CN103805253A - Hydrotreating method of inferior gasoline - Google Patents
Hydrotreating method of inferior gasoline Download PDFInfo
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- CN103805253A CN103805253A CN201210440449.0A CN201210440449A CN103805253A CN 103805253 A CN103805253 A CN 103805253A CN 201210440449 A CN201210440449 A CN 201210440449A CN 103805253 A CN103805253 A CN 103805253A
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Abstract
The invention discloses a hydrotreating method of inferior gasoline. The method comprises the following steps: (1) mixing inferior gasoline raw materials with circulating hydrogen and thermal loaded oil, performing pretreatment reaction of the mixture in a fluidized bed reactor; (2) allowing the effluent of the pretreatment reaction to enter a gasoline hydrogenation reactor; (3) heating the effluent of the hydrogenation reaction in a heating furnace, entering a heat exchanger, then entering a high temperature low pressure separator; (4) separating the obtained gas in a low temperature low pressure separator, performing gas stripping of the liquid to obtain the product; (5) heating the liquid which is obtained in step (3) and used as thermal loaded oil in the heat exchanger, and returning the liquid to step (1) for recycle. The method of the invention can ensure long-period running of the device, and make more effective use of heat energy.
Description
Technical field
The present invention relates to a kind of inferior patrol hydroprocessing process, particularly for oil refining enterprise's inferior patrol hydrotreater, can meet the method that long period is produced.
Technical background
In recent ten years, because crude production rate increasess slowly and heaviness increasingly, and market improves constantly light-end products requirement.Add the increasingly stringent of environmental regulation, therefore, also relatively propose higher requirement for the crude oil capacity to reprocess of oil refining enterprise.The secondary processing device of oil refining enterprise is mainly the devices such as coking, catalytic cracking, hydrogenation and catalytic reforming.
In refining of petroleum, coking is the abbreviation of residual oil coke, refers to that mink cell focus carries out cracking and the condensation reaction of the degree of depth under the hot conditions of 500 ℃ of left and right, produces the process of gas, gasoline, diesel oil, wax oil and refinery coke.Its advantage is to process various poor residuums, process is simple, investment and process cost are low, its shortcoming is that in coker gasoline and coker gas oil (being called for short coking gasoline and diesel in the present invention), unsaturated hydrocarbons content is high, and the content of the non-hydrocarbons such as sulfur-bearing, nitrogen is also high, need to further pass through hydrogen addition technology processing.
Also exist unsaturated hydrocarbons content high for the gasoline of catalytic unit output equally, and the also problem such as high of the content of the non-hydrocarbons such as sulfur-bearing, nitrogen, hydrogen addition technology processing need to further be passed through.Therefore, herein by above-mentioned catalytically cracked gasoline, the gasoline fractions such as coker gasoline and ardent solution gasoline are second-rate, and this patent is referred to as inferior patrol.
Carry out in hydrotreatment process at inferior patrol especially, oil refining enterprise finds because the unsaturated hydrocarbons in inferior patrol is relatively many, particularly the material such as alkene, diolefine at high temperature, easily there is Diels-Alder cyclization and polyreaction and form macromolecular organic compound, and further condensation green coke.These coking reactions mainly concentrate on high-temperature heat-exchanging and process furnace, and form incrustation, then take the positions such as reactor head to through logistics, cause production unit to need frequent shutdowns processing, cause to normal production and have a strong impact on.
Although interchanger and furnace outlet temperature of charge are also not bery high, heating-furnace pipe surface temperature is very high, as the furnace temperature of common hydrogenation unit process furnace can reach 500 ℃, high can reach more than 600 ℃, and therefore, the coking problem of interchanger and process furnace is very serious.Sometimes interchanger green coke material in process furnace can enter in reactor with material, is deposited on reactor catalyst bed top, has further accelerated the obstruction speed of reactor catalyst bed.
