CN103289739A - Method for modification by coupling hydrodesulfurization of FCC (Fluid Catalytic Cracking) gasoline and aromatization of liquefied petroleum gas - Google Patents
Method for modification by coupling hydrodesulfurization of FCC (Fluid Catalytic Cracking) gasoline and aromatization of liquefied petroleum gas Download PDFInfo
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Abstract
The invention provides a method for modification by coupling hydrodesulfurization of FCC (Fluid Catalytic Cracking) gasoline and aromatization of liquefied petroleum gas. All-fraction FCC gasoline is sequentially subjected to selective hydrogenation and preliminary desulfurization treatment to obtain HCN (Hydrogen Cyanide) heavy-component gasoline by fractionation, and the obtained HCN heavy-component gasoline is then subjected to hydrodesulfurization treatment; and the HCN heavy-component gasoline obtained from the hydrodesulfurization treatment and liquefied petroleum gas are co-fed into a fixed bed multi-stage aromatization reactor to recover/improve the octane number of a gasoline product through the processes of polymerization, pyrolysis, aromatization, hydrogen transfer and the like of olefin. The method is applied to the production process of ultra-low sulfur clean gasoline meeting national IV gasoline standard, and especially the ultra-low sulfur clean gasoline meeting national V gasoline standard. As a gradual desulfurization process is adopted, the operation conditions of all the units are mild, the desulfurization process is coupled with a liquefied petroleum gas aromatization process, and therefore the method has the characteristics that the gasoline desulfurization efficiency is high, the octane number loss of a product does not lose and is even increased, the gasoline yield is increased and the reaction process is flexible.
Description
Technical field
The invention belongs to the fuel for cleaning vehicle production technical field, specifically, relate to the method for a kind of FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modification.
Background technology
Along with China's rapid economy development, increasing for the demand of petroleum resources.The China's oil demand reached 4.55 hundred million tons in 2010, and wherein surplus crude oil and the processed oil import 2.5 hundred million tons, the shortage of petroleum resources has become the bottleneck of restriction China economy and society Sustainable development.And in coming few decades, the shortest in the oil derived product is automobile-used transport fuel, is mainly gasoline and diesel oil (contemporary petroleum and petrochemical industry, 2009 the 17th volume o. 11ths, the Thought of Countermeasures of China's oil refining and petrochemical industry Sustainable development).
Along with the growing interest to environmental issue, in recent years, various countries all have higher requirement to the quality standard of processed oil, particularly the restriction index of sulphur content are constantly upgraded.And being nearly 80% gasoline, the present situation of China's gasoline production comes catalytic cracking, its olefin(e) centent and sulphur content height (in the gasoline product＞95% sulphur from catalytically cracked gasoline), and aromaticity content lower (～20%).Alkene is bigger to the gasoline octane rating contribution in the FCC gasoline, for reaching state IV, Europe V standard clean gasoline, need further hydrogenating desulfurization to reduce sulfur in gasoline, olefin(e) centent, and the greatest problem that this process faces is that alkene is easily saturated for alkane by hydrogenation in deep desulfurization process, causes gasoline octane rating to descend significantly.Especially, China's local oil refining enterprise catalytic cracking intermingled dregs ratio height causes sulphur in the catalytic gasoline, olefin(e) centent height, and the gasoline cleaning difficulty is big.Traditional hydrofining technology is difficult to satisfy it and cleans the upgrading requirement.
In recent years, some catalytic gasoline selective hydrodesulfurization technology have been developed both at home and abroad, as the relevant gasoline hydrodesulfurizationmethod technology of Prime-G, Prime-GW and domestic R﹠D institution, but these technology exist in local oil refining enterprise high-sulfur, the hydrofining of high olefin catalytic gasoline are used that catalyst deactivation is fast, alkene saturation exponent height, deficiency that the gasoline octane rating loss is big.
The inventor is used for hydrodesulfurization process and has the advantages that desulfurization performance is good, alkene is saturated less, loss of octane number is low in advance at the method and the catalyzer thereof that have disclosed the FCC gasoline hydrodesulfurizationmethod in CN201110009189.7, CN200910028852.0, CN200810024072.4 etc.; The inventor has disclosed a kind of fixed bed multistage reactor for aromatizing reaction of olefin-containing liquefying gas and application at CN201010240719.4, can realize flexibly that the liquefied gas efficient catalytic is converted into vehicle fuel, and effectively control the reaction bed temperature rise.
