CN106753524A - A kind of gasoline hydrogenation technique - Google Patents
A kind of gasoline hydrogenation technique Download PDFInfo
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- CN106753524A CN106753524A CN201611020387.2A CN201611020387A CN106753524A CN 106753524 A CN106753524 A CN 106753524A CN 201611020387 A CN201611020387 A CN 201611020387A CN 106753524 A CN106753524 A CN 106753524A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of gasoline hydrogenation technique, it is comprised the following steps：（1）Hydrogenation reaction is carried out into hydrogenation of total effluent reactor after gasoline stocks and hydrogen mixing, hydrogenation of total effluent product isolates light petrol, hydrogasoline into hydrogenation of total effluent stabilizer；（2）Hydrogasoline is fractionated into prefractionator, fractionates out middle gasoline, heavy petrol；（3）After heavy petrol and hydrogen mixing hydrogenation reaction generation one-stage hydrogenation product is carried out into one-stage hydrogenation device；（4）One-stage hydrogenation product generates one section of high score oil after entering one section of desulfurizer desulfurization；（5）One section of high score is oily, middle gasoline and hydrogen are mixed into secondary hydrogenation device and carry out hydrogenation reaction generation secondary hydrogenation product；（6）Secondary hydrogenation product enters the cold high score oil of two sections of generation after two sections of desulfurizer desulfurization, and the refined generation treated gasoline of product stabilizer is entered after two sections of cold high score oil, and gasoline product is formed after treated gasoline and light petrol mixing.
Description
Technical field
The present invention relates to a kind of gasoline hydrogenation technique.
Background technology
In April, 2015, country《Accelerate product oil quality upgrading programme of work》Notify to put into effect, scheme was determined from 2017
The automobile-used petrol and diesel oil products of the comprehensive supply country V in the whole nation, 11 supply country of the provinces and cities V in east China area from January, 2016 from January 1
Automobile-used petrol and diesel oil product (sulfur content is not more than 10ppm).According to the requirement in quality upgrading time limit, petro-chemical corporation need to be to existing vapour
Oily hydrogenation plant carries out upgrading.Existing device is adopted the technology that carries out hydrogenation of total effluent first, then enters stabilizer
Infinite reflux, then enter fractionating column and be fractionated, fractionating column ejection light petrol, Fractionator Bottom goes out heavy petrol, and bottom of towe heavy petrol enters hydrogenation
Converge device with light petrol after reactor hydrogenation.Current device reaches 10ppm for improve product quality reduction sulfur content, carries
Reaction depth high, it is necessary to which drop amount is produced, and loss of octane number reaches 3.5 or so than larger.
The content of the invention
The technical problem to be solved in the present invention is to provide a kind of vapour that product sulfur content is reduced in the case of ensureing octane number
Oily hydrogenation technique.
In order to solve the above technical problems, gasoline hydrogenation technique of the present invention, it is comprised the following steps：
（1）Hydrogenation of total effluent reacts：Gasoline stocks add after mixing, be warming up to 160~200 DEG C with the hydrogen of excess into full cut
Hydrogen reactor carries out hydrogenation reaction under the conditions of the MPa of pressure 2.6~2.8, and hydrogenation of total effluent product is from hydrogenation of total effluent reactor
Enter hydrogenation of total effluent stabilizer after bottom of towe outflow, reacted under the conditions of the MPa of pressure 0.6~0.65, from hydrogenation of total effluent stabilization
Tower side line isolates light petrol, bottom of towe and isolates hydrogasoline, and it is 90~95 DEG C that wherein side line light petrol extracts temperature out；
（2）Prefractionator is fractionated：Temperature be 165~175 DEG C hydrogasoline into prefractionator be fractionated, pressure 0.24~
It is fractionated under the conditions of 0.29 MPa, prefractionator tower top fractionates out middle gasoline, and the temperature of tower top is 148~150 DEG C, bottom of towe point
Heavy petrol is distillated, the temperature of bottom of towe is 220~224 DEG C；
（3）One-stage hydrogenation reacts：Heavy petrol and hydrogen mixing enter one-stage hydrogenation device in pressure after being warming up to 270~275 DEG C
Hydrogenation reaction generation one-stage hydrogenation product is carried out under the conditions of 2.0~2.17MPa；
（4）One section of desulphurization reaction：One-stage hydrogenation product generates one section of high score oil after entering one section of desulfurizer desulfurization；
（5）Secondary hydrogenation reacts：One section of oily and middle gasoline of high score mixes and heats up after being mixed to form heavy petrol mixture with hydrogen
Hydrogenation reaction generation secondary hydrogenation is carried out under the conditions of 2.0~2.2MPa of pressure into secondary hydrogenation device after to 265~270 DEG C
Product；
（6）Two sections of desulphurization reactions：Secondary hydrogenation product enters the cold high score oil of two sections of generation after two sections of desulfurizer desulfurization, and temperature is
155~165 DEG C, enter the refined generation treated gasoline of product stabilizer after two that pressure is 0.7~0.78MPa section cold high score oil,
The product stabilizer column bottom temperature is 209~211 DEG C, and gasoline product is formed after treated gasoline and light petrol mixing.