CN1990830 provides a kind of hydrofinishing process of coker gasoline; stock oil enters hydrogenation protecting reactor after mixing with hydrogen and contacts with hydrogenation protecting agent; under the condition of low temperature, react; its reaction effluent enters hydrogenation main reactor after process furnace heats up; under the condition of high temperature with Hydrobon catalyst contact reacts; its resultant of reaction through cooling, separate after, obtain hydrogen-rich gas and refining after gasoline fraction.
CN102041086A provides a kind of high-sulfur, high olefin catalytically cracked gasoline to clean the method for production, it is that catalytic gasoline of whole fraction is entered to selective hydrogenation, adopt gasoline hydrogenation pretreatment catalyst to carry out hydrogenation, again by selective hydrogenation gasoline through fractionation be divided into gently, heavy naphtha, then after last running gasoline being mixed with hydrogen, penetration depth hydrogenating desulfurization unit, adopt gasoline hydrogenation treatment catalyst to obtain low-sulfur content heavy fractioning hydrogenation gasoline, finally will after lighting end gasoline and the mediation of heavy fractioning hydrogenation gasoline, obtain state's IV clean gasoline.
CN101368111 provides a kind of method of catalytic gasoline hydrogenation modifying, is lighting end, heavy fraction by full gasoline faction cut; Petroleum naphtha fraction removes mercaptan wherein through caustic wash desulfuration alcohol; Heavy petrol fraction and hydrogen catalytic desulfurhydrogenation, denitrogenation, olefin saturation, reaction effluent or reaction effluent contact with octane value recovering catalyst after removing hydrogen sulfide, carry out isomerization, aromizing and building-up reactions, separate hydrogenated oil and obtain lighter hydrocarbons and gasoline fraction, the hydrogen-rich gas of high score tank deck is recycled through hydrogen sulfide stripping tank, stablize the lighter hydrocarbons of tower top and return fractionating tank fractionation again.There is the problem of easy incrustation and coking in heavy petrol fraction hydrogenating.
US4,113,603 reports use the hydrofinishing process of two sections to process diolefine and the sulfide in pyrolysis gasoline, and first paragraph uses the catalyzer of nickeliferous-tungsten to remove mercaptan, and second segment uses precious metals palladium catalyst to remove diolefine, and technique is comparatively complicated.
At present inferior patrol hydrotreatment technology, can meet gasoline products standard, but it is serious well not solve incrustation and coking problem, causes oil refining enterprise to produce the some months slash head of will stopping work; If dealt with improperly, even one or two months will be skimmed an apparatus for examination and repair again.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of inferior patrol hydroprocessing process, particularly for oil refining enterprise's inferior patrol hydrotreater, solve due to incrustation and coking, cause the problem that device can not long-term operation.
A kind of inferior patrol hydroprocessing process of the present invention, comprises following content:
(1) after bad gasoline is carried oily mixing with circulating hydrogen and heat, enter ebullated bed reactor from reactor lower part, carry out hydrogenation pretreatment reaction;
(2) step (1) gained reaction effluent enters gasoline hydrogenation reactor, carries out selective hydrogenation under hydrogenation conditions;
(3) step (2) gained reaction effluent is first after process furnace heats, then after interchanger, enters high-temperature low-pressure separator, carries out gas-liquid separation;
(4) step (3) gained gas enters low-temp low-pressure separator, carries out gas-liquid separation, and gained hydrogen-rich gas recycles after purifying treatment, obtain liquid after air lift as gasoline blend component or industrial chemicals;
(5) step (3) gained liquid carries oil as heat, and the hydrogenation reaction effluent after the heating of interchanger and process furnace carries out returning to step (1) after heat exchange intensification and recycles.
In the inventive method, the described bad gasoline of step (1) generally refers to the secondary processing of gasoline inferior of output in oil refining enterprise.As described in inferior patrol can be the coker gasoline cut of coker output, or the gasoline fraction of catalytic cracking unit output or be catalytically cracked gasoline after cutting, need carry out the component of selective hydrodesulfurization, can also be the by product pyrolysis gasoline that preparing ethylene by steam cracking process obtains.The common feature of bad gasoline is wherein to contain a certain amount of diolefine, and diolefine is the very unsettled compound of one, and its course of processing for inferior patrol has obvious disadvantageous effect.
