CN103789007A - Wet starting method of hydrocracking unit - Google Patents
Wet starting method of hydrocracking unit Download PDFInfo
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- CN103789007A CN103789007A CN201210432669.9A CN201210432669A CN103789007A CN 103789007 A CN103789007 A CN 103789007A CN 201210432669 A CN201210432669 A CN 201210432669A CN 103789007 A CN103789007 A CN 103789007A
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Abstract
The invention relates to a wet starting method of a hydrocracking unit. A reaction zone of the hydrocracking unit is filled with a sulfurization type hydrogenation catalyst. The starting method comprises steps of heating starting oil through heat exchange to a certain temperature, passing the starting oil through a catalyst bed layer to raise the temperature of the catalyst bed layer to be 180+/-15 DEG C or higher by utilization of the heat of reactions during heat exchange and activation, blending a part of gas with a high olefin content into circulating gas, raising the temperature continuously to 230+/-15 DEG C by utilization of the heat of olefin hydrogenation reactions and activating at the constant temperature, introducing nitrogen-containing light distillate oil when the temperature is 245+/-15 DEG C, introducing nitrogen-containing heavy distillate oil instead when the temperature is 290+/-15 DEG C or higher, introducing raw oil instead step by step when the temperature is 320+/-15 DEG C, raising the temperature continuously by utilization of the heat of hydrogenation reactions of the raw oil, and finally adjusting the reaction temperature by the hydrogen cooling amount and a heat exchanger and shifting to normal production. Compared with the prior art, the starting method omits a heating furnace in the starting process of the hydrocracking unit and the starting process is smooth and steady.
Description
Technical field
The invention belongs to the working method of oil Refining Technologies, particularly relate to hydroeracking unit wet method start-up method.
Background technology
Along with environmental regulation increasingly stringent in global range, more and more to the demand of clean light clean fuel, hydrogen addition technology is the effective means of producing cleaning product, and therefore hydrogenation unit has become the standard configuration of refinery, and the hydrogenation unit in oil refining enterprise is on the increase.
Hydrocracking technology is the one in hydrogen addition technology, it is one of important means heavy distillate being processed as cleaning product, hydrocracking technology is generally take vacuum distillate or close distillate as raw material, produce high-quality petroleum naphtha, boat coal and diesel oil, hydrocracking tail oil is also steam cracking ethylene raw processed and the isomerization dewaxing Lube basic oil material feedstocks processed of high-quality simultaneously.The catalyzer that hydrocracking technology uses is dual-function catalyst, comprise cracking function and hydrogenating function, cracking function is provided by molecular sieve conventionally, and using is at present Y zeolite, Beta type molecular sieve, ZSM Series Molecules sieve, MCM Series Molecules sieve comparatively widely, and composite molecular screen etc.Its Hydrogenation comes from active metal, active metal is divided into two kinds of precious metal and base metals conventionally, most importantly base metal, mainly comprises VI B and VIII family metal (as Mo, W, Ni and Co etc.) element, and in commodity hydrogenation catalyst, these metals normally exist with the form of oxidation state.Because the Hydrogenation of oxidation state metal and atoms metal is lower, there is higher Hydrogenation just be only translated into sulphided state, therefore, in order to make the performance of hydrogenation catalyst reach best, need to vulcanize catalyzer before use.The prevulcanized of hydrogenation catalyst is divided in device two kinds of prevulcanizeds and the outer prevulcanized of device conventionally: in device, prevulcanized is hydrogenation catalyst is first loaded in hydrogenator, then adopt wet method or dry method to vulcanize, the outer prevulcanized of device refers to that catalyzer just carries out prevulcanized being loaded into before reactor, has two kinds of sulfide type and sulphided state.No matter use prevulcanized and the outer prevulcanized hydrogenation catalyst of device in device, hydrogenation unit can use liquid phase sulfuration (activation) start-up method.
