CN104611026B - A kind of low energy consumption produces the two-segment hydrocracking method of high-quality industrial chemicals - Google Patents
A kind of low energy consumption produces the two-segment hydrocracking method of high-quality industrial chemicals Download PDFInfo
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Abstract
The invention discloses a kind of low energy consumption method for hydrogen cracking producing high-quality industrial chemicals.Raw oil and hydrogen, after twice heat exchange, pass sequentially through hydrofinishing and hydrocracking reaction district；Hydrocracking reaction district includes at least two hydrocracking catalyst, loaded upstream catalyst I, downstream loading catalyst II；Wherein catalyst I wt% Han modified Y molecular sieve 30～70, catalyst II wt% Han modified Y molecular sieve 15～50, the content of modified Y molecular sieve 10～30 percents high compared with catalyst II in catalyst I.High Temperature High Pressure countercurrent heat-transfer technology is organically combined by the method with hydrocracking catalyst grating technology, comprehensive utilization hydrocracking reaction heat, both the feature of two kinds of dissimilar hydrocracking catalysts had been given full play to, while keeping catalyst choice, improve purpose product quality, reduce again construction investment and operation energy consumption.
Description
Technical field
The present invention relates to a kind of method for hydrogen cracking, particularly relate to a kind of low energy consumption two-segment hydrocracking method that can produce high-quality industrial chemicals.
Background technology
Along with being continuously increased of distillate demand between city's field alignment, needing refinery to produce more intermediate oil, new fuel standard proposes tightened up requirement to the index of vapour, diesel oil.Obviously, time processing means and FCC technique can not meet the market index request to cleaning fuel.Hydrocracking process is not only the secondary operations means of heavy charge lighting, obtains a kind of important means of high-quality industrial chemicals especially from inferior raw material.
Hydrocracking unit one-time investment is bigger, and operating cost is the highest.Therefore, countries in the world Ge great research company all carries out substantial amounts of research positive for reducing the cost being hydrocracked, and makes great progress.In terms of catalyst: the emphasis that each big patent business in the world is all developed the update of catalyst as oneself technology, in recent years, constantly at the material of catalyst, the activity of catalyst, life-span, stability and reduce the aspects such as catalyst cost and done substantial amounts of work.At process aspect: distillate hydrocracking technology is the most ripe, and each major oil companies, while optimizing hydrocracking operation further, are placed on innovative point and are hydrocracked on relevant group technology, reducing cost by optimum organization technique；It addition, by the further investigation being hydrocracked, seek the internal relation between catalyst performance and feedstock property and purpose product quality, set up the emphasis that suitable catalyst grade part system is also this area research current.
Being hydrocracked genus strong exothermal reaction, the heat of hydrocracking unit is superfluous.So the size of reaction heating furnace design load, it is often depending on the heating demand required for presulfiding of catalyst when device goes into operation.In hydrogenation plant start-up process, needing device is raised to higher temperature (generally more than 300 DEG C) at normal temperatures, usual hydrogenation plant arranges heating furnace, goes into operation for device and provides heat in production process.
For using the hydrogenation plant of presulfurization hydrogenation catalyst to go into operation, topmost method is to introduce the activation oil that goes into operation when low temperature, by heating and heat up according to certain programming rate, until temperature is close to substep swap-in raw oil during the initial reaction temperature of raw oil, start-up process is required to use heating furnace to provide the heat of response system temperature-rise period, start-up process energy consumption is bigger, for not having the device of heating furnace cannot realize start-up process, additionally use heating furnace and can increase considerably the pressure drop of system and energization consumption.
United States Patent (USP) (US 4737167) discloses a kind of multiple single-stage hydrocracking technique, mainly first paragraph and realizes being totally converted of raw material, then the intermediate oil that first paragraph generates is entered second reaction zone and is hydrocracked the product that production fraction is lower further.Heavy raw oil is completely converted into the lightest product by it, and chemical hydrogen consumption is very big, and does not produce this high-quality ethylene cracking material of hydrocracking tail oil.
