CN103805261B - A kind of inferior patrol hydrodesulfurizationprocess process - Google Patents
A kind of inferior patrol hydrodesulfurizationprocess process Download PDFInfo
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Abstract
The invention discloses a kind of inferior patrol hydrodesulfurizationprocess process.The method comprises: (1) inferior patrol first carries out heat exchange with hydrodesulfurization reaction effluent, then carries oil with heat and be mixed into ebullated bed reactor and carry out pretreatment reaction; (2) gained pretreated stream effluent enters gasoline hydrodesulfurizationmethod reactor; (3) hydrodesulfurization reaction effluent enter heat low point be separated; (4) heat low point of gas enters cold low point and is separated, and obtains gasoline products or gasoline blending component; (5) low point of heat obtains liquid and carries oil as heat and return step (1).The inventive method significantly can extend the running period of inferior patrol device.
Description
Technical field
The present invention relates to a kind of inferior patrol hydrodesulfurizationprocess process, particularly for oil refining enterprise's inferior patrol hydrotreater, because coking causes the improper break-down maintenance of device, the method that improper maintenance extends manufacture cycle can be reduced.
Technical background
In recent years, China's petrol and diesel oil product up-gradation was very fast, particularly required harsher for gasoline product quality.In current China gasoline component, secondary processing oil ratio example is higher, such as catalytically cracked gasoline, coker gasoline and pyrolysis gasoline etc.Have in above-mentioned gasoline products character, unsaturated hydrocarbons content is higher, and stability is poor, and sulphur and nitrogen are difficult to the gasoline standard of satisfied current China.Therefore most of oil refining enterprise carries out hydrotreatment to this type of gasoline.Herein by above-mentioned catalytically cracked gasoline, the gasoline fraction such as coker gasoline and pyrolysis gasoline is second-rate, and this patent is referred to as inferior patrol.
Carry out in hydroprocessing processes at inferior patrol, oil refining enterprise finds because the unsaturated hydrocarbons in inferior patrol is relatively many, particularly the material such as alkene, diolefine at high temperature, easy generation Diels-Alder cyclization and polyreaction 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 process, cause to normal production and have a strong impact on.
US4, the diolefine in the hydrofinishing process process pyrolysis gasoline of 113,603 report uses two sections and sulfide, first paragraph uses the catalyzer removing mercaptan of nickeliferous-tungsten, and second segment uses precious metals palladium catalyst removing diolefine, and technique is comparatively complicated.
CN101368111A provides a kind of method of catalytic gasoline hydrogenation modifying, is lighting end, heavy fraction by complete for gasoline faction cut; Light gasoline fractions removes mercaptan wherein through caustic wash desulfuration alcohol; Heavy gasoline fractions and hydrogen catalytic hydrogenating desulfurization, 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, be separated hydrogenated oil and obtain lighter hydrocarbons and gasoline fraction, recycled through hydrogen sulfide stripping tank by the hydrogen-rich gas of high score tank deck, the lighter hydrocarbons stablizing tower top return fractionating tank fractionation again.
CN102041086A provides a kind of method of high-sulfur, high olefin catalytically cracked gasoline cleanly production, it is that catalytic gasoline of whole fraction is entered selective hydrogenation, gasoline hydrogenation pretreatment catalyst is adopted to carry out hydrogenation, again selective hydrogenation gasoline is divided into gently through fractionation, 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 obtain state IV clean gasoline by after lighting end gasoline and heavy fractioning hydrogenation gasoline blending.There is the problem of easy incrustation and coking in heavy gasoline fractions hydrogenation.
Current inferior patrol hydrotreating techniques, can meet gasoline products standard, but it is serious well to solve incrustation and coking problem, causes oil refining enterprise to produce some months and will to stop work slash head; If dealt with improperly, even one or two months will skim 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 hydrodesulfurizationprocess process, particularly for oil refining enterprise's inferior patrol hydrotreater, solve due to incrustation and coking, cause device can not the problem of long-term operation.