Hydroeracking unit generally need to be at operation under comparatively high temps, in hydrogenation unit start-up process, device need to be raised to comparatively high temps (being generally more than 320 ℃) at normal temperatures, hydrogenation unit arranges process furnace conventionally, for providing heat in start up and production process.Hydrogenation reaction is generally strong exothermal reaction, in hydrogenation unit normal productive process, reactor outlet temperature, far above temperature in, now can realize the heating to reaction raw materials by heat exchange mode, if interchanger effect is enough, can in normal production, not use process furnace completely.But in start-up process, owing to not entering normal hydrogenation reaction, device heats up does not have origin of heat, adopts miscellaneous equipment generally cannot reach required temperature, and therefore start-up process need to arrange process furnace.Process furnace is the high-temperature high-pressure apparatus in hydrogenation unit, and facility investment is very large, and process furnace only uses in start-up process, and utilization ratio of device is low, and furnace tubing is one of important sources increasing high-pressure system Pressure Drop.
CN200910188142.4 discloses the vulcanizing agent supply method of catalyst wet sulfidation, and the method is mainly for liquid phase circulation hydrogenation unit start-up process, and start-up process must have process furnace.CN200510047487.X discloses a kind of FCC gasoline hydrodesulfurizationmethod and has fallen the start-up method of alkene technology, the main selectoforming of the method generates oil as vulcanized oil, the temperature rise of avoiding sulfidation to produce, and be only applicable to the gasoline hydrogenation device containing molecular sieve catalyst.
US 5688736 discloses a kind of catalyst vulcanization method, forbids to use the oil that goes into operation containing alkene in start-up process.CN200910188114.2, CN200910204266.7, CN200810010242.3, CN200810010245.7, CN200910204248.9, CN200910204249.3 disclose the start-up method that uses sulfide type catalyst hydrogenation unit, these methods all require to use the few activation oil of olefin(e) centent to go into operation in start-up process, and reactive system heats up needed heat all by providing with process furnace in catalyst activation process.The start-up method of CN 200910204283.0 Residue Hydrotreating Technology; the method discloses a kind of hydrogenation unit start-up method that contains the agent of partial vulcanization type hydrogenation protecting; start-up process needs additional vulcanizing agent catalyst oxidation type hydrogenation catalyst to carry out prevulcanized, and needs process furnace that heat is provided.
Go into operation for the hydroeracking unit that uses prevulcanized type catalyzer, topmost method is in the time of low temperature, to introduce the activation oil that goes into operation, by heating and heating up according to certain heat-up rate, until temperature substep swap-in stock oil while approaching the initial reaction temperature of stock oil, in start-up process, all need to provide with process furnace the heat of reactive system temperature-rise period, start-up process energy consumption is larger, cannot realize start-up process for the device that there is no process furnace, and use process furnace can increase considerably the Pressure Drop of system and energization consumption, in the time that temperature reaches certain temperature, to introduce in addition anhydrous liquid ammonia and carry out passivation, avoid the too high and raw hydrocracking reaction of the fry dried food ingredients that causes going into operation of hydrocracking catalyst initial activity, and raw material wet goods start-up process is steadily switched in realization.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of hydroeracking unit wet method start-up method, the implement device operation that steadily goes into operation under the prerequisite that does not use process furnace.
Hydroeracking unit wet method start-up method of the present invention comprises the steps:
(a) catalyzer that hydroeracking unit uses is selected sulfurized hydrogenation cracking catalyst;
(b) will go into operation after activation oil mixes with recycle hydrogen and introduce reactive system, and utilize low-temperature heat source that the activation oil that goes into operation is warmed up to the temperature that sulfide type catalyst priming reaction starts;
(c) stop using low-temperature heat source, the reaction heat that utilizes catalyst activation reaction to produce continues to be warmed up to 180 ± 15 ℃, then introduces the gas that is rich in alkene of suitable proportion;
(d) utilize the heat of olefin hydrogenation to continue to be warmed up to 230 ± 15 ℃, constant temperature is no less than 4 hours;
(e) while being warming up to 245 ± 15 ℃, introduce nitrogenous benzoline, while continuing to be warming up to 290 ± 15 ℃, nitrogenous benzoline is changed to nitrogenous heavy distillate;
(f) while continuing to be warming up to 320 ± 15 ℃ or higher temperature, the oil that goes into operation, the light ends oil that is rich in alkene and nitrogenous heavy distillate are replaced by stock oil gradually, the reaction heat that utilizes stock oil hydrogenating desulfurization, aromatic saturation to produce continues to heat up, while achieving the goal temperature adjust reaction zone temperature in by adjusting cold hydrogen amount and heat-exchange temperature, proceed to normal production operation.Described higher temperature is generally no more than 360 ℃.