The present invention is continuity and the expansion of foregoing invention, at existing FCC gasoline hydrodesulfurizationmethod technology be used for that high-sulfur, high olefin catalytic gasoline unifining process catalyst deactivation are fast, problems such as alkene saturation exponent height, gasoline octane rating loss are big, satisfy state IV, state V standard clean gasoline by heavy constituent gasoline after FCC gasoline hydrodesulfurizationmethod-hydrogenating desulfurization provided by the invention and the production of the co-fed aromizing combined process of liquefied gas, have reaction process flexibly, gasoline desulfur rate height, the product octane value does not lose in addition promote to some extent, characteristics that yield of gasoline increases.
Summary of the invention
The method that the purpose of this invention is to provide a kind of FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modification, specifically, the present invention by FCC gasoline hydrodesulfurizationmethod-hydrogenating desulfurization after the production of heavy constituent gasoline and liquefied gas coupling aromatization modification combined process satisfy state IV, Europe V standard clean gasoline, solve high-sulfur, high olefin FCC gasoline hydrofinishing process catalyst deactivation is fast, alkene saturation exponent height, problems such as gasoline octane rating loss is big, it is flexible to have a reaction process, gasoline desulfur rate height, the product octane value does not lose even promotes to some extent, the characteristics that yield of gasoline increases.
The invention provides the method for a kind of FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modification, cut FCC gasoline fractionates out the HCN heavy constituent again and carries out the hydrogenating desulfurization processing after handling through selective hydrogenation process and pre-sweetening process successively; HCN heavy constituent and liquefied gas after hydrogenating desulfurization is handled are co-fed, enter the fixed bed multistage aromatization reactor, the octane value of the polymerization by alkene, cracking, aromizing, hydrogen transference course recovery/lifting gasoline products.
The method of FCC gasoline hydrodesulfurizationmethod provided by the invention-liquefied gas through aromatization coupling modification, described full cut FCC gasoline selective hydrogenation process is to enter fixed bed selective hydrogenation device after full cut FCC gasoline mixes hydrogen, carries out the isomerization reaction of diolefine, cinnamic selective hydrogenation and removing and alpha-olefin.Described full cut FCC gasoline selective hydrogenation unit is the liquid-solid phase reaction, and operation condition is 120～200 ℃ of temperature, and pressure is 1.5～2.5MPa, reaction mass air speed 3.0～8.0h
-1, hydrogen to oil volume ratio 50～250.
The method of FCC gasoline hydrodesulfurizationmethod provided by the invention-liquefied gas through aromatization coupling modification, the pre-sweetening process of described full cut FCC gasoline is that the product of full cut FCC gasoline after selective hydrogenation enters the pre-desulphurization reactor of fixed bed hydrogenation, the low temperature that carries out small molecules mercaptan, thioether, thiophene, disulphide removes, and this process alkene saturation exponent is less than 5%.
The method of FCC gasoline hydrodesulfurizationmethod provided by the invention-liquefied gas through aromatization coupling modification, the pre-desulphurization reaction of described full cut FCC gasoline carries out at low temperatures, the operation condition temperature is 210～250 ℃, and reaction pressure is 1.5～2.5MPa, reaction mass air speed 4.0～10.0h
-1, the reaction hydrogen to oil volume ratio is 100～250.
The method of FCC gasoline hydrodesulfurizationmethod provided by the invention-liquefied gas through aromatization coupling modification, the pre-desulfurization product of described full cut FCC gasoline enters isolates oil phase and gas phase in the high pressure hot separator, gas phase is after overcooling, enter cold high pressure separator, isolated gas phase hydrogen-rich component recycles as hydrogen source after the recycle hydrogen de sulphuring treatment; Isolated oil phase enters separation column, isolates LCN light constituent and HCN heavy constituent, and the LCN light constituent carries out sending to the mediation unit as the clean gasoline blend component after depriving hydrogen sulphide is handled; The hydrogenating desulfurization processing is carried out in the HCN heavy constituent, and wherein organosulfurs such as mercaptan, thioether, thiophene and derivative thereof change into inorganic H
2S removes from gasoline, produces sulphur content less than 50ppm or low sulfur content clean gasoline more, has characteristics such as loss of octane number is few in long and steady, hydrogenation process running period, yield is high, the hydrogen consumption is low simultaneously.