Chinese patent (CN 101173189) discloses a kind of method for hydrogen cracking producing industrial chemicals, its feature is that heavy raw oil enters one-stage hydrogenation treatment region after mixing with hydrogen, the hydrogen-rich gas of one section of effluent isolated is directly entered secondary hydrogenation cracking reaction district, liquid enters fractionating column and carries out fractional distillation, obtaining gas, Petroleum and tail oil and go out system as industrial chemicals, intermediate oil individually or is mixed into secondary hydrogenation treatment region with other inferior distillate oil and carries out cracking.Although the method can convert two or more inferior raw material, but is the increase in equipment investment simultaneously.
Chinese patent CN1955260A discloses a kind of method for hydrogen cracking, the method is by after the most hydrogenated to heavy distillate and poor quality catalytic cracking diesel refining, after obtained logistics mixing, enter hydrocracking reactor, the crackate of gained, after gas-liquid separation, is fractionated into obtaining light, heavy naphtha, boat coal, diesel oil and tail oil.The method can produce the latent heavy naphtha of high virtue and high-quality tail oil simultaneously, but technological process is more complicated than conventional hydrocracking technological process, and has limitation, define that in raw material, the density of poor quality catalytic cracking diesel is at more than 0.9g/mL, arene content is more than 60wt%, Cetane number < 30.
Summary of the invention
For the deficiencies in the prior art, the present invention provides a kind of low energy consumption to produce the two-segment hydrocracking method of high-quality industrial chemicals, High Temperature High Pressure countercurrent heat-transfer technology is organically combined by the method with hydrocracking catalyst grating technology, comprehensive utilization hydrocracking reaction heat, reduces construction investment and operation energy consumption.Cracking zone passes through the layering in the reactor of two kinds of dissimilar hydrocracking catalysts and loads, give full play to the feature of two kinds of dissimilar hydrocracking catalysts, the inventive method can improve purpose product quality while holding two-segment hydrocracking method is strong to adaptability to raw material further.
A kind of low energy consumption of the present invention produces the two-segment hydrocracking method of high-quality industrial chemicals and includes following content:
(1) after inferior feedstock oil and hydrogen mix, through overheated high score gas/cold mixing feed exchanger, reaction effluent/hot mixing feed exchanger, twice heat exchange heats up, again with or without rising to reaction temperature after reaction heating furnace, enter hydrofining reaction district, contact with Hydrobon catalyst and react；
(2) hydrofining reaction product enters separator and carries out gas-liquid separation, separated after obtain hydrogen-rich gas and fluid product；
(3) step (2) obtains fluid product entrance hydrocracking reaction district, carries out hydrocracking reaction；Step (2) obtains hydrogen-rich gas and can recycle through circulating hydrogen compressor after purified treatment；
(4) the hydrocracking reaction effluent obtained by step (3), carries out gas-liquid separation, and gas recycles, and liquid enters fractionating system, obtains hydrocracked product.
According to method for hydrogen cracking of the present invention, the inferior feedstock oil described in step (1) is the conventional hydrocracking raw material of this area.The boiling range of inferior feedstock oil is generally 350～620 DEG C, and nitrogen content is typically at more than 0.2wt%, and usually 0.2 ~ 0.3 wt%, sulfur content is the most unrestricted；Can also be nitrogen content at 0.08 more than wt%, generally 0.1 ~ 0.2 wt%, sulfur content is at below 0.1wt%, the low-sulfur high-nitrogen raw oil of generally 0.01 ~ 0.08 wt%.Described inferior feedstock oil is selected generally from the various coker gas oils (CGO) that processing middle-eastern crude obtains, such as one or several in Iran CGO, Saudi Arabia CGO etc., can also be to process the various coker gas oils (CGO) that Changqing Crude Oil obtains, it is also possible to be shale oil and the coal tar of corresponding fraction.
The routine operation that gas-liquid separation is those skilled in the art in the method for hydrogen cracking of the present invention, in step (2).