In the inventive method, it can be the distillate after straight run oil or hydrotreatment that the described heat of step (1) is carried oil.Heat is carried oily initial boiling point should be higher than the final boiling point of inferior patrol (or doing), and preferably hot year oily initial boiling point is higher 60～100 ℃ than doing of inferior patrol.Heat is carried oily final boiling point and is generally 300～600 ℃, preferably 350～550 ℃.Described heat is carried oil specifically can select atmosphere 3rd side cut diesel oil, hydrogenation heavy gas oil, hydrocracking middle runnings or hydrocracking tail oil etc.Cycling hot is carried oily consumption, is generally 20%～150% of inferior patrol feedstock weight, is preferably 50%～100%.
In the inventive method, in step (1) before carrying oily mixed heat transfer with heat, bad gasoline and circulating hydrogen can first be warming up to 100～160 ℃ by heat exchange in cryogenic heat exchanger, then carry oil with the heat after heating and mixes also heat exchange to the required temperature of hydrogenation pretreatment reaction, enter hydrogenation pretreatment reaction device entrance.Reaction mass is after mixed heat transfer, and general control temperature is 220～260 ℃.
In the inventive method, the pretreatment condition of the described ebullated bed pretreatment reaction device of step (1) is generally: reaction pressure is generally 1～10MPa; Pretreatment temperature is 180 ℃～350 ℃, is preferably 200 ℃～300 ℃; Hydrogen to oil volume ratio (hydrogen/bad gasoline) is generally 50～500, and preferably 50～400; Volume space velocity is generally 0.5～10h
-1, be preferably 2～6 h
-1.
In the inventive method, in step (1), in ebullated bed reactor, be filled with boiling-bed catalyst.Described boiling-bed catalyst is the catalyzer with incrustation coking function.Described boiling-bed catalyst is shaped as spherical or bar shaped, and spherical diameter is 0.04～10mm, is preferably 0.04～5mm; Bar shaped is length 2～10mm, is preferably 3～6mm, and diameter is 1～6mm, is preferably 1.5～3.5mm.Described boiling-bed catalyst can be no acidic or weakly acidic porous oxide material, as in aluminum oxide, silicon oxide, amorphous silicon aluminium, titanium oxide and molecular sieve one or more etc.Also can be fresh or regenerated catalyst, protective material or the useless hydrogenation catalyst etc. take no acidic or weakly acidic porous oxide material as carrier.The hydrogenation activity component of catalyzer is generally one or more in W, Mo, Ni and Co, is generally 3wt%～50wt% in oxide compound hydrogenation activity component concentration.Boiling-bed catalyst can by technical process need to select suitable commercial catalyst, also can be by the preparation of existing method, can be also the regenerated catalyst of decaying catalyst after regeneration.
In the inventive method, in step (1), bad gasoline, circulating hydrogen and heat are carried oily mixed material and are entered pretreatment reaction device from reactor bottom, flow out the in-built aggrade dirt of reactor coking protective material from the top of reactor.According to method of the present invention, described pretreatment reaction device can also be by adding fresh boiling-bed catalyst in reactor head, and from the more serious boiling-bed catalyst of reactor discharge section incrustation coking, realize the online displacement of catalyzer, can long-term operation to maintain ebullated bed pretreatment reaction device.Described catalyzer is replaced into process well known to those skilled in the art online.