The method of FCC gasoline hydrodesulfurizationmethod provided by the invention-liquefied gas through aromatization coupling modification, the isolated oil phase of described separation column and thermal high enter the fixed bed hydrogenation desulphurization reactor after mixing hydrogen, in the mode of hydrogenation organic sulfide are converted into inorganic H
2S removes, and makes the product total sulfur satisfy state IV, Europe V gasoline standard.
The method of FCC gasoline hydrodesulfurizationmethod provided by the invention-liquefied gas through aromatization coupling modification, described organic sulfide are one or more in mercaptan, thioether, thiophene or above-mentioned three's the derivative.
The method of FCC gasoline hydrodesulfurizationmethod provided by the invention-liquefied gas through aromatization coupling modification, when hydrogenating desulfurization was carried out in described HCN heavy constituent, small amounts of olefins was by saturated, and operation condition is 240～300 ℃ of temperature, reaction pressure is 1.5～2.5MPa, and the reaction mass air speed is 2.0～4.0h
-1, hydrogen to oil volume ratio is 200～500.
The method of FCC gasoline hydrodesulfurizationmethod provided by the invention-liquefied gas through aromatization coupling modification, HCN heavy constituent and a certain proportion of liquefied gas after the described hydrogenating desulfurization are co-fed, enter the fixed bed multistage aromatization reactor, recover/promote the octane value of gasoline products; To account for the ratio of HCN and liquefied gas combined feed total feed be 10-60% to the liquefied gas raw material in this process, and reaction conditions is temperature 280-450 ℃, pressure 0.5-2.0MPa, total feed weight air speed 0.6-2.0h
-1The reaction after product is through separating, and isolated liquid phase component mixes with refining back LCN component, obtains product gasoline; By-product high-quality motor liquified gas and dry gas simultaneously on a small quantity.
The method of FCC gasoline hydrodesulfurizationmethod provided by the invention-liquefied gas through aromatization coupling modification, described fixed bed multistage reactor progression is the 2-6 level; Each reaction bed catalyst loading pattern is equivalent filling or inequality filling, is preferably the multistage type of feed such as the not section of grade that increases step by step from top to bottom.
The method of FCC gasoline hydrodesulfurizationmethod provided by the invention-liquefied gas through aromatization coupling modification, described aromatized catalyst are DL0810 and/or the DL0811 catalyzer of Dalian Inst of Chemicophysics, Chinese Academy of Sciences's exploitation.
The present invention by FCC gasoline hydrodesulfurizationmethod-hydrogenating desulfurization after the production of heavy constituent gasoline and liquefied gas coupling aromatization modification combined process satisfy state IV, Europe V standard clean gasoline, problems such as solve that high-sulfur, high olefin FCC gasoline hydrofinishing process catalyst deactivation are fast, alkene saturation exponent height, gasoline octane rating loss are big, have reaction process flexibly, gasoline desulfur rate height, the product octane value does not lose in addition promote to some extent, characteristics that yield of gasoline increases.
Description of drawings
Fig. 1 is process schematic representation of the present invention; Wherein, each digitized representation title is as follows among the figure: 01 raw material surge tank, 02 feedstock pump, 03 selective hydrogenation device, 04 pre-desulphurization reactor, 05,10 high pressure hot separators, 06,11 cold high pressure separators, 07,19 separation columns, 08 heavy oil topping-up pump, 09 heavy oil hydrodesulfurization reactor, 12 circulating hydrogen compressors, 13 liquefied gas storages, 14 upgrading feedstock pumps, 15 process furnace, 16 reforming reactors, 17 stabilizer towers, 18 absorb desorption tower.