Middle gasoline component contains about 45% alkene, and heavy gasoline components contain about 17% alkene, in middle gasoline component sulphur into
Divide predominantly small molecule mercaptan sulfur and thiophene, and sulphur composition is mainly the mercaptan sulfur of macromolecular and is taken with methyl in heavy gasoline components
For the intractable thiophene that dibenzothiophenes is representative.Heavy gasoline components need deep hydrogenation to remove sulfide, if middle gasoline
Component and heavy gasoline components are hydrogenated with together, will increase alkene saturation factor, lose octane number, so the present invention is by hydrogenation of total effluent
Raw material afterwards is divided into light petrol component, middle gasoline component and heavy gasoline components, with middle gasoline group after heavy gasoline components are first hydrogenated with
Divide and be further hydrogenated with after converging, realize reducing the sulfur content in product, the purpose of octane number is kept again.
Heavy petrol and hydrogen mixing are warming up to after 270~275 DEG C two grades of one-stage hydrogenation for initially entering one-stage hydrogenation device
Reactor carries out a hydrogenation reaction under the conditions of 2.12~2.17MPa of pressure, and a product for hydrogenation reaction enters one section and adds
The one-stage hydrogenation first-stage reactor of hydrogen production device temperature be 270~275 DEG C, pressure be 2.12~2.17MPa under conditions of carry out
Secondary hydrogenation reaction generates one-stage hydrogenation product.
Temperature is 195~205 DEG C, one section of high score oil entrance stripper stripping of 0.7~0.75MPa of pressure, is refined
One section of high score oil, one section of refined high score is oily to be mixed with middle gasoline, wherein the temperature of the stripped vapor of stripper be 245~
255 DEG C, pressure be 0.9~1.1MPa.
The oily and middle gasoline mixing of one section of refined high score is warming up to and secondary hydrogenation device is initially entered after 265~270 DEG C
Hydrogenation reactor carries out a hydrogenation reaction under the conditions of 2.0~2.2MPa of pressure, and one time the product of hydrogenation reaction enters two sections
The finishing reactor of hydrogenation plant carries out desulphurization reaction generation two under the conditions of 320~330 DEG C of temperature, 1.9~1.96MPa of pressure
Section hydrogenation products.One section of oily and middle gasoline of high score is fully hydrogenated with hydrogenation reactor, but hydrogen sulfide and alkene in hydrogenation process
Hydrocarbon can form mercaptan, in hydrogenation reactor generate product enter finishing reactor, under hot conditions by mercaptan decomposition be alkene
And hydrogen sulfide, hydrogen sulfide is with product into two sections of desulfurizers removings.The setting of finishing reactor can reduce containing for sulphur in product
Amount, improves the quality of finished product.
