method, and the method is filled using above-mentioned deep desulfurization of gasoline Put, comprise the following steps：

(1) after full distillation gasoline mixes with hydrogen, the pre- hydrogenation light petrol Cutting Tap is initially entered, is taken off After diolefin and mercaptan, the cutting of weight component is completed, cut point is 60~70 DEG C, obtains tower top light petrol With bottom of towe heavy petrol；

(2) tower top light petrol described in step (1) enters the Etherification of Light FCC Gasoline reactor, enters with methyl alcohol Row etherification reaction, sulfur content is less than 10 μ g/g in the etherified benzine after etherification reaction, and octane number is improved 3~5 units；

(3) bottom of towe heavy petrol described in step (1) enters the catalytic rectifying column, and the catalysis is anti- Answer rectifying column that gasoline alkylate sulfur transfer catalyst is housed, work of the thiophene-type sulfide in gasoline in catalyst There is alkylated reaction with light olefin with lower, obtain middle gasoline, bottom of towe heavy naphtha after tower top desulfurization, Middle gasoline and the bottom of towe heavy naphtha cut point are 110~120 DEG C after the tower top desulfurization；

(4) olefin(e) centent is down to 25% in bottom of towe heavy naphtha described in step (4), into described heavy Gasoline hydrodesulfurizationmethod reactor, obtains heavy petrol after bottom of towe desulfurization.

Deep desulfurization of gasoline method of the present invention, wherein, catalytic reaction rectification described in step (3) The process conditions of tower are preferably：Feed liquid weight space velocity is 0.5~1h^-1, the operation temperature control of conversion zone At 90~120 DEG C, bottom temperature is 130 DEG C~160 DEG C, 60~80 DEG C of reflux section temperature, and tower top temperature is not More than 40 DEG C, reflux ratio is 1：2~2：1, catalytic rectifying column atmospheric operation.

Deep desulfurization of gasoline method of the present invention, wherein, thiophene-based vulcanization in middle gasoline after the desulfurization The thing rate of transform is preferably greater than 90%, and middle sulfur content in gasoline is preferably below 15 μ g/g after the desulfurization, pungent Alkane value is not lost.

Deep desulfurization of gasoline method of the present invention, wherein, heavy petrol adds described in the step (5) The process conditions of hydrogen desulfurization reactor are：, preferably at 260~280 DEG C, volume space velocity is preferred during liquid for operation temperature 1.0~5.0h^-1, hydrogen-oil ratio is preferably 100：1~500：1, operating pressure preferably 1.0~3.0MPa.

Deep desulfurization of gasoline method of the present invention, wherein, sulfur content is less than in heavy petrol after the desulfurization It is preferred that 10 μ g/g, loss of octane number is preferably smaller than 2 units.

The present invention can also details are as follows：

The present invention is distributed according to the different hydrocarbons of catalytically cracked gasoline composition and sulphidic species, by light petrol ether Change, middle gasoline alkylate sulphur is shifted and is integrated combining for heavy petrol hydrodesulfurization Process improvement, group The group technology of high-quality state V normal benzine blend components is produced into deep desulfurization of gasoline.Its technological process See accompanying drawing 1, full distillation gasoline A mixes the pre- hydrogenation light petrol for being introduced into Etherification of Light FCC Gasoline unit with hydrogen B Cutting Tap 1, mercaptan sulfur and alkadienes in removing feed gasoline, feed gasoline is cut into two kinds of groups of weight Point, weight component cut point is 60 DEG C~70 DEG C, and light petrol removes light petrol ether from after the extraction of hydrogenation distillation tower top Change reactor 2 carries out etherification reaction with methyl alcohol C；Go to be filled with the anti-of catalyst more than 70 DEG C of gasoline components Answer in rectifying column 3, the thiophene-type sulfide in gasoline occurs alkyl in the presence of catalyst with light olefin Change sulphur transfer reaction, the thiophenic sulfur after alkylated reaction is transferred in heavy component, more than 70 DEG C of gasoline components Reacted rectifying column cuts into two kinds of components of middle heavy petrol, and cut point is 110 DEG C~120 DEG C, gasoline in desulfurization E is extracted out from tower top；The relatively low sulfur-rich heavy petrol of olefin(e) centent discharges heavy petrol hydrodesulfurization list from tower reactor Unit, deep desulfuration is carried out into heavy petrol hydrodesulphurisatioreactors reactors 4, and the heavy petrol F after desulfurization is light with etherificate Gasoline D and middle gasoline E are reconciled, can be as the blend component of production high-quality state V gasoline.

Its feature is described as follows step：

(1) the full distillation gasoline of gasoline initially enters Etherification of Light FCC Gasoline unit, and catalytically cracked gasoline cut enters It is filled with after removing diolefin and mercaptan in the light petrol Cutting Tap of the de- diene removal of mercaptans of selective hydrogenation, weight Component is cut, and cut point is 60~70 DEG C.