From the incoming stock surge tank 01 of the FCC gasoline of catalytic unit, after feedstock pump 02 boosted mixed hydrogen, heat exchange to temperature of reaction entered selective hydrogenation device 03, removes impurity such as diolefine.Reaction product is through being heated to pre-desulfurization reaction temperature, enter pre-desulphurization reactor 04, transform micromolecular organic sulfide, product enters high pressure hot separator 05 through heat exchange to certain temperature, isolating gas phase is cooled to below 40 ℃, enter cold high pressure separator 06, isolate gas phase and remove circulating hydrogen compressor 12 through the desulfurization processing, recycle after boosting, oil phase enters separation column 07, cat head is extracted LCN light constituent gasoline out and is gone to be in harmonious proportion the workshop, HCN heavy constituent gasoline is with after the high pressure hot separator oil phase mixes at the bottom of the tower, boosts with after hydrogen mixes through heavy oil topping-up pump 08, is heated to temperature of reaction, enter heavy oil hydrodesulfurization reactor 09, organic sulfide is converted into inorganic H
2S removes from gasoline, and reaction product is isolated gas phase through high pressure hot separator 10 earlier, through being cooled to below 55 ℃, enter cold high pressure separator 11, isolate the gas phase desulfurization after, use through recycle hydrogen press compression cycle, the hydrogen that reaction process consumes is replenished by new hydrogen.After isolating oil phase and oil phase in the high pressure hot separator 10 mixing, boost and mix from road liquefied gas in the liquefied gas storage 13 through upgrading feedstock pump 14, be heated to temperature of reaction through process furnace 15 and enter reforming reactor 16 from reactor head, 2～4 grades of entrances of other three routes reforming reactor that liquefied gas storage comes are introduced.Reaction product enters stabilizer tower 17, and overhead gas enters and absorbs desorption tower 18, and the sulfide hydrogen dry gas of desorb cat head enters the fuel pipe network, goes out the high-quality motor liquified gas at the bottom of the desorption tower.Oil phase at the bottom of the stabilizer tower enters separation column 19, and cat head extracts gasoline fraction out and the mediation of LCN light constituent gasoline obtains clean gasoline, goes out a spot of solar oil component at the bottom of the tower.
Embodiment
Following examples will give further instruction to the present invention, but not thereby limiting the invention.
FDJB-01/FDJB-02/FDJB-03, FDJY-01, trade mark protective material and catalyzer such as FDJY-02, FDJZ-05 that hydrofining segment protect of the present invention agent and catalyzer adopt Jiangsu good reputation letter company to produce.The main physical parameter of catalyzer and protective material sees 1.
The main physical parameter of table 1 catalyzer and protective material
Embodiment 1
Adopt method provided by the invention, be raw material with FCC gasoline in the table 21, earlier full cut FCC gasoline 1 being introduced the selective hydrogenation device reacts with pre-desulphurization reactor, diolefine in the raw material is reduced to below the 0.5v% from 1.5v%, total sulfur content is reduced to 745 μ g/g from 1250 μ g/g, alkene is saturated less than 3%, then pre-desulfurization product is entered separator-separation column machinery, be cut point with 75 ℃, with LCN: the HCN weight ratio is 40: 60, the LCN light constituent total sulfur that fractionates out is 45.5 μ g/g, and fractionating out HCN heavy constituent total sulfur is 1405.2 μ g/g, and HCN heavy constituent total sulfur after hydrogenating desulfurization is handled is reduced to 38.4 μ g/g, being in harmonious proportion afterwards with the LCN light constituent, total sulfur is 42.6 μ g/g, alkene is reduced to 31.2v% from 38.5v%, and RON is reduced to 90.9 from 92.5, and loss is 1.6 units.Corresponding operation condition and product relevant nature detailed data are listed in table 3.
Embodiment 2
Be raw material with FCC gasoline in the table 21, earlier full cut FCC gasoline 1 is introduced selective hydrogenation device and pre-desulphurization reactor, diolefine in the raw material is reduced to below the 0.5v% from 1.5v%, total sulfur content is reduced to 685 μ g/g from 1250 μ g/g, alkene is saturated less than 5%, then pre-desulfurization product is entered separator-separation column machinery, be cut point with 80 ℃, with LCN: the HCN weight ratio is 45: 55, the LCN light constituent total sulfur that fractionates out is 42.8 μ g/g, fractionating out HCN heavy constituent total sulfur is 1326.5 μ g/g, HCN heavy constituent total sulfur after hydrogenating desulfurization is handled is reduced to 44.5 μ g/g, and total sulfur is 43.9 μ g/g after being in harmonious proportion with the LCN light constituent, and alkene is reduced to 31.8v% from 38.5v%, RON is reduced to 91.0 from 92.5, and loss is 1.5 units.Operation condition and product relevant nature detailed data are listed in table 3.