Specific embodiment
Embodiment 1
Gasoline hydrogenation technique is comprised the following steps：（1）Hydrogenation of total effluent reacts：The hydrogen mixing of gasoline stocks and excess, intensification
Carry out hydrogenation reaction under the conditions of the MPa of pressure 2.6 into hydrogenation of total effluent reactor after to 160 DEG C, hydrogenation of total effluent product from
It is hydrogenated with the conditions of pressure 0.6MPa into hydrogenation of total effluent stabilizer after the outflow of hydrogenation of total effluent reactor column bottom, wherein entering
The temperature of the hydrogenation of total effluent product of hydrogenation of total effluent stabilizer is 144 DEG C, and hydrogenation of total effluent stabilizer column bottom temperature is 198
DEG C, tower top temperature be 76 DEG C, isolate light petrol, bottom of towe from hydrogenation of total effluent stabilizer side line and isolate hydrogasoline, wherein
Lateral line withdrawal function temperature is 90 DEG C；
（2）Prefractionator is fractionated：Temperature is that 175 DEG C of hydrogasolines enter into prefractionator under conditions of pressure is 0.24 MPa
Row fractionation, prefractionator tower top fractionates out middle gasoline, and the temperature of tower top is 148 DEG C, and bottom of towe fractionates out heavy petrol, the temperature of bottom of towe
It is 220 DEG C；
（3）One-stage hydrogenation reacts：Heavy petrol and hydrogen mixing be warming up to after 270 DEG C initially enter one section of one-stage hydrogenation device plus
Hydrogen second reactor carries out a hydrogenation reaction under the conditions of pressure 2.12MPa, and a product for hydrogenation reaction enters one section and adds
The one-stage hydrogenation first-stage reactor of hydrogen production device temperature be 271 DEG C, pressure be 2.13MPa under the conditions of carry out secondary hydrogenation reaction life
Into one-stage hydrogenation product；
（4）One section of desulphurization reaction：One-stage hydrogenation product generates one section of high score oil after entering one section of desulfurizer desulfurization, and temperature is
195 DEG C, one section of high score of pressure 0.7MPa oil enter stripper stripping, obtain one section of refined high score oil, wherein stripper
The temperature of stripped vapor is 245 DEG C, pressure is 0.9MPa；
（5）Secondary hydrogenation reacts：The oily and middle gasoline mixing of one section of refined high score initially enters secondary hydrogenation after being warming up to 265 DEG C
The hydrogenation reactor of device carries out a hydrogenation reaction under the conditions of pressure 2.0MPa, and one time the product of hydrogenation reaction enters two sections
The finishing reactor of hydrogenation plant carries out desulphurization reaction generation secondary hydrogenation product under the conditions of 320 DEG C of temperature, pressure 1.9MPa；
（6）Two sections of desulphurization reactions：Secondary hydrogenation product enters the cold high score oil of two sections of generation after two sections of desulfurizer desulfurization, and temperature is
155 DEG C, pressure is after two sections of 0.7MPa cold high scores oil to enter the refined generation treated gasoline of product stabilizer, product stabilizer tower
Bottom temperature is 209 DEG C, and gasoline product is formed after treated gasoline and light petrol mixing.