In the inventive method step (a), said sulfurized hydrogenation catalyst, preferably take the sulfide type catalyst as vulcanizing agent containing elemental sulfur, sulfide type catalyst can adopt the prior art preparation of this area routine, or adopts commodity sulfide type catalyst.
In the inventive method step (a), said hydrogenation catalyst at least contains hydrocracking catalyst, and the molecular sieve type of this catalyzer mainly comprises that Y zeolite, Beta type molecular sieve, ZSM Series Molecules sieve, MCM Series Molecules sieve or complex type molecular sieve etc. are widely used in one or more in the molecular sieve of hydrogen addition technology.Hydrocracking catalyst can be prepared by the existing method in this area, also can commodity in use hydrocracking catalyst.Reaction mass, by before hydrocracking catalyst, generally need to pass through Hydrobon catalyst (or hydrotreating catalyst), carries out the reactions such as desulfurization removing nitric.
In the inventive method step (b), recycle hydrogen is the high pressure gas that are rich in hydrogen in start-up process, and hydrogen purity is not less than 50%(volume), be preferably not less than 60%(volume), be preferably not less than 70%(volume).
In the inventive method step (b), the activation oil that goes into operation using when hydrogenation unit goes into operation is the petroleum fractions that is rich in stable hydrocarbon, as straight run boat coal, straight-run diesel oil etc., also can be boat coal, the diesel oil obtaining through deep hydrofinishing, or boat coal, diesel oil etc. that hydrocracking obtains, the requirement nitrogen content in oil that goes into operation is not more than 200 μ g/g, is preferably not more than 100 μ g/g.Reactor inlet temperature when introducing goes into operation activation oil is 50 ℃～150 ℃.Start-up process carries out under hydrogen exists.In start-up process, hydrogen to oil volume ratio is generally 100:1～2000:1.In start-up process, when liquid, body air speed is generally 0.1～10h
-1.The activation oil that goes into operation partly or entirely recycles, and preferably adopts hot oiling mode, and the activation oil of going into operation of discharging from reactor carries out gas-liquid separation without cooling, and liquid phase circulation uses, and after gas phase is cooling, recycles through circulating hydrogen compressor.
In the inventive method step (b), low-temperature heat source is often referred to temperature lower than the thermal source of 240 ℃, preferably lower than the thermal source of 200 ℃, can be that the equipment such as the process furnace by interchanger, vapour generator, separation column obtain.Utilize low-temperature heat source that the oil that goes into operation is warmed up to the temperature that sulfide type catalyst priming reaction starts, refer to that sulfide type catalyst activates the beginning temperature of thermopositive reaction, is generally 130～170 ℃.
In the inventive method step (c), it is 5%～80% gas hydro carbons that the gas that is rich in alkene refers generally to contain monoolefine mass content, the gas that is rich in alkene obtaining for olefin hydrocarbon apparatus etc. as catalytic unit, ethylene unit, Methanol, or coke-oven gas etc., C generally contained
2~ C
4alkene.Entering the content requirement that should carry out purifying treatment before hydrogenation unit and reach foreign gas.At this temperature, the heat release of alkene generation hydrogenation reaction, lifting gear temperature, need to introduce the light ends oil of different ratios according to the speed heating up, in general, the introduction volume that is rich in olefin gas accounts for new hydrogen (being the hydrogen make-up of start-up process) the more than 20% of volume, is preferably 25%～90%.Olefin-containing gas introduction volume is generally 5～40 ℃ by controlling the first beds temperature in poor with last beds temperature out, is preferably 8～25 ℃.When olefin-containing gas introduction volume is large, exothermic heat of reaction is many, and reaction temperature rising is large, quick heating.
In the inventive method step (d), constant temperature time is preferably 6～12 hours.