Embodiment 3
Be raw material with FCC gasoline in the table 22, earlier full cut FCC gasoline 2 is introduced selective hydrogenation device and pre-desulphurization reactor, after treatment diene content in the full cut FCC gasoline 2 is reduced to 0.45v% from 1.2v%, total sulfur content is reduced to 281.4 μ g/g from 412 μ g/g, and the alkene saturation exponent is less than 3%.Then pre-desulfurization product is introduced separation-fractionation machinery, the selective rectification point is 75 ℃, fractionating out LCN light constituent mass ratio is 40%, and total sulfur content is 36.5 μ g/g, and fractionating out HCN heavy constituent mass ratio is 60%, total sulfur content is 539.4 μ g/g, total sulfur is reduced to 41.8 μ g/g behind heavy-oil hydrogenation, and producing sulphur content after being in harmonious proportion with the LCN light constituent then is 39.4 μ g/g, and olefin(e) centent is reduced to 34.5v% from 39.4v%, RON will bring to 90.6 from 91.2, lose 0.6 unit.Corresponding operation condition and product relevant nature detailed data are listed in table 3.
Embodiment 4
Be raw material with FCC gasoline 2, main character sees Table 2 analytical data, full cut FCC gasoline 2 is incorporated into selective hydrogenation and pre-desulphurization reactor, after treatment diene content in the full cut FCC gasoline 2 is reduced to 0.45v% from 1.2v%, total sulfur content is reduced to 247.5 μ g/g from 412 μ g/g, and the alkene saturation exponent is less than 5%.Then pre-desulfurization product is introduced separation-fractionation machinery, the selective rectification point is 70 ℃, fractionating out LCN light constituent mass ratio is 35%, and total sulfur content is 9.0 μ g/g, and fractionating out HCN heavy constituent mass ratio is 65%, total sulfur content is 473.5 μ g/g, total sulfur is reduced to 8.4 μ g/g behind heavy-oil hydrogenation, and producing sulphur content after being in harmonious proportion with the LCN light constituent then is 8.6 μ g/g, and olefin(e) centent is reduced to 32.2v% from 39.4v%, RON is reduced to 90.0 from 91.2, loses 1.2 units.Corresponding operation condition and product relevant nature detailed data are listed in table 3.
Table 2FCC gasoline stocks character
| Project | FCC gasoline 1 | FCC gasoline 2 |
| Mi Du @20 ℃, kg/m 3 | 718 | 720 |
| Sulphur content, μ g/g | 1250 | 412 |
| Diene content, v% | 1.5 | 1.2 |
| Olefin(e) centent, v% | 38.5 | 39.4 |
| Boiling range/℃, ASTMD86 | ||
| IBP | 40 | 38 |
| 10％ | 55 | 53 |
| 30％ | 69 | 65 |
| 50％ | 95 | 88 |
| 70％ | 121 | 117 |
| 90％ | 159 | 167 |
| FBP | 183 | 189 |
| RON | 92.5 | 91.2 |
Table 3 embodiment 1～4 operating parameters and product main character
| Project | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 |
| Operating parameters | ||||
| One anti-temperature in, ℃ | 165 | 165 | 165 | 170 |
| Two anti-temperature ins, ℃ | 235 | 240 | 225 | 236 |
| Three anti-temperature ins, ℃ | 265 | 262 | 257 | 268 |
| One anti-air speed, h -1 | 5.0 | 5.0 | 6.0 | 6.0 |
| Two anti-air speeds, h -1 | 6.0 | 6.0 | 7.0 | 7.0 |
| Three anti-air speeds, h -1 | 3.0 | 3.0 | 3.0 | 2.5 |
| One or two counterpressures, MPa | 2.2 | 2.2 | 2.0 | 2.0 |
| Three reaction pressures, MPa | 1.8 | 1.8 | 1.8 | 2.0 |
| One or two antihydrogen oil volume ratios | 150 | 150 | 120 | 120 |
| Three antihydrogen oil volume ratios | 350 | 400 | 300 | 350 |
| Product property | ||||
| Mi Du @20 ℃, kg/m 3 | 718 | 719 | 720 | 721 |
| Total sulfur, μ g/g | 42.6 | 43.9 | 39.4 | 8.6 |
| Alkene, v% | 31.2 | 31.8 | 34.5 | 32.2 |
| RON | 90.9 | 91.0 | 90.6 | 90.0 |
| Boiling range/℃, | ||||
| IBP | 40 | 39 | 39 | 39 |
| 10％ | 56 | 54 | 53 | 54 |
| 30％ | 70 | 69 | 65 | 65 |
| 50％ | 95 | 96 | 88 | 88 |
| 70％ | 121 | 121 | 117 | 117 |
| 90％ | 159 | 159 | 167 | 167 |
| FBP | 183 | 182 | 189 | 189 |
Embodiment 5