A kind of inferior patrol hydrodesulfurizationprocess process of the present invention, comprises following content:
(1) after bad gasoline mixes with hydrogen, after interchanger heat exchange, carry oil with the heat of circulation mix, then after process furnace heating, enter ebullated bed reactor from reactor lower part, carry out weighted BMO spaces reaction;
(2) step (1) gained reaction effluent enters gasoline hydrodesulfurizationmethod reactor, under hydrodesulfurization reaction condition, carry out selective hydrodesulfurization reaction;
(3) step (2) gained reaction effluent enters high-temperature low-pressure separator after interchanger, 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 uses through purifying treatment Posterior circle, obtains liquid after air lift as gasoline products or gasoline blending component;
(5) step (3) gained liquid carries oil as heat and returns step (1) and recycle.
In the inventive method, the bad gasoline described in step (1) generally refers to the secondary processing of gasoline inferior that oil refining enterprise produces or petroleum naphtha.Described bad gasoline can need to carry out inferior patrol cut that the component of selective hydrodesulfurization or coking obtains or the inferior patrol cut that thermal cracking processes obtains or the by product pyrolysis gasoline etc. that steam cracking process of producing ethylene obtains for the gasoline fraction of various catalytic cracking unit output or catalytically cracked gasoline after cutting.The common feature of bad gasoline is that diolefine is a kind of very unstable compound, and its course of processing for inferior patrol has obvious disadvantageous effect wherein containing a certain amount of diolefine.
In the inventive method, after described bad gasoline mixes with hydrogen, first after interchanger and hydrodesulfurization reaction effluent carry out heat exchange, then after process furnace heating, ebullated bed preatreating reactors can be entered and carries out weighted BMO spaces reaction.
In the inventive method, the heat described in step (1) carries oil can for the distillate after straight run oil or hydrotreatment.Heat carries oily initial boiling point should higher than the final boiling point of inferior patrol (or doing), and the initial boiling point that preferred heat carries oil is higher 50 ~ 100 DEG C than doing of inferior patrol.The final boiling point that heat carries oil is generally 300 ~ 600 DEG C, preferably 350 ~ 550 DEG C.Described heat carries oil specifically can select atmosphere 3rd side cut diesel oil, hydrogenation heavy gas oil, hydrocracking middle runnings or hydrocracking tail oil etc.Cycling hot carries the consumption of oil, is generally 20% ~ 150% of inferior patrol feedstock weight, is preferably 50% ~ 100%.
In the inventive method, the pretreatment condition of the preatreating reactors described in step (1) is generally: reaction pressure is generally 1 ~ 6MPa; Pretreatment temperature is 180 DEG C ~ 350 DEG C, is preferably 230 DEG C ~ 300 DEG C; Hydrogen to oil volume ratio (hydrogen/bad gasoline) is generally 50 ~ 500, and preferably 50 ~ 200; Volume space velocity is generally 0.5 ~ 10h
-1, be preferably 2 ~ 6h
-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 shape is spherical or bar shaped, and spherical diameter is 0.04 ~ 10mm, is preferably 0.04 ~ 5mm; Bar shaped is length 2 ~ 10mm, and be preferably 3 ~ 6mm, 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 one or more in aluminum oxide, silicon oxide, amorphous silicon aluminium, titanium oxide and molecular sieve etc.Also can be carrier with no acidic or weakly acidic porous oxide material fresh or regenerated catalyst, protective material or useless hydrogenation catalyst etc.The hydrogenation active component of catalyzer is generally one or more in W, Mo, Ni and Co, is generally 3wt% ~ 50wt% with oxide basis hydrogenation active component content.Boiling-bed catalyst can select suitable commercial catalyst by the needs of technical process, also can prepare by existing method, also can be the regenerated catalyst of decaying catalyst after regeneration.