In described step (3), in hydrocracking reaction district, include at least two hydrocracking catalyst, i.e. hydrocracking catalyst I and hydrocracking catalyst II.According to the engagement sequence with reaction mass, the upstream catalyst bed filling hydrocracking catalyst I in hydrocracking reaction district, downstream catalyst bed filling hydrocracking catalyst II；Described hydrocracking catalyst I is with VI B race and/or VIII race's metal as active component, containing modified Y molecular sieve 30～70wt% in catalyst, it is preferably 45～60wt%, described hydrocracking catalyst II is equally with VI B race and/or VIII race's metal as active component, containing modified Y molecular sieve 15～50wt% in catalyst, preferably being preferably 30～40wt%, wherein the modified Y molecular sieve content in catalyst I exceeds 10～30 wt% compared with the modified Y molecular sieve content in catalyst II.
Hydrocracking catalyst I recited above and hydrocracking catalyst II are all with modified Y molecular sieve and aluminium oxide as carrier, or with modified Y molecular sieve, amorphous silica-alumina and aluminium oxide as carrier, with VI B race (such as tungsten, molybdenum) and/or VIII race (such as nickel, cobalt) metal as active metal component, catalyst can contain one or more in the elements such as some auxiliary agents such as phosphorus, titanium, zirconium, boron simultaneously.On the basis of the weight of catalyst, the content of VI B race and/or VIII race's active metal component generally 15 ~ 35 wt% in terms of oxide in hydrocracking catalyst.
According to the method for hydrogen cracking of present disclosure, in some detailed description of the invention, in hydrocracking catalyst I, the lattice constant of modified Y molecular sieve is generally 2.437～2.450nm；In hydrocracking catalyst II lattice constant of modified Y molecular sieve be generally 2.430～2.437nm, preferably 2.430 to less than 2.437nm(2.430～< 2.437nm).
In a more preferred embodiment, the SiO of modified Y molecular sieve in hydrocracking catalyst I2/Al2O3Mol ratio is general 5～25, and its relative crystallinity is generally 80～130%；The SiO of modified Y molecular sieve in hydrocracking catalyst II2/Al2O3Mol ratio is generally 5～70, and relative crystallinity is generally 90～130%.
Satisfactory hydrocracking catalyst I and hydrocracking catalyst II can select the commercial catalysts in this area, such as catalyst or the serial hydrocracking catalyst of Fushun Petrochemical Research Institute's development and production such as HC-14, HC-24, HC-29, HC-185, HC-190, HC-185LT, HC-175LT of Uop Inc.'s development and production.Satisfactory hydrocracking catalyst I can also be prepared voluntarily as required according to method well known in the art.Described hydrocracking catalyst II can be catalyst or its mixture such as HC-16, HC-26, HC-43, HC-53, HC-140LT, HC-150 of UOP development and production；The satisfactory hydrocracking catalyst of molecular sieve content II can also be prepared voluntarily as required according to the method that it is well known that.
According to the method for present disclosure, described hydrocracking reaction district should include at least two beds, generally includes 3～5 beds.Described hydrocracking catalyst I and hydrocracking catalyst II are seated at least two beds respectively.Wherein said two or more beds can be arranged in a reactor, or can be respectively arranged in two or more reactor.The admission space of wherein said hydrocracking catalyst I and hydrocracking catalyst II than generally 1:5～5:1, preferably 1:3～3:1.
In the method for hydrogen cracking of the present invention, the condition of the hydrofining reaction described in step (1) is generally: reactive hydrogen dividing potential drop 5.0～20.0MPa, average reaction temperature 280～427 DEG C, volume space velocity 0.1～10.0h-1, hydrogen to oil volume ratio 300～3000.
In the method for hydrogen cracking of the present invention, the operating condition in hydrocracking reaction district described in step (3) is generally, reactive hydrogen dividing potential drop 5.0～20.0MPa, average reaction temperature 280～427 DEG C, volume space velocity 0.1～10.0h-1, hydrogen to oil volume ratio 300～3000.The generally average reaction temperature of hydrocracking catalyst II is high compared with the average reaction temperature of hydrocracking catalyst I 3～20 DEG C, preferably 5～15 DEG C.