In the inventive method, the described gasoline hydrogenation reactor of step (2) is conventional fixed-bed reactor.The hydrogenation catalyst of reactor charge is generally with no acidic or weakly acidic porous oxide material, as in aluminum oxide, silicon oxide, amorphous silicon aluminium, titanium oxide and molecular sieve one or more etc. be carrier, in carrier, can contain suitable auxiliary agent, as P, B etc. simultaneously.The hydrogenation activity component of hydrogenation catalyst is generally one or more in W, Mo, Ni and Co, is generally 3wt%～50wt% in oxide compound hydrogenation activity component concentration.Gasoline hydrogenation catalyst can by technical process need to select suitable commercial catalyst, also can be by the preparation of existing method, can be also the regenerated catalyst of decaying catalyst after regeneration.
In the inventive method, the processing condition of the described hydrogenation reaction of step (2) are: reactive hydrogen dividing potential drop 1～10MPa, volume space velocity 1～10h
-1, 200～360 ℃ of temperature of reaction, hydrogen to oil volume ratio (hydrogen/bad gasoline) is generally 100～1000.
In the inventive method, described process furnace and interchanger are process furnace known in the art and interchanger, and its operational condition is also condition well known to those skilled in the art.The temperature control of described process furnace is to mix needed heat with coker gasoline raw material.
In the inventive method, the described high-temperature low-pressure separator (low point of heat) of step (3) is gas-liquid separator known in the art, and its operational condition is well known to those skilled in the art.The service temperature general control that heat is low point is 10～60 ℃ of the final boiling point higher than catalytically cracked gasoline, preferably high 30～55 ℃.
In the inventive method, the described low-temp low-pressure separator (cold low point) of step (4) is gas-liquid separator known in the art, and its operational condition is also condition well known to those skilled in the art.
The inventive method will increase a pretreatment reaction device before inferior patrol hydrodesulfurization unit reactor, and carries oil as heat-carrying and make the medium that in pretreatment reaction device, incrustation coking protective material seethes with excitement by heat, and tool has the following advantages:
1, raw material provided by the invention and heat are carried oil and are directly mixed into pretreatment reaction device, avoided bad gasoline in high temperature heat exchange and heat-processed due to local superheating, unsaturated hydrocarbons polymerization coking is deposited in equipment, then brings reactor head into and cause the generation of improper shut-down phenomenon.In the inventive method, a small amount of unsaturated hydrocarbons polymerization coking containing in bad gasoline, will bring pretreatment reaction device into by liquid phase stream and carry out incrustation and coking, the more effective heat energy that utilizes, and the long-term operation of assurance device simultaneously.
2, in the inventive method; adopt ebullated bed reactor as pretreatment reaction device; pretreatment reaction device is replaced incrustation coking protective material online; can avoid top incrustation and the coking of hydrogenator; avoid the impact of skimming head due to the shut-down of Pressure Drop generation device; the long-term operation of assurance device, easy and simple to handle, there is considerable economic benefit.
3, the inventive method for the treatment of the coker gasoline raw material inferior that carries coke powder time, can more effectively prevent that coke powder from entering hydrodesulphurisatioreactors reactors top.
4, bad gasoline provided by the invention heat higher with temperature under low-temperature condition carry oil directly mix, mixing time is very short, more uniform temperature can more effectively be utilized heat energy, reduction plant energy consumption.
5, in the inventive method, owing to there being the reaction effluent after pair hydrogenating desulfurization to heat, and carry oily heat exchange with heat again, not only avoided raw material and heat to carry the local superheating problem of oil in direct heat exchange and heat-processed, be also more conducive to material and distribute.
Accompanying drawing explanation
Fig. 1 is a kind of principle process schematic diagram of the inventive method.
Embodiment
Method the present invention being disclosed below in conjunction with the drawings and specific embodiments is for a more detailed description.