In the inventive method, in step (1), bad gasoline, hydrogen and heat are carried oily mixed material and are entered preatreating reactors from reactor bottom, flow out from the top of reactor, reactor in-built aggrade dirt coking protective material.According to method of the present invention, described preatreating reactors can also 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 preatreating reactors.Described catalyzer is replaced into process well known to those skilled in the art online.
In the inventive method, the gasoline hydrodesulfurizationmethod reactor described in step (2) is fixed-bed reactor.The catalyst for selectively hydrodesulfurizing of reactor charge is generally with no acidic or weakly acidic porous oxide material, if one or more in aluminum oxide, silicon oxide, amorphous silicon aluminium, titanium oxide and molecular sieve etc. are carrier, can suitable auxiliary agent be contained, as P, B etc. in carrier simultaneously.The hydrogenation active component of catalyst for selectively hydrodesulfurizing is generally one or more in W, Mo, Ni and Co, is generally 3wt% ~ 50wt% with oxide basis hydrogenation active component content.Catalyst for selectively hydrodesulfurizing can select suitable commercial catalyst by the needs of technical process, also can prepare by existing method, also can be the regenerated catalyst of decaying catalyst after regeneration.
In the inventive method, the processing condition of the selective hydrodesulfurization reaction described in step (2) are: reaction pressure 1 ~ 6MPa, volume space velocity) 1 ~ 10h
-1, temperature of reaction 230 ~ 360 DEG C, hydrogen to oil volume ratio (hydrogen/bad gasoline 100 ~ 1000.
In the inventive method, the high-temperature low-pressure separator (low point of heat) described in step (3) is gas-liquid separator known in the art.The temperature of low point of heat controls at the final boiling point 10 ~ 50 DEG C higher than inferior patrol, is preferably 20 ~ 40 DEG C.
In the inventive method, the low-temp low-pressure separator (cold low point) described in 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 increases a preatreating reactors by before inferior patrol hydrodesulfurization unit reactor, and carries oil as heat-carrying and the medium making incrustation coking protective material boiling in preatreating reactors by heat, and tool has the following advantages:
1, raw material provided by the invention and hydrogen are first after heat exchange, carry oil with heat directly to mix successively by preatreating reactors and selective hydrodesulfurization reactor, avoid inferior patrol in heat exchange and heat-processed due to local superheating, unsaturated hydrocarbons polymerization coking is deposited in a device, then brings the problem of reactor head into.In the inventive method, a small amount of unsaturated hydrocarbons polymerization coking, brings preatreating reactors into by liquid phase stream heat year oil and carries out incrustation and coking; Even if after preatreating reactors, in raw material, still have a small amount of unsaturated hydrocarbons to be polymerized in selective hydrodesulfurization reactor, equally also can be dissolved in heat and carry in oil, take reactive system out of, reduce the coking factor in selective hydrodesulfurization reactor.Simultaneously because heat carries the existence of oil, reaction mass is gas-liquid two-phase, more effectively can utilize heat energy, and the long-term operation of assurance device.
2, method provided by the invention, as long as simply transform existing apparatus equipment, just requirement can be reached, preatreating reactors replaces incrustation coked catalyst online, can avoid top incrustation and the coking of hydrogenator, avoiding stops work due to Pressure Drop generation device skims the impact of head, the long-term operation of assurance device, easy and simple to handle, there is considerable economic benefit.
3, in the inventive method, carry oil owing to there being heat and not only avoid the local superheating problem of raw material in direct heat exchange and heat-processed, the problem that resin and asphalt that hydrogenation process produces on a small quantity is deposited on catalyst surface can also be solved, make resin and asphalt be dissolved in heat medium oil, be also more conducive to material distribution.
4, due in the method, heat year oil and raw material, after pretreatment reaction, enter selective hydrodesulfurization reactor, are more conducive to material distribution, can ensure that raw material better carries out selective hydrodesulfurization reaction.