Embodiment 2
Gasoline hydrogenation technique is comprised the following steps：（1）Hydrogenation of total effluent reacts：The hydrogen mixing of gasoline stocks and excess, intensification
Carry out hydrogenation reaction under the conditions of the MPa of pressure 2.7 into hydrogenation of total effluent reactor after to 170 DEG C, hydrogenation of total effluent product from
It is hydrogenated with the conditions of pressure 0.62MPa into hydrogenation of total effluent stabilizer after the outflow of hydrogenation of total effluent reactor column bottom, wherein entering
The temperature for entering the hydrogenation of total effluent product of hydrogenation of total effluent stabilizer is 148 DEG C, and hydrogenation of total effluent stabilizer column bottom temperature is 198
DEG C, tower top temperature be 76 DEG C, isolate light petrol, bottom of towe from hydrogenation of total effluent stabilizer side line and isolate hydrogasoline, wherein
Lateral line withdrawal function temperature is 92 DEG C；
（2）Prefractionator is fractionated：Temperature is that 173 DEG C of hydrogasolines enter into prefractionator under conditions of pressure is 0.26 MPa
Row fractionation, prefractionator tower top fractionates out middle gasoline, and the temperature of tower top is 149 DEG C, and bottom of towe fractionates out heavy petrol, the temperature of bottom of towe
It is 222 DEG C；
（3）One-stage hydrogenation reacts：Heavy petrol and hydrogen mixing be warming up to after 271 DEG C initially enter one section of one-stage hydrogenation device plus
Hydrogen second reactor carries out a hydrogenation reaction under the conditions of pressure 2.14MPa, and a product for hydrogenation reaction enters one section and adds
The one-stage hydrogenation first-stage reactor of hydrogen production device temperature be 272 DEG C, pressure be 2.16MPa under the conditions of carry out secondary hydrogenation reaction life
Into one-stage hydrogenation product；
（4）One section of desulphurization reaction：One-stage hydrogenation product generates one section of high score oil after entering one section of desulfurizer desulfurization, and temperature is
198 DEG C, one section of high score of pressure 0.72MPa oil enter stripper stripping, obtain one section of refined high score oil, wherein stripper
The temperature of stripped vapor is 249 DEG C, pressure is 0.94MPa；
（5）Secondary hydrogenation reacts：The oily and middle gasoline mixing of one section of refined high score initially enters secondary hydrogenation after being warming up to 266 DEG C
The hydrogenation reactor of device carries out a hydrogenation reaction under the conditions of pressure 2.1MPa, and one time the product of hydrogenation reaction enters two sections
The finishing reactor of hydrogenation plant carries out desulphurization reaction generation secondary hydrogenation under the conditions of 325 DEG C of temperature, pressure 1.92MPa and produces
Thing；
（6）Two sections of desulphurization reactions：Secondary hydrogenation product enters the cold high score oil of two sections of generation after two sections of desulfurizer desulfurization, and temperature is
159 DEG C, pressure is after two sections of 0.73MPa cold high scores oil to enter the refined generation treated gasoline of product stabilizer, product stabilizer
Column bottom temperature is 210 DEG C, and gasoline product is formed after treated gasoline and light petrol mixing.
Embodiment 3
Gasoline hydrogenation technique is comprised the following steps：（1）Hydrogenation of total effluent reacts：The hydrogen mixing of gasoline stocks and excess, intensification
Hydrogenation reaction, hydrogenation of total effluent product are carried out under the conditions of the MPa of pressure 2.69 into hydrogenation of total effluent reactor after to 180 DEG C
It is hydrogenated with the conditions of pressure 0.6MPa into hydrogenation of total effluent stabilizer from after the outflow of hydrogenation of total effluent reactor column bottom, wherein entering
The temperature for entering the hydrogenation of total effluent product of hydrogenation of total effluent stabilizer is 150 DEG C, and hydrogenation of total effluent stabilizer column bottom temperature is 199
DEG C, tower top temperature be 77 DEG C, isolate light petrol, bottom of towe from hydrogenation of total effluent stabilizer side line and isolate hydrogasoline, wherein
Lateral line withdrawal function temperature is 94 DEG C；
（2）Prefractionator is fractionated：Temperature is that 170 DEG C of hydrogasolines enter into prefractionator under conditions of pressure is 0.28 MPa
Row fractionation, prefractionator tower top fractionates out middle gasoline, and the temperature of tower top is 148 DEG C, and bottom of towe fractionates out heavy petrol, the temperature of bottom of towe
It is 223 DEG C；
（3）One-stage hydrogenation reacts：Heavy petrol and hydrogen mixing be warming up to after 273 DEG C initially enter one section of one-stage hydrogenation device plus
Hydrogen second reactor carries out a hydrogenation reaction under the conditions of pressure 2.15MPa, and a product for hydrogenation reaction enters one section and adds
The one-stage hydrogenation first-stage reactor of hydrogen production device temperature be 274 DEG C, pressure be 2.14MPa under the conditions of carry out secondary hydrogenation reaction life
Into one-stage hydrogenation product；
（4）One section of desulphurization reaction：One-stage hydrogenation product generates one section of high score oil after entering one section of desulfurizer desulfurization, and temperature is
200 DEG C, one section of high score of pressure 0.73MPa oil enter stripper stripping, obtain one section of refined high score oil, wherein stripper
The temperature of stripped vapor is 250 DEG C, pressure is 0.98MPa；
（5）Secondary hydrogenation reacts：The oily and middle gasoline mixing of one section of refined high score initially enters secondary hydrogenation after being warming up to 268 DEG C
The hydrogenation reactor of device carries out a hydrogenation reaction under the conditions of pressure 2.13MPa, and the product of a hydrogenation reaction enters two
The finishing reactor of section hydrogenation plant carries out desulphurization reaction generation secondary hydrogenation under the conditions of 327 DEG C of temperature, pressure 1.92MPa and produces
Thing；
（6）Two sections of desulphurization reactions：Secondary hydrogenation product enters the cold high score oil of two sections of generation after two sections of desulfurizer desulfurization, and temperature is
160 DEG C, pressure is after two sections of 0.74MPa cold high scores oil to enter the refined generation treated gasoline of product stabilizer, product stabilizer
Column bottom temperature is 210 DEG C, and gasoline product is formed after treated gasoline and light petrol mixing.