As shown in Figure 1, bad gasoline is mixed with the hydrogen through pipeline 17 through pipeline 19 through pipeline 1, heat year oil, enters ebullated bed pretreatment reaction device 3 through pipeline 2, carries out hydrogenation pretreatment reaction.Add hydrogen pretreatment gained reaction effluent and enter gasoline hydrogenation reactor 5 without separating directly through pipeline 4, carry out hydrogenation reaction.Hydrogenation gained reaction effluent, enters interchanger 9 and carries out heat exchange through pipeline 8 through pipeline 6 after process furnace 7 heats, then enters high-temperature low-pressure separator 11 through pipeline 10 and carry out gas-liquid separation.The isolated gas phase effluent of high-temperature low-pressure separator 11 enters low-temp low-pressure separator 13 through pipeline 12 and carries out gas-liquid separation, and gained liquid is discharged through pipeline 15, after further processing, obtains gasoline blend component or industrial chemicals.Gained gas leaves through pipeline 14, after further purifying treatment, after the new hydrogen of introducing mixes, utilizes through pipeline 17 and the raw material mixed cycle in pipeline 1 with pipeline 16.High-temperature low-pressure separator 11 is isolated liquid phase effluent through pipeline 18, enters interchanger 9 and carries out heat exchange, then mix through pipeline 1 with through the hydrogen of pipeline 17 with bad gasoline through pipeline 19, returns to boiling bed hydrogenation pretreatment reaction device through pipeline 2.
Below in conjunction with preferred embodiment, the present invention is further described, should be appreciated that preferred embodiment described herein, only for description and interpretation the present invention, is not intended to limit the present invention.
In the embodiment of the present invention, heat used is carried oil nature in table 1 simultaneously.
Table 1 heat is carried oil nature.
| Turning oil title | Hydrocracking diesel oil |
| Boiling range scope/℃ | 260～369 |
| Sulphur content/μ gg -1 | <5 |
| Nitrogen content/μ gg -1 | <1 |
Embodiment 1
Adopt the technical process shown in Fig. 1.Raw materials used oil properties is listed in table 2, and catalyst property is listed in table 3, and processing condition and test-results are listed in respectively table 4 and table 12.
Table 2 stock oil character.
| Oil product title | FCC gasoline |
| Density, g/cm 3 | 0.7310 |
| Boiling range scope/℃ | 36～206 |
| Sulphur content/μ gg -1 | 576 |
| Nitrogen content/μ gg -1 | 38 |
The chief component of table 3 catalyzer and character.
| ? | Pretreatment catalyst | Hydrogenation catalyst |
| Catalyzer composition | ? | ? |
| MoO 3+CoO/wt% | 3 | 20 |
| Carrier | Aluminum oxide | Aluminum oxide |
| The main character of catalyzer | ? | ? |
| Particle diameter, mm | 0.2 | — |
| Specific surface/m 2·g -1 | 180 | 226 |
| Pore volume/mlg -1 | 0.68 | 0.51 |
Table 4 embodiment 1 processing condition.
| Processing condition | Data |
| Ebullated bed pretreatment reaction device | ? |
| Volume space velocity, h -1 | 4 |
| Heat is carried oily consumption/raw material weight ratio | 0.55 |
| Hydrogen/FCC gasoline volume ratio | 400 |
| Average reaction temperature/℃ | 230 |
| Reaction pressure/MPa | 2.5 |
| Hydrotreating reactor | ? |
| Reaction pressure/MPa | 2.5 |
| Average reaction temperature ,/℃ | 280 |
| Hydrogen to oil volume ratio/v/v | 400 |
| Volume space velocity/h -1 | 4.0 |
Embodiment 2
Adopt the technical process shown in Fig. 1.Raw material oil properties is listed in table 5, and catalyst property is listed in table 6, and processing condition and test-results are listed in respectively table 7 and table 12.