In the inventive method step (e), said nitrogenous benzoline refers to do and is not more than 320 ℃, and be preferably not more than the distillate of 300 ℃, nitrogen content is not less than 200 μ g/g conventionally, is preferably not less than 400 μ g/g.Nitrogen content is not more than 1000 μ g/g conventionally, is preferably not more than 800 μ g/g.As the boat coal cut of straight run naphthenic base oil or solar oil cut, coking boat coal cut or solar oil cut, the light ends wet goods of coal tar light ends oil, coal direct liquefaction oil.
In the inventive method step (e), said nitrogenous heavy distillate refers to any distillate of cut scope in 220 ~ 400 ℃, the preferably any distillate in 230 ~ 380 ℃, nitrogen content is for being not less than 600 μ g/g, preferably be not less than 800 μ g/g, the nitrogen content upper limit can not need restriction, generally can be below 8000 μ g/g.Nitrogenous heavy distillate is as the diesel oil distillate of straight run naphthenic base oil, fraction of coker gas oil, the diesel oil distillate of coal tar, the diesel oil distillate wet goods of coal direct liquefaction oil.
In the inventive method step (e), nitrogenous benzoline accounts for 10%～50%, preferably 15%～35% of the activation weight of oil that goes into operation by weight.In start-up process, the weight of introducing nitrogenous benzoline accounts for 0.5% ~ 10% of hydrocracking catalyst gross weight in total nitrogen content in the nitrogenous benzoline of introducing.
In the inventive method step (e), nitrogenous heavy distillate accounts for 15%～80% of the activation weight of oil that goes into operation by weight, is preferably 20%～40%.In general the gross weight of, introducing nitrogenous heavy distillate is with the nitrogenous benzoline gross weight many 30% ~ 60% than introducing.
In the inventive method step (f), after sulfidation finishes, divide and progressively increase reactor feed Raw oil ratio example swap-in stock oil for 2～6 times, this process is well known to those skilled in the art.As specifically can be respectively according to 25% stock oil (be that 25 quality % are stock oil in charging, 75 quality % are the oil that goes into operation, lower with), 50% stock oil, 75% stock oil and 100% stock oil substep swap-in stock oil, when each stock oil of swap-in, general interval is more than 2 hours.Adjust the requirement that temperature of reaction reaches product, last swap-in 100% stock oil.For hydrocracking process, stock oil is generally heavy distillate, as poor-quality diesel-oil by cut fraction oil, and vacuum distillate, diasphaltene wet goods.Stock oil accounts for combined feed total feed quality more than 30%, is preferably 50% when above, stops passing into nitrogenous heavy distillate.
In the inventive method, the pressure of the reactivation process that goes into operation can be working pressure, also can be low compared with working pressure, be preferably 50%～100% of design operation pressure, and be preferably 75%～100% of design pressure.
The wet method of prior art hydrogenation unit goes into operation in sulfidation, and the heat that need to provide reaction bed temperature to improve with process furnace, also needs to use anhydrous liquid ammonia to carry out catalyst deactivation.The present invention is rich in alkene benzoline by the heat, the introducing that produce by low-temperature heat source, sulfide type catalyst reactivation process and reacts at a lower temperature the reaction heat obtaining, the next common finishing device start-up process of reaction heat that utilizes stock oil hydrogenation reaction to obtain under comparatively high temps, the process furnace that goes into operation be can not use, facility investment and process cost greatly reduced.Replace anhydrous liquid ammonia with nitrogenous distillate, while being low temperature, use nitrogenous benzoline, by there is absorption reaction, molecular sieve is carried out to passivation, hydrogenation reaction also occurs simultaneously and obtain further passivation of ammonia, and can carry out the thermal source that generator heats up because of hydrogenation reaction; When high temperature, introduce nitrogenous heavy distillate, in the time of nitride generation desorption in the benzoline of absorption, again increase the nitride that adsorptive power is stronger like this, thereby guarantee to keep molecular sieve initial activity further to suppress, and some nitride generation ammonia that reacts, strengthening suppresses the initial activity of molecular sieve.In the time that temperature exceedes certain and swap-in stock oil, utilize Hydrogenation and cracking performance by nitride and the ammonia desorption of absorption, when after swap-in stock oil, suppress the initial activity of hydrocracking catalyst by the nitrogen hydrogenation reaction generation ammonia improving in temperature and stock oil, thereby realize the smooth transition of start-up process.