(2) light petrol in step (1) enters Etherification of Light FCC Gasoline unit, and etherification reaction is carried out with methyl alcohol, Light petrol sulfur content is less than 10 μ g/g after etherification reaction, and octane number improves 3~5 units.

(3) entering equipped with gasoline alkylate sulphur transfer reaction more than 70 DEG C of gasoline fractions in step (1) In catalyst distillation column reactor section.More than 70 DEG C of gasoline fractions middle heavy two kinds of vapour is cut into through catalytic rectifying tower Oil distillate, to there is alkylation in the thiophene-type sulfide in middle gasoline anti-in the presence of catalyst with light olefin Should.

(4) blend component of the middle gasoline in step (3) directly as clean gasoline.

(5) the heavy petrol olefin(e) centent in step (3) is reduced to 25% or so, de- into heavy petrol hydrogenation Reaction of Salmon-Saxl device desulfurization.

(6) process conditions of catalytic rectifying tower operation are in the step (3)：Feed liquid weight space velocity It is 0.5~1h^-1, at 90 DEG C~120 DEG C, bottom temperature is 130 DEG C~160 for the operation temperature control of conversion zone DEG C, reflux section temperature 60 C~80 DEG C, tower top temperature is not more than 40 DEG C, reflux ratio control 1：2~2：1, Catalytic rectifying tower atmospheric operation.In, heavy petrol cut point be 110~120 DEG C, in middle gasoline thiophene-based vulcanization The thing rate of transform be more than 90%, through alkyl sulfur transfer reaction after, middle content of sulfur in gasoline be below 15 μ g/g, Octane number does not lose.

(7) heavy petrol hydrodesulfurization reaction process conditions in the step (5)：Operation temperature is at 260 DEG C ~280 DEG C, 1.0~5.0h of volume space velocity during liquid^-1, hydrogen-oil ratio is 100：1~500：1, operating pressure 1.0~3.0MPa, the heavy petrol sulfur content after desulfurization is less than 10 μ g/g, and loss of octane number is less than 2 units.

(8) heavy petrol after desulfurization is reconciled with etherified benzine and middle gasoline, by the group technology, Content of sulfur in gasoline is less than 10 μ g/g after mediation, and octane number increases 1-2 unit, can be as production high-quality The blend component of state's V normal benzines.

It is combined by Etherification of Light FCC Gasoline, the transfer of middle gasoline alkylate sulphur and heavy petrol hydrodesulfurizationmodification modification technology Group technology, the light petrol cut point of Etherification of Light FCC Gasoline unit is 60~70 DEG C, and the light petrol for cutting out enters Etherification of Light FCC Gasoline unit, etherification reaction is carried out with methyl alcohol, and light petrol sulfur content is less than 10 μ g/g, and octane number is carried 3~5 units high；Catalytic distillation alkyl sulfur buanch unit, middle heavy petrol cut point is 110~120 DEG C, In middle gasoline the thiophene-type sulfide rate of transform be more than 90%, through alkyl sulfur transfer reaction after, middle gasoline sulfur contains It is below 15 μ g/g to measure, and octane number does not lose；After the hydrogenated desulfurization modification of heavy petrol, sulfur content is less than 10 μ g/g, loss of octane number is less than 2 units.

Gently, in, after heavy petrol mediation, the sulfur content of full distillation gasoline is less than 10 μ g/g, and octane number increases 1-2 unit, can be as the blend component of production high-quality state V gasoline.

The present invention has the following advantages：

The present invention first adds gasoline alkylate sulphur transfer reaction distillation technology and Etherification of Light FCC Gasoline and heavy petrol Combining for hydrogen sulfur removal technology Process improvement is integrated, composition deep desulfurization of gasoline production high-quality state V marks The group technology of quasi- gasoline blend component, flexibly, investment is simple, can be with the existing vapour in refinery for technological process Oily desulfurization and raising octane number device are combined.Gasoline alkylate sulphur transfer reaction distillation technology and light petrol ether Change and heavy petrol hydro-upgrading technology is combined, light petrol cut point can be reduced, obtain the etherificate without sulphur light Gasoline；After middle gasoline is through catalytic distillation alkyl sulfur transfer reaction, without hydrodesulfurization, can be directly as Blend component；Heavy petrol initial boiling point can bring up to 120 DEG C, the heavy petrol hydrodesulfurization unit of reduction it is negative Lotus, due to the olefin(e) centent reduction in heavy petrol, while deep desulfurization of gasoline, it is possible to reduce gasoline is pungent The loss of alkane value.