Table 5 stock oil character.
| Oil product title | Coker gasoline raw material |
| Density, g/cm 3 | 0.7413 |
| Boiling range scope/℃ | 57～206 |
| Sulphur content/μ g/g | 5656 |
| Nitrogen content/μ g/g | 236 |
The chief component of table 6 catalyzer and character.
| ? | Pretreatment catalyst | Hydrogenation catalyst |
| Catalyzer composition | ? | ? |
| MoO 3+CoO/wt% | 0 | 25 |
| Carrier | Aluminum oxide | Aluminum oxide |
| The main character of catalyzer | ? | ? |
| Particle diameter, mm | 0.3 | — |
| Specific surface/m 2·g -1 | 180 | 226 |
| Pore volume/mlg -1 | 0.68 | 0.51 |
Table 7 embodiment 2 processing condition.
| Processing condition | Data |
| Ebullated bed pretreatment reaction device | ? |
| Volume space velocity, h -1 | 4 |
| Heat is carried oily consumption/raw material weight ratio | 0.60 |
| Hydrogen/coker gasoline volume ratio | 400 |
| Average reaction temperature/℃ | 230 |
| Reaction pressure/MPa | 2.5 |
| Hydrotreating reactor | ? |
| Reaction pressure/MPa | 2.5 |
| Average reaction temperature/℃ | 290 |
| Hydrogen to oil volume ratio/v/v | 400 |
| Volume space velocity/h -1 | 4.0 |
Comparative example 1
Adopt in prior art, coker gasoline and year oil are mixed, be introduced into pre-guard reactor, then enter the production technique of hydrogenator.Mixture enters all and enters from pre-guard reactor and hydrogenator top, and flow out bottom.Stock oil, heat year oil and catalyzer are with embodiment 2, and processing condition and test-results are listed in respectively table 8 and table 12.
Table 8 comparative example 1 processing condition.
| Processing condition | Data |
| Volume space velocity, h -1 | 4 |
| Heat is carried oily consumption/raw material weight ratio | 0.60 |
| Hydrogen/coker gasoline volume ratio | 400 |
| Pre-protection average reaction temperature/℃ | 220 |
| Hydrogenator average reaction temperature/℃ | 280 |
| Reaction pressure/MPa | 2.5 |
Comparative example 2
Adopt the technical process in disclosed method in prior art CN201010615240.4.Bad gasoline and thermal cycling oil are mixed into hydrogenation pretreatment reaction device, react entering hydrotreatment through the raw material heat exchange after hydrotreatment, after hydrotreatment, mixture enters process furnace heating, again with pretreated raw material heat exchange, finally carry out again product and thermal cycling oil separating, output qualified product.
Stock oil is with embodiment 2, and a heat year oil nature is listed in table 9, and catalyst property is listed in table 10, and processing condition and test-results are listed in respectively table 11 and table 12.
Table 9 heat is carried oil nature.
| Turning oil title | Hydrofining vacuum distillate |
| Boiling range scope/℃ | 390～550 |
| Sulphur content/μ gg -1 | <5 |
| Nitrogen content/μ gg -1 | <1 |
The chief component of table 10 catalyzer and character.
| ? | Pretreatment catalyst | Hydrogenation catalyst |
| Catalyzer composition | ? | ? |
| MoO
3+CoO/ |
12 | 20 |
| Carrier | Aluminum oxide | Aluminum oxide |
| The main character of catalyzer | ? | ? |
| Particle diameter, mm | 0.3 | — |
| Specific surface/m 2·g -1 | 180 | 226 |
| Pore volume/mlg -1 | 0.68 | 0.51 |
Table 11 comparative example 2 processing condition.
| Processing condition | Data |
| Volume space velocity, h -1 | 4 |
| Heat is carried oily consumption/raw material weight ratio | 0.25 |
| Hydrogen/coker gasoline volume ratio | 400 |
| Pretreatment reaction device average reaction temperature/℃ | 160 |
| Hydrotreating reactor average reaction temperature/℃ | 290 |
| Reaction pressure/MPa | 2.5 |
Table 12 product property and 3500 hours pressure drop ratios are.
| Result | Embodiment 1 | Embodiment 2 | Comparative example 1 | Comparative example 2 |
| 300 hours sulphur content/μ gg -1 | 35 | 46 | 56 | 59 |
| 300 hours nitrogen content/μ gg -1 | — | 5 | 6 | 6 |
| 3000 hours sulphur content/μ gg -1 | 36 | 47 | 66 | 71 |
| 3000 hours nitrogen content/μ gg -1 | — | 5 | 8 | 9 |
| 3000 hours Pressure Drop (sum falls in two reactor pressures)/MPa | 0.05 | 0.05 | 0.13 | 0.13 |
Result by table 12 can be found out, after the running of 3000 hours, the processing technological flow that adopts the inventive method to provide, quality product is better, device pressure drop is lower, simultaneously because pretreatment reaction device in the inventive method is ebullated bed reactor, can realize displacement online after boiling-bed catalyst coking, can assurance device pressure drop in lower scope, better solving device problem of pressure drop.