5, due in the method, heat year oil and raw material are after selective hydrodesulfurization reaction, through interchanger, enter high-temperature low-pressure separator, utilize heat to carry oil and be separated with the boiling range difference of raw material, isolated heat carries oil at a certain temperature, mix with raw material before turning back to preatreating reactors, carry out recycle, heat energy is fully utilized, can plant energy consumption be reduced.
Accompanying drawing explanation
Fig. 1 is a kind of principle process schematic diagram of the inventive method.
Embodiment
The method disclosed the present invention below in conjunction with the drawings and specific embodiments is for a more detailed description.
As shown in Figure 1, the technical process of a kind of inferior patrol hydrodesulfurizationprocess process of the present invention is: bad gasoline through pipeline 1, mix with the hydrogen through pipeline 2, enters interchanger 3, carries out heat exchange with selective hydrodesulfurization reaction effluent.Parallel feeding after heat exchange and through the heat of pipeline 16 carry oil mixing after, enter process furnace 17 and heat, then enter ebullated bed preatreating reactors 5 through pipeline 4, carry out weighted BMO spaces reaction.Weighted BMO spaces gained reaction effluent directly enters selective hydrodesulfurization reactor 7 through pipeline 6 without separation, carries out selective hydrodesulfurization reaction.Selective hydrodesulfurization gained reaction effluent enters interchanger 3 through pipeline 8 and carries out heat exchange, then enters high-temperature low-pressure separator 10 through pipeline 9 and carry out gas-liquid separation.The isolated vapor phase stream effluent of high-temperature low-pressure separator 10 enters low-temp low-pressure separator 12 through pipeline 11 and carries out gas-liquid separation, and gained liquid through line 13 is discharged, after processing further, obtain gasoline products or gasoline blending component.Gained gas leaves through pipeline 14, and after further purifying treatment, after the new hydrogen introduced with pipeline 15 mixes, the raw material mixed cycle in pipeline 2 with pipeline 1 utilizes.High-temperature low-pressure separator 10 isolates liquid phase stream effluent through pipeline 16, returns boiling bed hydrogenation preatreating reactors.
Below in conjunction with preferred embodiment, the present invention is further described, should be appreciated that preferred embodiment described herein is only for instruction and explanation of the present invention, is not intended to limit the present invention.
In the embodiment of the present invention, heat used carries oil nature in table 1 simultaneously.
Table 1 heat carries oil nature.
| Turning oil title | Hydrocracking diesel oil |
| Boiling range scope/DEG C | 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 lists in table 2 respectively, and catalyst property lists in table 3, and processing condition and test-results list in table 4 and table 12 respectively.
Table 2 stock oil character.
| Oil product title | FCC gasoline |
| Density, g/cm 3 | 0.7310 |
| Boiling range scope/DEG C | 36～206 |
| Sulphur content/μ gg -1 | 576 |
| Nitrogen content/μ gg -1 | 38 |
| Mercaptan sulfur/μ gg -1 | 35.4 |
| RON | 93.5 |
The main composition of table 3 catalyzer and character.
| Catalyzer | Pretreatment catalyst | Hydrogenation catalyst |
| Catalyzer forms | ||
| 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 preatreating reactors | |
| Volume space velocity, h -1 | 4 |
| Heat carries oil/raw material weight ratio | 0.55 |
| Hydrogen/FCC gasoline volume ratio | 400 |
| Average reaction temperature/DEG C | 230 |
| Reaction pressure/MPa | 2.5 |
| Hydrodesulphurisatioreactors reactors | |
| Reaction pressure/MPa | 2.5 |
| Average reaction temperature/DEG C | 280 |
| Hydrogen/FCC gasoline volume ratio/v/v | 400 |
| Volume space velocity/h -1 | 4.0 |
Embodiment 2
Adopt the technical process shown in Fig. 1.Stock oil character lists in table 5, and catalyst property lists in table 6, and processing condition and test-results list in table 7 and table 12 respectively.