Embodiment
Method of the present invention is specific as follows: straight-run diesel oil is for activating the oil that goes into operation, first in the time of low temperature, introduce the activation oil that goes into operation by the reaction zone of the sulfurized hydrogenation catalyst containing molecular sieve, then heat up by interchanger, in the time that temperature reaches 150 ℃, sulfide type catalyst reaction heat continues temperature to be raised to 175 ℃～185 ℃, introduction volume accounts for new hydrogen amount 70%(volume) the purifying and catalyzing gas (mixture of catalysis drying gas and liquefied gas, alkene volume content is more than 30%), then the reaction heat that utilizes hydrogenation of olefins to obtain heats up, in the time that temperature reaches 230 ℃, constant temperature activation 8 hours, then continue to be warming up to 240 ℃ of nitrogenous benzolines, continue to be warming up to 290 ℃ nitrogenous benzoline is changed to nitrogenous heavy distillate, continue to be warming up to 315 ℃, substep swap-in stock oil, utilize the reaction heat that in stock oil, hydrogenation reaction obtains that temperature in is raised to temperature of reaction, adjust operational condition and proceed to normal production.
Further illustrate particular case of the present invention below by embodiment.Catalyzer FF-46 is the hydrogenation pretreatment catalyst of China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute's development and production, catalyzer FC-50 and FC-32 are the hydrocracking catalyst of China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute's development and production, in FC-50 and FC-32 catalyzer, contain Y zeolite.
The chief component of table 1 gas
| Unstripped gas | Purifying and catalytic cracking gas |
| Composition, v% | |
| H 2 | 2.4 |
| C 2H 4 | 6.5 |
| C 3H 6 | 24.6 |
| H 2S | 2.0 |
| CO+CO 2 | <20μg/g |
Table 2 go into operation oil and stock oil main character
| Stock oil | Straight-run diesel oil | Nitrogenous benzoline | Nitrogenous heavy distillate | Iran VGO |
| Density (20 ℃)/gcm -3 | 0.846 | 0.786 | 0.867 | 0.914 |
| Boiling range/℃ | 170~350 | 180~245 | 230~360 | 350~545 |
| Sulphur content, wt% | 1.0 | 0.87 | 0.96 | 1.74 |
| Nitrogen content/μ gg -1 | 80 | 750 | 2100 | 1535 |
| Aromatic hydrocarbons, wt% | 20.1 | — | — | 43.8 |
| Alkene, wt% | — | — | — | — |
Table 3 embodiment processing condition and test-results
| Processing condition | Embodiment 1 | Reference example 1 | Embodiment 2 | Embodiment 3 |
| Catalyzer | FF-46/FC-32 | FF-46/FC-32 | FF-46/FC-32 | FF-46/FC-50 |
| Start-up method | Wet method | Wet method | Wet method | Wet method |
| Have or not the process furnace that goes into operation | Nothing | Have | Nothing | Nothing |
| Pressure/MPa | 15.0 | 15.0 | 12.0 | 17.0 |
| Introducing go into operation activation oil temperature/℃ | 80 | 80 | 70 | 90 |
| Introducing purifying and catalyzing gas temperature/℃ | 180 | — | 175 | 185 |
| Introduce nitrogenous benzoline (or anhydrous liquid ammonia) temperature/℃ | 240 | 240(liquefied ammonia) | 240 | 240 |
| Nitrogenous benzoline introduction volume (account for and activate the oil ratio example that goes into operation, %) | 20 | — | 25 | 15 |
| Change to nitrogenous heavy distillate temperature/℃ | 290 | — | 290 | 290 |
| Stop purifying and catalyzing gas temperature/℃ | 290 | — | 295 | 300 |
| Nitrogenous heavy distillate introduction volume (account for and activate the oil ratio example that goes into operation, %) | 20 | — | 35 | 15 |
| Change to stock oil temperature/℃ | 315 | 315 | 315 | 315 |
| Stop nitrogenous heavy distillate (or anhydrous liquid ammonia) temperature/℃ | 320 | 320(anhydrous liquid ammonia) | 315 | 310 |
| Catalyst activity appreciation condition and result | ||||
| Stock oil | Iran VGO | Iran VGO | Iran VGO | Iran VGO |