Claims (12)
1. an inferior patrol hydroprocessing process, comprises following content:
(1) after bad gasoline is carried oily mixing with circulating hydrogen and heat, enter ebullated bed reactor from reactor lower part, carry out hydrogenation pretreatment reaction;
(2) step (1) gained reaction effluent enters gasoline hydrogenation reactor, carries out selective hydrogenation under hydrogenation conditions;
(3) step (2) gained reaction effluent is first after process furnace heats, then after interchanger, enters high-temperature low-pressure separator, carries out gas-liquid separation;
(4) step (3) gained gas enters low-temp low-pressure separator, carries out gas-liquid separation, and gained hydrogen-rich gas recycles after purifying treatment, obtain liquid after air lift as gasoline blend component or industrial chemicals;
(5) step (3) gained liquid carries oil as heat, and the hydrogenation reaction effluent after the heating of interchanger and process furnace carries out returning to step (1) after heat exchange intensification and recycles.
2. in accordance with the method for claim 1, it is characterized in that, in step (1), before carrying oily mixed heat transfer with heat, bad gasoline and circulating hydrogen are first warming up to 100～160 ℃ by heat exchange in cryogenic heat exchanger.
3. in accordance with the method for claim 1, it is characterized in that, described bad gasoline is coker gasoline, catalytically cracked gasoline or pyrolysis gasoline.
4. in accordance with the method for claim 1, it is characterized in that, it is the distillate after straight run oil or hydrotreatment that described heat is carried oil, and heat is carried the final boiling point of oily initial boiling point higher than bad gasoline.
5. in accordance with the method for claim 4, it is characterized in that, it is higher 60～100 ℃ than doing of inferior patrol that described heat is carried oily initial boiling point.
6. in accordance with the method for claim 5, it is characterized in that, described heat is carried oily final boiling point and is generally 300～600 ℃.
7. in accordance with the method for claim 1, it is characterized in that, it is 20%～150% of bad gasoline weight that described heat is carried oily consumption.
8. in accordance with the method for claim 1, it is characterized in that, the pretreatment condition of the ebullated bed reactor described in step (1) is: reactive hydrogen dividing potential drop is 1～10MPa, pretreatment temperature is 180 ℃～350 ℃, hydrogen/inferior patrol volume ratio is 50～500, and inferior patrol volume space velocity is 0.5～10h
-1.
9. in accordance with the method for claim 1; it is characterized in that; in step (1), in boiling bed hydrogenation pretreatment reaction device, be filled with boiling-bed catalyst; described boiling-bed catalyst is one or more in aluminum oxide, silicon oxide, amorphous silicon aluminium, titanium oxide and molecular sieve, or is fresh or regenerated catalyst, protective material or useless hydrogenation catalyst take no acidic or weakly acidic porous oxide material as carrier.
10. in accordance with the method for claim 1, it is characterized in that, in step (2), the hydrogenation catalyst of gasoline hydrogenation reactor charge is take no acidic or weakly acidic porous oxide material as carrier, hydrogenation activity component is one or more in W, Mo, Ni and Co, take oxide compound hydrogenation activity component concentration as 3wt%～50wt%.
11. in accordance with the method for claim 1, it is characterized in that, the described hydrogenation conditions of step (2) is: reactive hydrogen dividing potential drop 1～10MPa, inferior patrol volume space velocity 1～10h
-1, 200～360 ℃ of temperature of reaction, hydrogen/inferior patrol volume ratio 100～1000.