Embodiment 4
Gasoline hydrogenation technique is comprised the following steps：（1）Hydrogenation of total effluent reacts：The hydrogen mixing of gasoline stocks and excess, intensification
Hydrogenation reaction, hydrogenation of total effluent product are carried out under the conditions of the MPa of pressure 2.75 into hydrogenation of total effluent reactor after to 190 DEG C
It is hydrogenated with the conditions of pressure 0.64MPa into hydrogenation of total effluent stabilizer from after the outflow of hydrogenation of total effluent reactor column bottom, wherein
Temperature into the hydrogenation of total effluent product of hydrogenation of total effluent stabilizer is 153 DEG C, and hydrogenation of total effluent stabilizer column bottom temperature is
198 DEG C, tower top temperature be 76 DEG C, isolate light petrol, bottom of towe from hydrogenation of total effluent stabilizer side line and isolate hydrogasoline, its
Middle lateral line withdrawal function temperature is 94 DEG C；
（2）Prefractionator is fractionated：Temperature is that 167 DEG C of hydrogasolines enter into prefractionator under conditions of pressure is 0.28 MPa
Row fractionation, prefractionator tower top fractionates out middle gasoline, and the temperature of tower top is 149 DEG C, and bottom of towe fractionates out heavy petrol, the temperature of bottom of towe
It is 223 DEG C；
（3）One-stage hydrogenation reacts：Heavy petrol and hydrogen mixing be warming up to after 274 DEG C initially enter one section of one-stage hydrogenation device plus
Hydrogen second reactor carries out a hydrogenation reaction under the conditions of pressure 2.16MPa, and a product for hydrogenation reaction enters one section and adds
The one-stage hydrogenation first-stage reactor of hydrogen production device temperature be 273 DEG C, pressure be 2.16MPa under the conditions of carry out secondary hydrogenation reaction life
Into one-stage hydrogenation product；
（4）One section of desulphurization reaction：One-stage hydrogenation product generates one section of high score oil after entering one section of desulfurizer desulfurization, and temperature is
203 DEG C, one section of high score of pressure 0.74MPa oil enter stripper stripping, obtain one section of refined high score oil, wherein stripper
The temperature of stripped vapor is 253 DEG C, pressure is 1.0MPa；
（5）Secondary hydrogenation reacts：The oily and middle gasoline mixing of one section of refined high score initially enters secondary hydrogenation after being warming up to 273 DEG C
The hydrogenation reactor of device carries out a hydrogenation reaction under the conditions of pressure 2.15MPa, and the product of a hydrogenation reaction enters two
The finishing reactor of section hydrogenation plant carries out desulphurization reaction generation secondary hydrogenation under the conditions of 329 DEG C of temperature, pressure 1.95MPa and produces
Thing；
（6）Two sections of desulphurization reactions：Secondary hydrogenation product enters the cold high score oil of two sections of generation after two sections of desulfurizer desulfurization, and temperature is
163 DEG C, pressure is after two sections of 0.77MPa cold high scores oil to enter the refined generation treated gasoline of product stabilizer, product stabilizer
Column bottom temperature is 210 DEG C, and gasoline product is formed after treated gasoline and light petrol mixing.