Table 5 stock oil character.
| Oil product title | Coker gasoline raw material |
| Density, g/cm 3 | 0.7413 |
| Boiling range scope/DEG C | 57～206 |
| Sulphur content, μ g/g | 5656 |
| Nitrogen content, μ g/g | 236 |
The main composition of table 6 catalyzer and character.
| Catalyzer | Pretreatment catalyst | Hydrogenation catalyst |
| Catalyzer forms | ||
| 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 |
| Preatreating reactors | |
| Volume space velocity, h -1 | 4 |
| Heat carries oil/raw material weight ratio | 0.60 |
| Hydrogen/coker gasoline volume ratio | 400 |
| Reaction pressure/MPa | 2.5 |
| Average reaction temperature/DEG C | 230 |
| Hydrodesulphurisatioreactors reactors | |
| Volume space velocity, h -1 | 4 |
| Hydrogen/coker gasoline volume ratio | 400 |
| Average reaction temperature ,/DEG C | 290 |
| Reaction pressure/MPa | 2.5 |
Comparative example 1
Adopt in prior art and coker gasoline and year oil are mixed, be introduced into pre-guard reactor, then enter the production technique of hydrogenator.Mixture enters and all enters from pre-guard reactor and hydrogenator top, and bottom is flowed out.Raw materials used oil, heat year oil and catalyzer are with embodiment 2, and processing condition and test-results list in table 8 and table 12 respectively.
Table 8 comparative example 1 processing condition.
| Processing condition | Data |
| Volume space velocity, h -1 | 4 |
| Heat carries oil/raw material weight ratio | 0.60 |
| Hydrogen/coker gasoline volume ratio | 400 |
| Pre-treatment average reaction temperature/DEG C | 230 |
| Hydrotreatment average reaction temperature/DEG C | 290 |
| Reaction pressure/MPa | 2.5 |
Comparative example 2
Adopt the technical process in method disclosed in prior art CN201010615240.4.Bad gasoline and thermal cycling oil are mixed into weighted BMO spaces reactor, again through with hydrotreatment after raw material heat exchange enter hydrotreating reactor, after hydrotreatment, mixture enters process furnace heating, again with pretreated raw material heat exchange, finally carry out product and thermal cycling oil separating again, output qualified product.
Stock oil is with embodiment 2, and a heat year oiliness lists in table 9, and catalyst property lists in table 10, and processing condition and test-results list in table 11 and table 12 respectively.
Table 9 heat carries oil nature.
| Turning oil title | Hydrofining vacuum distillate |
| Boiling range scope/DEG C | 390～550 |
| Sulphur content/μ gg -1 | <5 |
| Nitrogen content/μ gg -1 | <1 |
The main composition of table 10 catalyzer and character.
| Catalyzer | Pretreatment catalyst | Hydrogenation catalyst |
| Catalyzer forms | ||
| MoO 3+CoO/wt% | 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 |
| Turning oil consumption/raw material weight ratio | 0.25 |
| Hydrogen/coker gasoline volume ratio | 400 |
| Preatreating reactors average reaction temperature/DEG C | 170 |
| Hydrotreating reactor average reaction temperature ,/DEG C | 290 |
| Reaction pressure/MPa | 2.5 |
Table 12 product property and 3500 hours pressure drop ratios are comparatively.
| 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 |
As can be seen from the result of table 12, after the running of 3000 hours, adopt the processing technological flow of the method that the invention provides, quality product is better, device pressure drop is lower, simultaneously because preatreating reactors in the inventive method is ebullated bed reactor, can realize the online displacement after boiling-bed catalyst coking, can assurance device pressure drop in lower scope, better solving device problem of pressure drop.