In the method for hydrogen cracking of the present invention, separation in step (4) and fractionation operation are the routine operation of those skilled in the art.Gas circulation in step (3) and step (4) can be circulated by after circulating hydrogen compressor respectively, it is also possible to shares a set of circulating hydrogen compressor system and is circulated.
Heat exchanger described in the inventive method, for High Temperature High Pressure countercurrent heat-transfer winding pipe heat exchanger, the existing various Patents technology in market can be chosen, as, the winding pipe heat exchanger CN 202902937U of Zhenhai Petrochemical Jianan Engineering Co., Ltd.'s exploitation, the full countercurrent heat-transfer of High Temperature High Pressure can be realized, there is the features such as heat transfer efficiency high (cold and hot end heat transfer temperature difference is little, generally 3 DEG C～8 DEG C), heat exchange area is big, use that number of units is few, manufacturing expense is low and floor space is little.
Reaction heating furnace described in the inventive method is served only for meeting device and goes into operation the intensification requirement of temperature-rise period low-temperature space, during normal operating, reaction heating furnace only puts altar lamp, design load is far below the popular response heating furnace of same device same treatment amount, generally the 20%～60% of the similar treating capacity of same device, construction investment and operation energy consumption are substantially reduced.
Compared with prior art, the method for hydrogen cracking of the present invention has the following characteristics that
1, the present invention is on the basis of existing hydrocracking process technology, High Temperature High Pressure countercurrent heat-transfer technology is organically combined with hydrocracking catalyst grating, technique and engineering height set, innovate supporting start-up method, develop normal operating flames of anger reaction heating furnace is hydrocracked complete technology, scientific and reasonable make use of hydrogenation reaction heat, decreases construction investment, reduces fuel consumption.
2, in the inventive method, use two-stage reforming technological process, widen the scope of raw oil, reduce the impurity such as the ammonia impact on hydrocracking catalyst generated in inferior feedstock oil preprocessing process to greatest extent, improve the hydrogen dividing potential drop in hydrocracking reaction district, can farthest play the performance of hydrocracking catalyst.
3, in the inventive method, modified Y molecular sieve that two kinds of hydrocracking catalysts that hydrocracking reaction district selects contain different content, that particularly have different lattice constant is as cracking active component.Two kinds of catalyst examples the most according to a certain volume are loaded.The hydrocracking catalyst I of upstream mates properly with hydrogenation center containing higher molecular sieve content, acid centre, has good heavy naphtha selectivity；The hydrocracking catalyst II in downstream has stronger aromatic hydrocarbons conversion capability simultaneously, aromatic hydrocarbons in heavy constituent in raw oil can be converted into less molecular distribution in heavy naphtha fraction, the hydrocracking catalyst synergism of two kinds of different molecular sieve content, significantly improve the quality of hydrocracked product, the virtue in particular improving heavy naphtha is dived, and reduces the BMCI value of tail oil.
4, in prior art, hydrocracking reaction district uses traditional Catalyst packing method, when only making a kind of hydrocracking catalyst, exothermic heat of reaction amount is relatively big, when hydrocracking unit operates, needs to take away the reaction temperature rising of 24～40 DEG C with cold hydrogen, and the method using the present invention, by the filling order of reasonable arrangement catalyst, in addition to can greatly improving product quality, additionally it is possible to the exothermic heat of reaction of scientific utilization upper bed layer, between bed can not liquid hydrogen injection, or few liquid hydrogen injection.Quenching hydrogen consumption and the hydrocracking unit accident cold hydrogen reserve level (typically can reduce by 30～70 %) of cracker can be greatly reduced, play effect that is the most energy-conservation and that reduce operating cost.