Embodiment 5
Gasoline hydrogenation technique is comprised the following steps：（1）Hydrogenation of total effluent reacts：The hydrogen mixing of gasoline stocks and excess, intensification
Carry out hydrogenation reaction under the conditions of the MPa of pressure 2.8 into hydrogenation of total effluent reactor after to 200 DEG C, hydrogenation of total effluent product from
It is hydrogenated with the conditions of pressure 0.65MPa into hydrogenation of total effluent stabilizer after the outflow of hydrogenation of total effluent reactor column bottom, wherein entering
The temperature for entering the hydrogenation of total effluent product of hydrogenation of total effluent stabilizer is 155 DEG C, and hydrogenation of total effluent stabilizer column bottom temperature is 198
DEG C, tower top temperature be 77 DEG C, isolate light petrol, bottom of towe from hydrogenation of total effluent stabilizer side line and isolate hydrogasoline, wherein
Lateral line withdrawal function temperature is 95 DEG C；
（2）Prefractionator is fractionated：Temperature is that 165 DEG C of hydrogasolines enter into prefractionator under conditions of pressure is 0.29MPa
Row fractionation, prefractionator tower top fractionates out middle gasoline, and the temperature of tower top is 150 DEG C, and bottom of towe fractionates out heavy petrol, the temperature of bottom of towe
It is 224 DEG C；
（3）One-stage hydrogenation reacts：Heavy petrol and hydrogen mixing be warming up to after 275 DEG C initially enter one section of one-stage hydrogenation device plus
Hydrogen second reactor carries out a hydrogenation reaction under the conditions of pressure 2.17MPa, and a product for hydrogenation reaction enters one section and adds
The one-stage hydrogenation first-stage reactor of hydrogen production device temperature be 275 DEG C, pressure be 2.17MPa under the conditions of carry out secondary hydrogenation reaction life
Into one-stage hydrogenation product；
（4）One section of desulphurization reaction：One-stage hydrogenation product generates one section of high score oil after entering one section of desulfurizer desulfurization, and temperature is
205 DEG C, one section of high score of pressure 0.75MPa oil enter stripper stripping, obtain one section of refined high score oil, wherein stripper
The temperature of stripped vapor is 255 DEG C, pressure is 1.1MPa；
（5）Secondary hydrogenation reacts：The oily and middle gasoline mixing of one section of refined high score initially enters secondary hydrogenation after being warming up to 270 DEG C
The hydrogenation reactor of device carries out a hydrogenation reaction under the conditions of pressure 2.2MPa, and one time the product of hydrogenation reaction enters two sections
The finishing reactor of hydrogenation plant carries out desulphurization reaction generation secondary hydrogenation under the conditions of 330 DEG C of temperature, pressure 1.96MPa and produces
Thing；
（6）Two sections of desulphurization reactions：Secondary hydrogenation product enters the cold high score oil of two sections of generation after two sections of desulfurizer desulfurization, and temperature is
165 DEG C, pressure is after two sections of 0.78MPa cold high scores oil to enter the refined generation treated gasoline of product stabilizer, product stabilizer
Column bottom temperature is 211 DEG C, and gasoline product is formed after treated gasoline and light petrol mixing.