The FCC gasoline stocks is identical with embodiment 2 with hydrodesulfurization process, difference is, isolated HCN heavy constituent mix with a part of liquefied gas raw material after embodiment 2 hydrogenating desulfurizations, enter reactor from fixed bed multistage aromatization reactor top, the remaining fluid gasification is divided into 3 the tunnel and enters the 2-4 stage reactor, and each section of reactor liquefied gas charge proportion is 1: 2: 3: 4; Catalyzer is the DL0810 catalyzer, and each section of catalyzer filling ratio is 2: 1.5: 2.5: 4.The liquefied gas raw material accounts for 50% of HCN and liquefied gas combined feed total feed quality, and shown in the liquefied gas table composed as follows, wherein C 4 olefin content is 45% in the raw material; Reaction conditions is temperature 290-340 ℃, 1.0MPa, combined feed total feed air speed 1.5h
-1
Table 4 embodiment 5 liquefied gas raw materials are formed
The reaction after product is through separating, and isolated liquid phase component mixes with refining back LCN component, obtains product gasoline; By-product high-quality motor liquified gas and dry gas simultaneously on a small quantity.
Behind isolated HCN heavy constituent after the hydrogenating desulfurization and the co-fed aromatization modification of liquefied gas, HCN component sulphur content further is reduced to 35.5 μ g/g from 44.5 μ g/g, and octane value is compared with HCN component after the hydrogenating desulfurization, and RON increases by 3.5 units.Aromatization reaction products obtains gasoline products after gasoline component that separation obtains and the blending of LCN light constituent.Gasoline products is compared with raw material, and sulphur content is reduced to 38.8 μ g/g from 1250 μ g/g; Octane value does not have loss, and increases by 0.8 unit than raw material; The gasoline products yield increases by 19.8%.
Embodiment 6
The FCC gasoline stocks is identical with embodiment 4 with hydrodesulfurization process, difference is that isolated HCN heavy constituent mix with a part of liquefied gas raw material after the hydrogenating desulfurization, enter reactor from fixed bed multistage aromatization reactor top, the remaining fluid gasification is divided into 3 the tunnel and enters the 2-4 stage reactor, and each section of reactor liquefied gas charge proportion is 1: 2: 3: 4; Catalyzer is the DL0811 catalyzer, and each section of catalyzer filling ratio is 2: 1.5: 2.5: 4.The liquefied gas raw material accounts for 30% of HCN and liquefied gas total feed, and liquefied gas is formed identical with example 5.
Behind isolated HCN heavy constituent after the hydrogenating desulfurization and the co-fed aromatization modification of liquefied gas, gasoline HCN product sulphur content further is reduced to 6.3 μ g/g from 8.4 μ g/g, and RON increases by 2.8 units behind the HCN component behind the hydrogenation and the liquefied gas through aromatization upgrading; Compare with the FCC gasoline stocks with the product after the LCN blending, sulphur content is reduced to 7.8 μ g/g from 412 μ g/g, and octane value does not have loss, and increases by 0.3 unit.
Claims (12)
1. the method for FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modification is characterized in that: after cut FCC gasoline is handled through selective hydrogenation process and pre-sweetening process successively entirely, fractionate out the HCN heavy constituent again and carry out the hydrogenating desulfurization processing; HCN heavy constituent and liquefied gas after hydrogenating desulfurization is handled are co-fed, enter the fixed bed multistage aromatization reactor, the octane value of the polymerization by alkene, cracking, aromizing, hydrogen transference course recovery/lifting gasoline products.
2. according to the method for the described FCC gasoline hydrodesulfurizationmethod of claim 1-liquefied gas through aromatization coupling modification, it is characterized in that: described full cut FCC gasoline selective hydrogenation process is to enter fixed bed selective hydrogenation device after full cut FCC gasoline mixes hydrogen, carries out the isomerization reaction of diolefine, cinnamic selective hydrogenation and removing and alpha-olefin.
