CN109988636A - Flexible single-stage hydrocracking technique - Google Patents

Abstract

The invention discloses a kind of flexible single-stage hydrocracking techniques.Wax oil raw material enters single-stage hydrocracking reactor after mixing with hydrogen, is divided into two strands by the material after the Catalyst For Single-stage Hydrocracking bed of top；One material obtains liquid through gas-liquid separator separates among bed, and extracts hydrocracking reactor out and enter the progress isocraking of hydroisomerizing cracker with hydrogen and react；Another strand of material is gas-liquid mixed logistics, and mixture flow continues to flow downwardly through the Catalyst For Single-stage Hydrocracking bed of lower part；Single-stage hydrocracking reaction mass and hydroisomerizing cracking reaction material carry out gas-liquid separation and fractionation respectively, obtain different size naphtha, boat coal, diesel oil and tail oil product.The present invention provides a kind of on a set of hydrogenation plant while producing the single-stage hydrocracking technique of two or more different size fraction oil products, heat entrained by partial cracking material can be made full use of, realizes the coupling operation of single-stage hydrocracking reactor and hydroisomerizing cracker.

Description

Flexible single-stage hydrocracking technique

Technical field

The invention belongs to petroleum refining fields, and in particular to one kind flexibly produce high-quality naphtha of different nature, boat coal, The single-stage hydrocracking technique of diesel oil, tail oil product.

Background technique

Hydrogen addition technology is the important manufacturing process of light materialization of heavy oil and light-end products quality upgrading.Hydrocracking technology because Feedstock oil is adaptable, product flexibility is good, liquid product yield is high, high quality has obtained faster development. Existing hydrocracking technology can be divided into three kinds according to processing flow: one-stage serial hydrocracking process flow, single hop add hydrogen Process process and two-stage reforming process flow.According to tail oil, whether circulate operation can be divided into three kinds: one way is primary Pass through process flow, part circulation technology process and complete alternation process flow.The wherein catalysis that single-stage hydrocracking technology uses Agent is mainly a type of Catalyst For Single-stage Hydrocracking, and usage quantity usually accounts for 80% or more of total catalyst volume, urges The Cracking Component of agent is mainly amorphous silica-alumina, can also contain a small amount of Y type molecular sieve, beta molecular sieve, SAPO Series Molecules Sieve and ZSM-5 molecular sieve etc..It is hydrocracked a group timesharing using different type, obtained light-end products composition and property have larger Difference, the composition and property of tail oil also have biggish difference.

CN100569921C discloses a kind of single-stage hydrocracking process, and this method is pre- for prepared using body phase method plus hydrogen Handle the single-stage hydrocracking technique of catalyst；CN001075550C discloses a kind of single-stage hydrocracking process, and this method is Use the single-stage hydrocracking technique containing Y type molecular sieve Catalyst For Single-stage Hydrocracking；CN001415707A discloses one kind It is raised productivity and improved the quality the method for diesel oil by distillate, this method adds hydrogen containing isomery performance in the filling of original hydrocracking catalyst rear portion Cracking catalyst with achieve the purpose that reduce hydrocracked product condensation point, but above-mentioned these be hydrocracked it is obtained each The product of fraction only has a kind of specification.

CN001566283A, CN001766051A and CN101402048A etc. disclose a kind of middle oil type hydrocracking and urge Agent and preparation method thereof is prepared for urging in the single-stage hydrocracking that amorphous silicon aluminium and a small amount of Y type molecular sieve are acid centre Agent；CN001712498A discloses a kind of hydrogenation catalyst and preparation method thereof of maximum diesel oil yield, the catalyst with Amorphous silicon aluminium and modified beta molecular sieve are main cracking center, but are hydrocracked skill using these hydrocracking catalysts The product of each obtained fraction of art only has a kind of specification.

CN103394368B discloses a kind of light oil type hydrogen cracking catalyst and preparation method thereof containing composite molecular screen And application, CN103551186B disclose a kind of middle oil type hydrocracking catalyst containing composite molecular screen and preparation method thereof and Using US6670295 and US4837396A disclose a kind of preparation of complex type molecular sieve catalysis.Such technology can be with wax Oil is feedstock oil, by using containing Y type molecular sieve and heterogeneous types molecular sieve complex type molecular sieve hydrocracking catalyst Method for hydrogen cracking produces various high-quality hydrocracked products, but the product of each fraction only has a kind of specification, Er Qieji All in one-stage serial hydrocracking or hydrogenation modifying process in sheet.