With same gasoline stocks（Wherein sulfur content is 1200 ppm, and octane number is 91）By the finished product that existing process is produced
Quality of gasoline index contrasts as follows with the quality index of the gasoline product of the technique productions in the present invention：
| Sulfur content（ppm） | Octane number | Alkene saturation factor | |
| By the gasoline product that existing process is produced | 10 | 86.5 | 11 |
| Embodiment 1 | 10 | 89 | 6.5 |
| Embodiment 2 | 10 | 88.6 | 6.8 |
| Embodiment 3 | 10 | 88.5 | 7 |
| Embodiment 4 | 10 | 88.3 | 7.5 |
| Embodiment 5 | 10 | 88.0 | 7.8 |
Claims (4)
1. a kind of gasoline hydrogenation technique, it is characterised in that comprise the following steps：
（1）Hydrogenation of total effluent reacts：Gasoline stocks add after mixing, be warming up to 160~200 DEG C with the hydrogen of excess into full cut
Hydrogen reactor carries out hydrogenation reaction under the conditions of the MPa of pressure 2.6~2.8, and hydrogenation of total effluent product is from hydrogenation of total effluent reactor
Enter hydrogenation of total effluent stabilizer after bottom of towe outflow, reacted under the conditions of the MPa of pressure 0.6~0.65, from hydrogenation of total effluent stabilization
Tower side line isolates light petrol, bottom of towe and isolates hydrogasoline, and it is 90~95 DEG C that wherein side line light petrol extracts temperature out；
（2）Prefractionator is fractionated：Temperature be 165~175 DEG C hydrogasoline into prefractionator be fractionated, pressure 0.24~
It is fractionated under the conditions of 0.29 MPa, prefractionator tower top fractionates out middle gasoline, and the temperature of tower top is 148~150 DEG C, bottom of towe point
Heavy petrol is distillated, the temperature of bottom of towe is 220~224 DEG C；
（3）One-stage hydrogenation reacts：Heavy petrol and hydrogen mixing enter one-stage hydrogenation device in pressure after being warming up to 270~275 DEG C
Hydrogenation reaction generation one-stage hydrogenation product is carried out under the conditions of 2.0~2.17MPa；
（4）One section of desulphurization reaction：One-stage hydrogenation product generates one section of high score oil after entering one section of desulfurizer desulfurization；
（5）Secondary hydrogenation reacts：One section of oily and middle gasoline of high score mixes and heats up after being mixed to form heavy petrol mixture with hydrogen
Hydrogenation reaction generation secondary hydrogenation is carried out under the conditions of 2.0~2.2MPa of pressure into secondary hydrogenation device after to 265~270 DEG C
Product；
（6）Two sections of desulphurization reactions：Secondary hydrogenation product enters the cold high score oil of two sections of generation after two sections of desulfurizer desulfurization, and temperature is
155~165 DEG C, enter the refined generation treated gasoline of product stabilizer after two that pressure is 0.7~0.78MPa section cold high score oil,
The product stabilizer column bottom temperature is 209~211 DEG C, and gasoline product is formed after treated gasoline and light petrol mixing.
2. gasoline hydrogenation technique according to claim 1, it is characterized in that heavy petrol and hydrogen mixing are warming up to 270~275
The one-stage hydrogenation second reactor that one-stage hydrogenation device is initially entered after DEG C is carried out once under the conditions of 2.12~2.17MPa of pressure
Hydrogenation reaction, product for hydrogenation reaction enter the one-stage hydrogenation first-stage reactor of one-stage hydrogenation device temperature be 270~
275 DEG C, pressure be to carry out secondary hydrogenation reaction generation one-stage hydrogenation product under conditions of 2.12~2.17MPa.
3. gasoline hydrogenation technique according to claim 1, it is characterized in that temperature be 195~205 DEG C, pressure 0.7~
One section of high score oil of 0.75MPa enters stripper stripping, obtains one section of refined high score oil, and one section of refined high score is oily with middle vapour
Oil mixing, the wherein temperature of the stripped vapor of stripper are 245~255 DEG C, pressure is 0.9~1.1MPa.
4. gasoline hydrogenation technique according to claim 3, it is characterized in that the oily and middle gasoline mixing liter of one section of refined high score
The hydrogenation reactor that secondary hydrogenation device is initially entered after warm to 265~270 DEG C carries out one under the conditions of 2.0~2.2MPa of pressure
Secondary hydrogenation reaction, one time the product of hydrogenation reaction enters the finishing reactor of secondary hydrogenation device in 320~330 DEG C of temperature, pressure
Desulphurization reaction generation secondary hydrogenation product is carried out under the conditions of 1.9~1.96MPa of power.
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Citations (10)
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