| Reaction pressure/MPa | 15.0 | 15.0 | 12.0 | 17.0 |
| Pretreatment section operational condition | ||||
| Catalyzer | FF-46 | FF-46 | FF-46 | FF-46 |
| Volume space velocity/h -1 | 0.9 | 0.9 | 1.1 | 1.5 |
| Hydrogen to oil volume ratio | 600 | 600 | 1000 | 1200 |
| Average reaction temperature/℃ | 368 | 368 | 375 | 380 |
| Generate oily nitrogen content/μ gg -1 | 3.2 | 3.4 | 7.5 | 10.0 |
| Cracking zone operational condition | ||||
| Catalyzer | FC-32 | FC-32 | FC-32 | FC-50 |
| Volume space velocity/h -1 | 1.5 | 1.5 | 1.2 | 2.0 |
| Hydrogen to oil volume ratio | 1000 | 1000 | 1200 | 800 |
| Average reaction temperature/℃ | 375 | 375 | 370 | 390 |
| Transformation efficiency, quality % | ~70 | ~70 | ~60 | ~73 |
Can be found out by embodiment, adopt the wet method start-up method of the inventive method, replace anhydrous liquid ammonia with nitrogenous distillate, not only can effectively bring into play the activity of catalyzer, and can under the prerequisite that there is no process furnace, realize and stablize start-up process.
Claims (23)
1. a hydroeracking unit wet method start-up method, is characterized in that comprising the steps:
(a) catalyzer that hydroeracking unit uses is selected sulfurized hydrogenation cracking catalyst;
(b) will go into operation after activation oil mixes with recycle hydrogen and introduce reactive system, and utilize low-temperature heat source that the activation oil that goes into operation is warmed up to the temperature that sulfide type catalyst priming reaction starts;
(c) stop using low-temperature heat source, the reaction heat that utilizes catalyst activation reaction to produce continues to be warmed up to 180 ± 15 ℃, then introduces the gas that is rich in alkene of suitable proportion;
(d) utilize the heat of olefin hydrogenation to continue to be warmed up to 230 ± 15 ℃, constant temperature is no less than 4 hours;
(e) while being warming up to 245 ± 15 ℃, introduce nitrogenous benzoline, while continuing to be warming up to 290 ± 15 ℃, nitrogenous benzoline is changed to nitrogenous heavy distillate;
(f) while continuing to be warming up to 320 ± 15 ℃ or higher temperature, the oil that goes into operation, the gas that is rich in alkene and nitrogenous heavy distillate are replaced by stock oil gradually, the reaction heat that utilizes stock oil hydrogenating desulfurization, aromatic saturation to produce continues to heat up, while achieving the goal temperature adjust reaction zone temperature in by adjusting cold hydrogen amount and heat-exchange temperature, proceed to normal production operation.
2. method according to claim 1, is characterized in that: in step (a), sulfurized hydrogenation catalyst is take the sulfide type catalyst as vulcanizing agent containing elemental sulfur.
3. method according to claim 1, it is characterized in that: in step (a), hydrogenation catalyst comprises hydrocracking catalyst, and its molecular sieve comprises one or more in Y zeolite, Beta type molecular sieve, ZSM Series Molecules sieve, MCM Series Molecules sieve etc. or complex type molecular sieve.
4. method according to claim 1, is characterized in that: in step (b), recycle hydrogen is the high pressure gas that are rich in hydrogen in start-up process, and hydrogen volume purity is not less than 50%, is preferably not less than 60%, is preferably not less than 70%.
5. method according to claim 1, it is characterized in that: in step (b), the activation oil that goes into operation using when hydrogenation unit goes into operation is the petroleum fractions that is rich in stable hydrocarbon, the requirement nitrogen content in oil that goes into operation is not more than 200 μ g/g, preferably be not more than 100 μ g/g, the reactor inlet temperature of introducing while going into operation activation oil is 50 ℃～150 ℃.