5, it is distributed due to whole reactor reaction temperature show an ascending trend, reactor outlet temperature is made relatively to improve, improve the temperature of heat exchanger thermal source, and the inventive method selects the High Temperature High Pressure adverse current winding pipe heat exchanger that heat transfer efficiency is high, energy can obtain more reasonably comprehensively utilizing, the reaction heating furnace normal operating flames of anger can be realized, greatly reduce fuel consumption.
Accompanying drawing explanation
Fig. 1 is a kind of principle process flow diagram of the inventive method.
Detailed description of the invention
Below in conjunction with the accompanying drawings the method for the present invention is described in detail.
As shown in Figure 1, the technological process of the two-segment hydrocracking method that a kind of low energy consumption of the present invention produces high-quality industrial chemicals is as follows: inferior feedstock oil mixes with hydrogen, through overheated high score gas/cold mixing feed exchanger 1, reaction effluent/hot mixing feed exchanger 2, twice heat exchange heats up, the most reacted heating furnace 3 rises to reaction temperature, enters hydrofining reaction district 4 and carries out hydrofining reaction.Refining reaction product enters separator 5 and carries out gas-liquid separation, and separator 5 generally includes high-pressure separator and low pressure separator.nullSeparator 5 obtains gas purification Posterior circle and uses，The liquid obtained enters hydrocracking reaction district 6，Successively with hydrocracking catalyst I 7 and hydrocracking catalyst II bed 8 haptoreaction，After reaction effluent oil feeds reacted effluent/hot mixing feed exchanger 2 heat exchange with hot mixing，Enter high pressure hot separator 9，High pressure hot separator 9 top hot high score gas out is after hot high score gas/cold mixing feed exchanger 1 heat exchange，Cold high pressure separator 10 is entered again after air cooler cools down，Hot high score gas carries out oil in cold high pressure separator 10、Water、Gas three phase separation，Gas recycles through circulating hydrogen compressor 11 after treatment，Bottom high pressure hot separator 9, hot high score oil out enters thermal low-pressure separators 12 flash distillation，Low point of gas of heat is mixed into cold low separator 13 flash distillation with cold high score oil after cooling，Cold low point of oil and low point of oil of heat are mixed into fractionating system 14，Through fractional distillation acquisition corresponding product: gas 15、Petroleum 16、Jet fuel 17、Diesel oil 18 and hydrogenation tail oil 19.
The two-segment hydrocracking method a kind of low energy consumption of the present invention being produced high-quality industrial chemicals followed by specific embodiment is further described.
Embodiment 1-3
Use the process chart shown in Fig. 1.Selection FF-46 pretreating catalyst by hydrocracking is equipped with the catalyst system of the hydrocracking catalyst I/hydrocracking catalyst II of different volumes ratio.In embodiment 1-3, the volume ratio of hydrocracking catalyst I/hydrocracking catalyst II is respectively 3:2,1:1 and 2:3.
At reaction stagnation pressure 15.7MPa, refining stage and cracking zone hydrogen to oil volume ratio are respectively 900:1 and 1200:1, refining stage and cracking zone volume space velocity and are respectively 1.0h-1And 1.5h-1, controlling refined oil nitrogen content is 5～8 μ g × g-1, carried out 350 DEG C of conversion ratios of ＞ and be about the engineer testing of 75wt%, wherein controlled to keep 8 DEG C of temperature difference between hydrocracking catalyst I and hydrocracking catalyst II bed, investigated the product quality of each fraction.
Comparative example 1
Technological process is with embodiment 1-3, and raw oil is with embodiment 1-3.Select the catalyst system of FF-46 pretreating catalyst by hydrocracking and hydrocracking catalyst I.At reaction stagnation pressure 15.7MPa, refining stage and cracking zone hydrogen to oil volume ratio are respectively 900:1 and 1200:1, refining stage and cracking zone volume space velocity and are respectively 1.0h-1And 1.5h-1, controlling refined oil nitrogen content is 5～8 μ g × g-1, carried out 350 DEG C of conversion ratios of ＞ and be about the engineer testing of 75wt%, investigated the product quality of each fraction.