Claims (11)
1. an inferior patrol hydrodesulfurizationprocess process, comprises following content:
(1) after bad gasoline mixes with hydrogen, after interchanger heat exchange, carry oil with the heat of circulation mix, then after process furnace heating, enter ebullated bed reactor from reactor lower part, carry out weighted BMO spaces reaction; The initial boiling point that described heat carries oil is higher 50 ~ 100 DEG C than doing of inferior patrol;
(2) step (1) gained reaction effluent enters gasoline hydrodesulfurizationmethod reactor, under hydrodesulfurization reaction condition, carry out selective hydrodesulfurization reaction;
(3) step (2) gained reaction effluent enters high-temperature low-pressure separator after interchanger, 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 uses through purifying treatment Posterior circle, obtains liquid after air lift as gasoline products or gasoline blending component;
(5) step (3) gained liquid carries oil as heat and returns step (1) and recycle.
2. in accordance with the method for claim 1, it is characterized in that, in step (1), after described bad gasoline mixes with hydrogen, first after interchanger and hydrodesulfurization reaction effluent carry out heat exchange, then carry oily mixing with the heat of circulation.
3. in accordance with the method for claim 1, it is characterized in that, the final boiling point that described heat carries oil is 300 ~ 600 DEG C.
4. in accordance with the method for claim 1, it is characterized in that, it is 20% ~ 150% of bad gasoline weight that the heat of described circulation carries oily consumption.
5. in accordance with the method for claim 1, it is characterized in that, the condition of the preatreating reactors described in step (1) is: reaction pressure is 1 ~ 6MPa; Pretreatment temperature is 180 DEG C ~ 350 DEG C; Hydrogen/bad gasoline volume ratio is 50 ~ 500, and volume space velocity is 0.5 ~ 10h
-1; The processing condition of the selective hydrodesulfurization reaction described in step (2) are: reaction pressure 1 ~ 6MPa, volume space velocity 1 ~ 10h
-1, temperature of reaction 230 ~ 360 DEG C, hydrogen/inferior patrol volume ratio is 100 ~ 1000.
6. in accordance with the method for claim 1, it is characterized in that, be filled with boiling-bed catalyst in ebullated bed reactor in step (1), described boiling-bed catalyst is spherical or bar shaped, and spherical diameter is 0.04 ~ 10mm; Bar shaped is length 2 ~ 10mm, and diameter is 1 ~ 6mm.
7. according to the method described in claim 1 or 6, it is characterized in that, described boiling-bed catalyst is one or more in no acidic or weakly acidic aluminum oxide, silicon oxide, amorphous silicon aluminium, titanium oxide and molecular sieve.
8. in accordance with the method for claim 1; it is characterized in that; fresh or regenerated catalyst, protective material or useless hydrogenation catalyst that described boiling-bed catalyst is is carrier with no acidic or weakly acidic porous oxide material; the hydrogenation active component of catalyzer is one or more in W, Mo, Ni and Co, with oxide basis hydrogenation active component content for 3wt% ~ 50wt%.
9. in accordance with the method for claim 1, it is characterized in that, described preatreating reactors by adding fresh boiling-bed catalyst in reactor head, and from the more serious boiling-bed catalyst of reactor discharge section incrustation coking, realizes the online displacement of catalyzer.
10. in accordance with the method for claim 1, it is characterized in that, in the inventive method, the catalyst for selectively hydrodesulfurizing of the gasoline hydrodesulfurizationmethod reactor charge described in step (2) with one or more in no acidic or weakly acidic aluminum oxide, silicon oxide, amorphous silicon aluminium, titanium oxide and molecular sieve for carrier, with one or more in W, Mo, Ni and Co for hydrogenation active component, with oxide basis hydrogenation active component content for 3wt% ~ 50wt%.
11. in accordance with the method for claim 1, it is characterized in that, the temperature of the high-temperature low-pressure separator described in step (3) controls at the final boiling point 10 ~ 50 DEG C higher than inferior patrol.
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| 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 |
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| 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 |
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| Edward Furimsky.沸腾床反应器.《重油转化催化剂》.2010, * |
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