In conclusion the existing hydrocracking technology using several different type cracking center catalyst of comparison, uses Amorphous silicon aluminium Catalyst For Single-stage Hydrocracking or amorphous silicon aluminium-Y type molecular sieve Catalyst For Single-stage Hydrocracking single hop Hydrocracking technology, obtained boat product of coal freezing point is relatively high, smoke point is relatively low, and diesel product Cetane number is high, but It is that condensation point is relatively high, tail oil product condensation point is very high, and typically larger than 30 DEG C；It is catalyzed using heterogeneous types molecular sieve hydrocracking The single-stage hydrocracking technology of agent, obtained boat coal smoke point is relatively high, and diesel product sulfur content is low, and condensation point is low, and tail oil is close Spend relatively large, but isomery hydrocarbon content is high, and condensation point is very low, usually less than 0 DEG C.Above-mentioned single-stage hydrocracking technology, The hydrocracking tail oil differentiation of product produced in identical conversion ratio is larger, wherein using the tail oil of Y zeolite catalyst It is the raw material of fine quality catalytic cracking raw material, preparing ethylene by steam cracking, the tail oil using heterogeneous types molecular sieve catalyst is can be with Directly produce High Quality Lube Base Oils or the raw material as High Quality Lube Base Oils.Therefore be used alone it is above-mentioned it is several plus When hydrogen process, different types of Catalyst For Single-stage Hydrocracking can only be selected as needed, or use two kinds of molecular sieves Composite catalyst, or two kinds of hydrocracking catalyst gradations is selected to use, but these techniques can only produce a kind of property Tail oil product, i.e. operating flexibility compares poor.

Summary of the invention

In view of the deficiencies of the prior art, the present invention provides a kind of flexible single-stage hydrocracking technique, i.e., by from using list Extraction section reaction stream in the middle part of the single-stage hydrocracking reactor of section hydrocracking catalyst, the wax oil feedstock oil is led to Cross Catalyst For Single-stage Hydrocracking be hydrocracked it is flexible with heterogeneous types hydrocracking catalyst hydroisomerizing cracking combined method The hydrocracking tail oil product of a variety of high quality, the naphtha product of plurality of specifications and the high-quality automotive fuel of plurality of specifications is produced to produce Product.

The method of flexible single-stage hydrocracking technique of the invention, includes the following steps:

A, wax oil feedstock oil adds hydrogen to split under the conditions of single-stage hydrocracking by single-stage hydrocracking reactor top single hop first Change catalyst bed, obtains the first single-stage hydrocracking logistics, this part reaction stream is divided into two parts, and a portion passes through Gas-liquid separator, separating obtained liquid stream extract single-stage hydrocracking reactor out；

B, the first single-stage hydrocracking logistics continuation of remainder adds hydrogen to split under hydrocracking condition by single hop in step a Change the lower part Catalyst For Single-stage Hydrocracking bed of reactor, single-stage hydrocracking logistics separated, is fractionated to obtain single hop and is added hydrogen Cracking high pressure hydrogen-rich gas, single-stage hydrocracking gas products, single-stage hydrocracking naphtha product, single-stage hydrocracking boat coal Product, single-stage hydrocracking diesel product and single-stage hydrocracking tail oil product；

C, first of extraction device obtained by step a is hydrocracked after liquid stream is mixed with recycle hydrogen splits in single hop hydroisomerizing It is split under the conditions of change by the single hop hydroisomerizing containing heterogeneous types molecular sieve catalyst of single hop hydroisomerizing cracker Change catalyst bed, single hop hydroisomerizing cracked-stream separated, be fractionated to obtain single hop hydroisomerizing cracking high pressure hydrogen-rich gas, Single hop hydroisomerizing cracked gas product, single hop hydroisomerizing cracked naphtha product, single hop hydroisomerizing cracking boat product of coal, Single hop hydroisomerizing cracked diesel oil product and single hop hydroisomerizing cracking tail oil product.

Hydrocracking process according to the present invention, wherein can also include step d: the single-stage hydrocracking that step b is obtained It is recycled after the single hop hydroisomerizing cracking high pressure hydrogen-rich gas mixing that high pressure hydrogen-rich gas and step c are obtained.

The impurity such as S, N, O in wax oil feedstock oil are effectively removed when passing through Catalyst For Single-stage Hydrocracking, aromatic hydrocarbons one Determine to obtain in degree plus hydrogen saturation, cyclic hydrocarbon generating unit divide ring-opening reaction, macromolecular is cracked into small molecule, a portion single hop It is hydrocracked logistics and continues single-stage hydrocracking, available normal hydrocarbon content is higher, the lower boat coal of arene content produces Product, diesel product and tail oil product；A part the first single-stage hydrocracking liquid stream of extraction passes through containing heterogeneous types point Continue isomery after the hydroisomerizing Cracking catalyst of sub- sieve catalyst to be hydrocracked, because heterogeneous types molecular sieve is with different The characteristics of structure and cracking, the isocraking product of available high isomery hydrocarbon content, the condensation point of especially diesel product is low, tail oil produces The condensation point of product is low, and viscosity index (VI) is high.