3. according to the method for claims 1 and 2 described FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modifications, it is characterized in that: described full cut FCC gasoline selective hydrogenation unit is the liquid-solid phase reaction, operation condition is 120～200 ℃ of temperature, pressure is 1.5～2.5MPa, reaction mass air speed 3.0～8.0h
-1, hydrogen to oil volume ratio 50～250.
4. according to the method for claims 1 described FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modification, it is characterized in that: the pre-sweetening process of described full cut FCC gasoline is that the product of full cut FCC gasoline after selective hydrogenation enters the pre-desulphurization reactor of fixed bed hydrogenation, the low temperature that carries out small molecules mercaptan, thioether, thiophene, disulphide removes, and this process alkene saturation exponent is less than 5%.
5. according to the method for claims 1 and 4 described FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modifications, it is characterized in that: the pre-desulphurization reaction of described full cut FCC gasoline carries out at low temperatures, the operation condition temperature is 210～250 ℃, reaction pressure is 1.5～2.5MPa, reaction mass air speed 4.0～10.0h
-1, the reaction hydrogen to oil volume ratio is 100～250.
6. according to the method for claims 1 described FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modification, it is characterized in that: the pre-desulfurization product of described full cut FCC gasoline enters isolates oil phase and gas phase in the high pressure hot separator, gas phase is gone into cold high pressure separator through overcooling is laggard, and isolated gas phase hydrogen-rich component recycles as hydrogen source after the recycle hydrogen de sulphuring treatment; Isolated oil phase enters separation column, isolates LCN light constituent and HCN heavy constituent, and the LCN light constituent carries out depriving hydrogen sulphide and handles the back as the clean gasoline blend component, and the HCN heavy constituent are carried out hydrogenating desulfurization and handled.
7. according to the method for claim 1 and 6 described FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modifications, it is characterized in that: described HCN heavy constituent enter the fixed bed hydrogenation desulphurization reactor after mixing hydrogen, in the mode of hydrogenation the organic sulfide in the HCN heavy constituent is converted into inorganic H2S and removes, make the product total sulfur satisfy state IV, Europe V gasoline standard.
8. according to the method for claim 1 and 6 described FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modifications, it is characterized in that: when hydrogenating desulfurization is carried out in described HCN heavy constituent, small amounts of olefins is by saturated, operation condition is 240～300 ℃ of temperature, reaction pressure is 1.5～2.5MPa, and the reaction mass air speed is 2.0～4.0h
-1, hydrogen to oil volume ratio is 200～500.
9. according to the method for the described FCC gasoline hydrodesulfurizationmethod of claim 1-liquefied gas through aromatization coupling modification, it is characterized in that: HCN heavy constituent and a certain proportion of liquefied gas after the described hydrogenating desulfurization are co-fed, enter the fixed bed multistage aromatization reactor, recover/promote the octane value of gasoline products; To account for the ratio of HCN and liquefied gas combined feed total feed be 10-60% to the liquefied gas raw material in this process, and reaction conditions is temperature 280-450 ℃, pressure 0.5-2.0MPa, total feed weight air speed 0.6-2.0h
-1The reaction after product is through separating, and isolated liquid phase component mixes with refining back LCN component, obtains product gasoline; By-product high-quality motor liquified gas and dry gas simultaneously on a small quantity.
10. according to the method for claim 1 and 10 described FCC gasoline hydrodesulfurizationmethod-liquefied gas through aromatization coupling modifications, it is characterized in that: described fixed bed multistage reactor progression is the 2-6 level; Each reaction bed catalyst loading pattern is equivalent filling or inequality filling.
11. the method according to the described FCC gasoline hydrodesulfurizationmethod of claim 11-liquefied gas through aromatization coupling modification is characterized in that: multistage not the wait section type of feed of each reaction bed catalyst loading pattern of described fixed bed multistage reactor for increasing step by step from top to bottom.
12. the method according to the described FCC gasoline hydrodesulfurizationmethod of claim 1-liquefied gas through aromatization coupling modification is characterized in that: described aromatized catalyst is DL0810 and/or the DL0811 catalyzer of Dalian Inst of Chemicophysics, Chinese Academy of Sciences's exploitation.
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