Brief description of the drawings

Fig. 1：Deep gasoline desulfurization device adopting figure

Wherein, reference

1 pre- hydrogenation light petrol Cutting Tap

2 Etherification of Light FCC Gasoline reactors

3 catalytic rectifying columns

4 heavy petrol hydrodesulphurisatioreactors reactors

5 full distillation gasoline entrances

Fuel dispensing outlet in 6 tower tops

7 bottom of towe heavy petrol are exported

8 pre- etherified benzine entrances

9 bottom of towe etherified benzines are exported

Fuel dispensing outlet in 10 tower tops

11 pre- catalytic gasoline oil product entrances

12 bottom of towe heavy naphthas are exported

13 tower tops are hydrogenated with sweet oil product entrance in advance

Heavy petrol outlet after 14 bottom of towe desulfurization

The full distillation gasolines of A

B hydrogen

C methyl alcohol

D etherified benzines

Middle gasoline after E desulfurization

Heavy petrol after F desulfurization.

Specific embodiment

Embodiments of the invention are elaborated below：The present embodiment is premised on technical solution of the present invention Under implemented, give detailed implementation method and process, but protection scope of the present invention be not limited to it is following Embodiment, the experimental technique of unreceipted actual conditions in the following example, generally according to normal condition.

Referring to the drawings 1, the present embodiment be deep gasoline desulfurization device adopting figure, including pre- hydrogasoline Cutting Tap 1, Etherification of Light FCC Gasoline reactor 2, catalytic rectifying column 3, heavy petrol hydrodesulphurisatioreactors reactors 4；

The pre- hydrogasoline Cutting Tap is provided with tower top light petrol outlet 6, bottom of towe heavy petrol outlet 7 and complete Distillation gasoline entrance 5；

The Etherification of Light FCC Gasoline reactor 2 is provided with pre- etherified benzine entrance 8 and the outlet of bottom of towe etherified benzine 9；

The catalytic rectifying column 3 is provided with fuel dispensing outlet 10, bottom of towe heavy naphtha outlet 12 in tower top And pre- catalytic gasoline oil product entrance 11；

The heavy petrol hydrodesulphurisatioreactors reactors 4 are provided with tower top and are hydrogenated with sweet oil product entrance 13, Yi Jita in advance Heavy petrol outlet 14 after the desulfurization of bottom；

After full distillation gasoline A pipelines are connected with hydrogen B pipelines, then with the full distillation gasoline entrance 5 are connected by pipeline；After the tower top light petrol outlet 6 is connected by pipeline with toluene C pipelines, It is connected by pipeline with the pre- etherified benzine entrance 8 again；Bottom of towe heavy petrol outlet 7 with it is described Pre- catalytic gasoline oil product entrance 11 is connected by pipeline；The bottom of towe heavy naphtha outlet 12 is by pipe After line is connected with the hydrogen B pipelines, then sweet oil product entrance 13 is hydrogenated with advance with the tower top passes through Pipeline is connected.

The embodiment that the present invention is given is that the gasoline deep of the transfer reaction distillation technology of sulphur containing gasoline alkylate takes off The group technology implementation result of sulphur, group technology is by Etherification of Light FCC Gasoline unit, gasoline alkylate sulphur buanch unit And heavy petrol hydrodesulfurizationunit unit is combined, technological process is as described in Figure 1.

The raw material oil property of table 1

Project	Unit	Full fraction
			HK	℃	34.7
10% recovered temperature	℃	53.0
			50% recovered temperature	℃	95.0
90% recovered temperature	℃	169.5
			KK	℃	196.6
Sulfur content	ug/g	226
			RON	-	90.3

The technological condition of Etherification of Light FCC Gasoline unit and heavy petrol hydrodesulfurizationunit unit is shown in Table in each embodiment 2, the technological condition of alkylation desulfurization of gasoline unit is shown in Table 3, is described in detail below.

Embodiment 1：

Etherification of Light FCC Gasoline reaction temperature is 60 DEG C in the embodiment, and reaction pressure is 0.4MPa；Gasoline alkyl Change sulphur buanch unit process conditions：Feed weight air speed 0.5h^-1, reflux ratio 2：1, reaction pressure normal pressure； Heavy petrol hydrodesulfurization reaction temperature is 260 DEG C, hydrogen-oil ratio 500：1, volume space velocity 1.0h during liquid^-1, instead Answer pressure 1.0MPa.

Embodiment 2：

Etherification of Light FCC Gasoline reaction temperature is 65 DEG C in the embodiment, and reaction pressure is 0.4MPa；Gasoline alkyl Change sulphur buanch unit process conditions：Feed weight air speed 0.5h^-1, reflux ratio 1：1, reaction pressure normal pressure； Heavy petrol hydrodesulfurization reaction temperature is 270 DEG C, hydrogen-oil ratio 300：1, volume space velocity 1.0h during liquid^-1, instead Answer pressure 2.0MPa.