12. in accordance with the method for claim 1, it is characterized in that, the temperature that the described high-temperature low-pressure of step (3) divides is controlled at higher than 10～60 ℃ of the final boiling point of catalytically cracked gasoline.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018019490A1 (en) * | 2016-07-27 | 2018-02-01 | IFP Energies Nouvelles | Method for the selective hydrogenation of a pyrolysis gasoline feedstock with a three-phase reactor |
| WO2018019489A1 (en) * | 2016-07-27 | 2018-02-01 | IFP Energies Nouvelles | Method for the selective hydrogenation of a pyrolysis gasoline feedstock with a three-phase reactor in the presence of a heavy paraffin hydrocarbon cut |
| CN107815329A (en) * | 2016-09-14 | 2018-03-20 | 中国石化工程建设有限公司 | A kind of method of heavy oil combined hydrogenation |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1510111A (en) * | 2002-12-26 | 2004-07-07 | 中国科学院大连化学物理研究所 | Hydrocarbon oil cryogenic desulfurizing method |
| CN101148607A (en) * | 2006-09-20 | 2008-03-26 | 中国石油化工股份有限公司 | Hydrocarbon hydroprocessing technique |
| CN102559260A (en) * | 2010-12-22 | 2012-07-11 | 冯刚 | Rear inferior gasoline fraction hydrotreating method for heating furnace |
-
2012
- 2012-11-07 CN CN201210440449.0A patent/CN103805253B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1510111A (en) * | 2002-12-26 | 2004-07-07 | 中国科学院大连化学物理研究所 | Hydrocarbon oil cryogenic desulfurizing method |
| CN101148607A (en) * | 2006-09-20 | 2008-03-26 | 中国石油化工股份有限公司 | Hydrocarbon hydroprocessing technique |
| CN102559260A (en) * | 2010-12-22 | 2012-07-11 | 冯刚 | Rear inferior gasoline fraction hydrotreating method for heating furnace |
Non-Patent Citations (2)
| Title |
|---|
| EDWARD FURIMSKY: "《重油转化催化剂》", 31 December 2010, 石油工业出版社 * |
| 日本石油学会 编: "《石油炼制工艺方法手册》", 31 July 1979, 石油工业出版社 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2018019490A1 (en) * | 2016-07-27 | 2018-02-01 | IFP Energies Nouvelles | Method for the selective hydrogenation of a pyrolysis gasoline feedstock with a three-phase reactor |
| WO2018019489A1 (en) * | 2016-07-27 | 2018-02-01 | IFP Energies Nouvelles | Method for the selective hydrogenation of a pyrolysis gasoline feedstock with a three-phase reactor in the presence of a heavy paraffin hydrocarbon cut |
| FR3054555A1 (en) * | 2016-07-27 | 2018-02-02 | IFP Energies Nouvelles | METHOD FOR SELECTIVE HYDROGENATION OF A PYROLYTIC ESSENCE LOAD WITH A THREE-PHASE REACTOR IN THE PRESENCE OF A CUTTING OF HEAVY PARAFFINIC HYDROCARBONS |
| FR3054556A1 (en) * | 2016-07-27 | 2018-02-02 | IFP Energies Nouvelles | METHOD FOR SELECTIVE HYDROGENATION OF A PYROLYTIC ESSENCE LOAD WITH A THREE-PHASE REACTOR |
| US10829700B2 (en) | 2016-07-27 | 2020-11-10 | IFP Energies Nouvelles | Method for the selective hydrogenation of a pyrolysis gasoline feedstock with a three-phase reactor |
| CN107815329A (en) * | 2016-09-14 | 2018-03-20 | 中国石化工程建设有限公司 | A kind of method of heavy oil combined hydrogenation |
| CN107815329B (en) * | 2016-09-14 | 2019-09-06 | 中国石化工程建设有限公司 | A kind of method of heavy oil combined hydrogenation |
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