6. method according to claim 5, is characterized in that: the diesel oil that the activation oil of going into operation obtains for straight run boat coal, straight-run diesel oil, the boat coal obtaining through deep hydrofinishing, diesel oil that process deep hydrofinishing obtains, boat coal that hydrocracking obtains or hydrocracking.
7. want the method described in 1 according to right, it is characterized in that: start-up process carries out under hydrogen exists, and hydrogen to oil volume ratio is 100:1～2000:1, and in start-up process, when liquid, body air speed is 0.1～10h
-1.
8. method according to claim 1, is characterized in that: in step (b), low-temperature heat source refers to that temperature, lower than the thermal source of 240 ℃, preferably, lower than the thermal source of 200 ℃, obtains by the furnace apparatus of interchanger, vapour generator, separation column.
9. method according to claim 1, it is characterized in that: in step (b), utilize low-temperature heat source that the activation oil of going into operation is warmed up to the temperature that sulfide type catalyst priming reaction starts, thermopositive reaction while referring to that sulfide type catalyst activates, is generally 130～170 ℃.
10. according to the method for claim 1, it is characterized in that: in step (c), it is 5%～80% gas hydro carbons that the gas that is rich in alkene refers to contain monoolefine mass content.
11. methods according to claim 10, is characterized in that: the gas amount of quoting that is rich in alkene need to be determined according to the speed heating up.
12. according to the method described in claim 1 or 11, it is characterized in that: the introduction volume that is rich in olefin gas accounts for the more than 20% of new hydrogen volume amount, is preferably 25%～90%.
13. methods according to claim 12, is characterized in that: being rich in the introduction volume of olefin gas, is 5～40 ℃ by controlling the first beds temperature in poor with last beds temperature out, is preferably 8～25 ℃ of controls.
14. methods according to claim 1, is characterized in that: in step (e), nitrogenous benzoline refers to do and be not more than 320 ℃, and be preferably not more than the distillate of 300 ℃, nitrogen content is not less than 200 μ g/g conventionally, is preferably not less than 400 μ g/g.
15. according to the method described in claim 1 or 14, it is characterized in that: in step (e), nitrogenous benzoline nitrogen content is not more than 1000 μ g/g conventionally, is preferably not more than 800 μ g/g.
16. according to the method described in claim 1 or 14, it is characterized in that: in step (e), nitrogenous benzoline accounts for 10%～50%, preferably 15%～35% of the activation weight of oil that goes into operation by weight.
17. according to the method described in claim 1 or 14, it is characterized in that: in step (e), the weight of introducing nitrogenous benzoline accounts for 0.5% ~ 10% of sulfurized hydrogenation cracking catalyst gross weight in total nitrogen content in the nitrogenous benzoline of introducing.
18. methods according to claim 1, it is characterized in that: in step (e), nitrogenous heavy distillate refers to any distillate of cut scope in 220 ~ 400 ℃, preferably any distillate in 230 ~ 380 ℃, nitrogen content, for being not less than 600 μ g/g, is preferably not less than 800 μ g/g.
19. according to the method described in claim 1 or 17, it is characterized in that: in step (e), nitrogenous benzoline accounts for 10%～50%, preferably 15%～35% of the activation weight of oil that goes into operation by weight.
20. methods according to claim 18, is characterized in that: in step (e), introduce the gross weight of nitrogenous heavy distillate with the nitrogenous benzoline gross weight many 30% ~ 60% than introducing.
21. methods according to claim 1, is characterized in that: in step (f), after sulfidation finishes, divide and progressively increase reactor feed Raw oil ratio example swap-in stock oil for 2～6 times.
22. methods according to claim 1, is characterized in that: in step (f), temperature reaches 290 ± 15 ℃ or when above, stops injecting the light ends oil that is rich in alkene.
23. methods according to claim 1, is characterized in that: the pressure of reactivation process is working pressure, or low compared with working pressure, is preferably 50%～100% of design operation pressure, is preferably 75%～100% of design pressure.
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