Embodiment 3：

Etherification of Light FCC Gasoline reaction temperature is 70 DEG C in the embodiment, and reaction pressure is 0.4MPa；Gasoline alkyl Change sulphur buanch unit process conditions：Feed weight air speed 0.5h^-1, reflux ratio 1：2, reaction pressure normal pressure； Heavy petrol hydrodesulfurization reaction temperature is 280 DEG C, hydrogen-oil ratio 100：1, volume space velocity 1.0h during liquid^-1, instead Answer pressure 3.0MPa.

Embodiment 4：

Etherification of Light FCC Gasoline reaction temperature is 60 DEG C in the embodiment, and reaction pressure is 0.4MPa；Gasoline alkyl Change sulphur buanch unit process conditions：Feed weight air speed 1h^-1, reflux ratio 2：1, reaction pressure normal pressure；Weight Gasoline hydrodesulfurizationmethod reaction temperature is 260 DEG C, hydrogen-oil ratio 500：1, volume space velocity 2.0h during liquid^-1, reaction Pressure 1.0MPa.

Embodiment 5：

Etherification of Light FCC Gasoline reaction temperature is 65 DEG C in the embodiment, and reaction pressure is 0.4MPa；Gasoline alkyl Change sulphur buanch unit process conditions：Feed weight air speed 1h^-1, reflux ratio 1：1, reaction pressure normal pressure；Weight Gasoline hydrodesulfurizationmethod reaction temperature is 270 DEG C, hydrogen-oil ratio 300：1, volume space velocity 2.0h during liquid^-1, reaction Pressure 2.0MPa.

Embodiment 6：

Etherification of Light FCC Gasoline reaction temperature is 70 DEG C in the embodiment, and reaction pressure is 0.4MPa；Gasoline alkyl Change sulphur buanch unit process conditions：Feed weight air speed 1h^-1, reflux ratio 1：2, reaction pressure normal pressure；Weight Gasoline hydrodesulfurizationmethod reaction temperature is 280 DEG C, hydrogen-oil ratio 100：1, volume space velocity 2.0h during liquid^-1, reaction Pressure 3.0MPa.

The technological condition of the Etherification of Light FCC Gasoline unit of table 2 and heavy petrol hydrodesulfurizationunit unit

Each embodiment gasoline alkylate prevailing operating conditions of table 3

It is light in each embodiment, in, the heavy petrol and sulfur content and octane number situation of whole-distillate gasoline are shown in after reconciling Table 4

Each gasoline component property of table 4

As can be seen from Table 4 using the process conditions of each embodiment, the sulfur content of the full distillation gasoline after mediation Less than 10 μ g/g, octane number increased 1~1.9 unit, can be as production high-quality state V gasoline Blend component.

Claims

1. a kind of deep gasoline desulfurization device adopting, it is characterised in that including pre- hydrogasoline Cutting Tap, light vapour Oily methyltertiarvbutyl ether reactor, catalytic rectifying column, heavy petrol hydrodesulphurisatioreactors reactors；

2. a kind of deep desulfurization of gasoline method, deep desulfurization of gasoline dress described in the method usage right requirement 1 Put, comprise the following steps：

(4) olefin(e) centent is down to 25% in bottom of towe heavy naphtha described in step (3), into described heavy Gasoline hydrodesulfurizationmethod reactor, obtains heavy petrol after bottom of towe desulfurization.

3. deep desulfurization of gasoline method according to claim 2, it is characterised in that in step (3) The process conditions of the catalytic rectifying column are：Feed liquid weight space velocity is 0.5~1h^-1, conversion zone At 90~120 DEG C, bottom temperature is 130 DEG C~160 DEG C, 60~80 DEG C of reflux section temperature for operation temperature control, Tower top temperature is not more than 40 DEG C, and reflux ratio is 1：2~2：1, catalytic rectifying column atmospheric operation.

4. deep desulfurization of gasoline method according to claim 3, it is characterised in that after the desulfurization The thiophene-type sulfide rate of transform is more than 90% in middle gasoline, and middle sulfur content in gasoline is 15 μ g/g after the desulfurization Hereinafter, octane number does not lose.

5. the deep desulfurization of gasoline method according to any one of claim 2~4, it is characterised in that institute The process conditions for stating heavy petrol hydrodesulphurisatioreactors reactors described in step (4) are：Operation temperature is 260~280 DEG C, 1.0~5.0h of volume space velocity during liquid^-1, hydrogen-oil ratio is 100：1~500：1,1.0~3.0MPa of operating pressure.

6. deep desulfurization of gasoline method according to claim 5, it is characterised in that after the desulfurization Sulfur content is less than 10 μ g/g in heavy petrol, and loss of octane number is less than 2 units.