Table 1 raw oil main character.
| Source | Wax oil |
| Density (20 DEG C)/g cm-3 | 0.8942 |
| Boiling range scope/DEG C | 252～567 |
| Sulfur/μ g g-1 | 1600 |
| Nitrogen/μ g g-1 | 2200 |
Table 2 catalyst main character.
| Catalyst | FF-46 | Hydrocracking catalyst I | Hydrocracking catalyst II |
| Face shaping | SANYE swath | Cylindrical bars | Cylindrical bars |
| Particle diameter, mm | 1.1~1.3 | 1.5～1.7 | 1.5～1.7 |
| Bar is long, mm | 3~8 | 3~8 | 3~8 |
| Modified Y molecular sieve content, wt% | — | 45 | 35 |
| Lattice constant, nm | — | 2.448 | 2.440 |
| SiO2/Al2O3Mol ratio | — | 8 | 14 |
| Relative crystallinity * | — | 95 | 105 |
| Chemical composition, m%: | |||
| NiO | 4.0 | 5.0 | 6.5 |
| MoO3 | 24.0 | 15.0 | — |
| WO3 | — | — | 19.0 |
* relative crystallinity: Xc=Wc (Wc+Wa), in formula, Wc and Wa is respectively the percetage by weight shared by crystalline portion and non-crystallized part.
Table 3 technological condition.
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative example 1 | |
| Reactive hydrogen dividing potential drop, MPa | 15.7 | 15.7 | 15.7 | 15.7 |
| Reaction temperature/DEG C | 380/373/381 | 380/374/382 | 380/375/383 | 380/380 |
| Volume space velocity, h-1 | 1.0/1.5 | 1.0/1.5 | 1.0/1.5 | 1.0/1.5 |
| Hydrogen to oil volume ratio, v/v | 900:1/1200:1 | 900:1/1200:1 | 900:1/1200:1 | 900:1/1200:1 |
| 350 DEG C of conversion ratios of ＞, wt% | ~78 | ~78 | ~78 | ~78 |
The distribution of table 4 hydrocracked product and major product quality
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Comparative example 1 | |
| Heavy naphtha | ||||
| Yield, % | 37.41 | 37.12 | 36.67 | 36.27 |
| Boiling range/DEG C | 67～185 | 66～186 | 67～185 | 68～172 |
| Virtue is latent, % | 63.32 | 64.53 | 67.23 | 56.14 |
| Boat coal | ||||
| Yield, % | 19.05 | 19.57 | 20.69 | 19.05 |
| Boiling range/DEG C | 186～247 | 185～248 | 187～249 | 186～248 |
| Smoke point/mm | 23 | 22 | 22 | 23 |
| Diesel oil | ||||
| Yield, % | 10.45 | 11.19 | 11.56 | 10.57 |
| Boiling range/DEG C | 267～331 | 272～330 | 271～331 | 269～325 |
| Condensation point/DEG C | -14 | -13 | -12 | -17 |
| Cetane lndex | 72.3 | 71.8 | 69.4 | 71.1 |
| Tail oil | ||||
| Yield, % | 24.87 | 24.94 | 25.34 | 24.37 |
| Boiling range/DEG C | 361～535 | 362～535 | 363～538 | 365～527 |
| Condensation point/DEG C | 34 | 34 | 34 | 34 |
| BMCI value | 9.2 | 8.1 | 6.4 | 13.7 |
Claims (11)
1. low energy consumption produces a two-segment hydrocracking method for high-quality industrial chemicals, including following content:
(1) after inferior feedstock oil and hydrogen mix, through overheated high score gas/cold mixing feed exchanger, reaction effluent/hot mixing feed exchanger, twice heat exchange heats up, reaction temperature is risen to again with or without reaction heating furnace, enter hydrofining reaction district, contact with Hydrobon catalyst and react；
(2) hydrofining reaction product enters separator and carries out gas-liquid separation, separated after obtain hydrogen-rich gas and fluid product；
(3) step (2) obtains fluid product entrance hydrocracking reaction district, carries out hydrocracking reaction；Step (2) obtains hydrogen-rich gas and recycles through circulating hydrogen compressor after purified treatment；Two kinds of hydrocracking catalysts are included, according to the engagement sequence with reaction mass, upstream catalyst bed filling hydrocracking catalyst I, downstream catalyst bed filling hydrocracking catalyst II in hydrocracking reaction district；The admission space of hydrocracking catalyst I and hydrocracking catalyst II is than for 1:5～5:1；Described hydrocracking catalyst I is with VI B race and/or VIII race's metal as active component, and containing modified Y molecular sieve 30～70wt% in catalyst, the lattice constant of modified Y molecular sieve is 2.437～2.450nm；Described hydrocracking catalyst II is with VI B race and/or VIII race's metal as active component, and containing modified Y molecular sieve 15～50wt% in catalyst, the lattice constant of modified Y molecular sieve is 2.430 to less than 2.437nm；Wherein the modified Y molecular sieve content in catalyst I exceeds 10～30 percentage points compared with the modified Y molecular sieve content in catalyst II；
(4) the hydrocracking reaction effluent obtained by step (3), carries out gas-liquid separation, and gas recycles, and liquid enters fractionating system, obtains hydrocracked product；
Wherein, the boiling range of described inferior feedstock oil is 350～620 DEG C；Nitrogen content is at more than 0.2wt%, or nitrogen content is at more than 0.08wt%, and sulfur content is at below 0.1wt% simultaneously.
The most in accordance with the method for claim 1, it is characterised in that described hydrocracking catalyst I is containing modified Y molecular sieve 45～60wt%.
The most in accordance with the method for claim 1, it is characterised in that described hydrocracking catalyst II is containing modified Y molecular sieve 30～40wt%.
The most in accordance with the method for claim 1, it is characterised in that on the basis of the weight of catalyst, in hydrocracking catalyst I and II, the content of VI B race and/or VIII race's active metal component is calculated as 15 ~ 35 wt% with oxide.
The most in accordance with the method for claim 1, it is characterised in that the SiO of modified Y molecular sieve in hydrocracking catalyst I2/Al2O3Mol ratio is 5～25, and its relative crystallinity is 80～130%；The SiO of modified Y molecular sieve in hydrocracking catalyst II2/Al2O3Mol ratio is 5～70, and relative crystallinity is 90～130%.
The most in accordance with the method for claim 1, it is characterised in that the condition of the hydrofining reaction described in step (1) is: reactive hydrogen dividing potential drop 5.0～20.0MPa, average reaction temperature 280～427 DEG C, volume space velocity 0.1～10.0h-1, hydrogen to oil volume ratio 300～3000.
The most in accordance with the method for claim 1, it is characterised in that described in step (3), the operating condition in hydrocracking reaction district is, reactive hydrogen dividing potential drop 5.0～20.0MPa, average reaction temperature 280～427 DEG C, volume space velocity 0.1～10.0h-1, hydrogen to oil volume ratio 300～3000.
The most in accordance with the method for claim 7, it is characterised in that the average reaction temperature of hydrocracking catalyst II is high compared with the average reaction temperature of hydrocracking catalyst I 3～20 DEG C.
The most in accordance with the method for claim 1, it is characterised in that described hot high score gas/cold mixing feed exchanger, reaction effluent/hot mixing feed exchanger are High Temperature High Pressure countercurrent heat-transfer winding pipe heat exchanger.
The most in accordance with the method for claim 1, it is characterised in that the admission space of described hydrocracking catalyst I and hydrocracking catalyst II is than for 1:3～3:1.
11. in accordance with the method for claim 9, it is characterised in that the average reaction temperature of hydrocracking catalyst II is high compared with the average reaction temperature of hydrocracking catalyst I 5～15 DEG C.
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| CN104611026A (en) | 2015-05-13 |
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