Compared with prior art, the advantages of present invention flexible single-stage hydrocracking technique, is:

It 1, include at least two Catalyst For Single-stage Hydrocracking beds in single-stage hydrocracking reactor in the present invention.By setting Set the gas-liquid separator among single-stage hydrocracking reactor bed by a portion cracked liquid material extraction step, i.e., Effective distribution to single-stage hydrocracking material stock can be achieved, then obtained material is made to pass through different hydrocracking process, So as to flexibly produce the purpose product of different size, especially tail oil product.Meanwhile it being extracted among reactor bed anti- Answering logistics is technically also to be easily achieved.And in the prior art, although by adjusting conversion ratio and adjusting evaporating for product The available a variety of light-end products of journey, but due to only one single-stage hydrocracking reactor outlet, a set of single hop adds The same fraction range of hydrogen cracking unit is typically only capable to obtain a type of light naphtha product, heavy naphtha product, boat coal production Product, diesel product and tail oil product；If it is intended to obtaining the hydrocracked product of different size, two sets or more of single hop is needed to add Hydrogen cracking unit.Therefore, the present invention provides one kind on a set of single-stage hydrocracking process unit for the first time while producing two kinds Above with fraction range, product of coal, two or more different sizes but different size tail oil product, two or more different sizes navigate The single-stage hydrocracking technique of diesel product and a variety of different size naphtha products.

2, the present invention among the catalyst bed of hydrocracking reactor by being arranged gas-liquid separator, by wax oil raw material Extract reactor by the first single-stage hydrocracking liquid phase stream of single-stage hydrocracking, and be sent to be separately provided plus Hydrogen isocraking reactor carries out hydroisomerizing cracking reaction, the condensation point for being hydrocracked rear material is further decreased, to make Different arene contents, the naphtha product of different isomerization hydrocarbon content, boat product of coal, bavin can flexibly be produced by obtaining method of the invention Oil product and tail oil product.

3, in the present invention, in the product that two reactor streams are fractionated, by containing Catalyst For Single-stage Hydrocracking Or the heavy naphtha virtue obtained after being hydrocracked containing a small amount of Y type molecular sieve hydrocracking catalyst dive it is relatively high, boat coal produce Product smoke point is relatively high, and diesel product Cetane number is relatively high, and tail oil product paraffinicity is high, BMCI value is relatively low； It is hydrocracked by part containing Catalyst For Single-stage Hydrocracking, containing after the hydroisomerizing cracking of heterogeneous types molecular sieve catalyst Obtained naphtha isomery hydrocarbon content is high, boat product of coal freezing point is low, and diesel product condensation point is low, tail oil product hydrocarbon isomer content height, Viscosity index (VI) is big, condensation point is low；Naphtha, boat product of coal, diesel product and the tail oil that production different size can be met respectively produce The needs of product.

4, in the present invention, the impurity such as S, N in feedstock oil are converted into H after weighted BMO spaces and partial hydrogenation cracking₂S And NH₃, the major part H after gas-liquid separator separates₂S and NH₃It is present in gas phase, and H in liquid phase₂S and NH₃Content it is less, To reduce the inhibiting effect to hydroisomerizing Cracking catalyst molecular sieve, so that the reaction of hydroisomerizing Cracking catalyst is living Property improve, that is, reaching required reaction temperature when same reaction effect reduces, and single-stage hydrocracking reactor adds hydrogen to split Changing obtained liquid itself among catalyst bed has very high temperature and pressure, with the mixed temperature of recycle hydrogen although It slightly reduces, but still can be directly entered and reaction effect is reacted and reached in newly-installed hydroisomerizing cracker Fruit realizes that hydroisomerizing cracker and single hop add hydrogen to make full use of heat entrained by this thigh division compound material The coupling operation of cracker.

Detailed description of the invention

Fig. 1 is principle process schematic diagram of the invention.

Wherein: 1- feedstock oil, 2- hydrocracking reactor, 3- are hydrocracked logistics, 4- hydroisomerizing cracked stock logistics, 5- hydroisomerizing cracker, 6- are hydrocracked high-pressure separator hydrogen-rich gas, and 7- hydroisomerizing cracking high-pressure separator is rich Hydrogen, 8- are hydrocracked high-pressure separator, 9- hydroisomerizing cracking high-pressure separator, and 10- is hydrocracked fractionating column, and 11- adds Hydrogen isocraking fractionating column, 12- are hydrocracked light naphtha product, and 13- is hydrocracked heavy naphtha product, and 14- is hydrocracked Navigate product of coal, and 15- is hydrocracked diesel product, 16- hydrocracking tail oil product, 17- hydroisomerizing cracking light naphtha product, 18- hydroisomerizing cracking heavy naphtha product, 19- hydroisomerizing cracking boat product of coal, 20- hydroisomerizing cracked diesel oil product, 21- hydroisomerizing cracking tail oil product, 22- supplement hydrogen, 23- gas-liquid separator, 24- hydroisomerizing cracking recycle hydrogen, 25- add hydrogen Cracking recycle hydrogen.

Specific embodiment

The initial boiling point of wax oil raw material described in step a is 100~400 DEG C, and the end point of distillation is 405~600 DEG C.The wax oil is former Material oil can be one of straight-run gas oil, wax tailings, deasphalted oil, catalytic cycle oil that PETROLEUM PROCESSING obtains etc., from coal One of obtained coal tar, coal direct liquefaction oil, ICL for Indirect Coal Liquefaction oil, synthetic oil, shale oil etc., be also possible to them its In several miscella.

Catalyst For Single-stage Hydrocracking described in step a is conventional wax oil Catalyst For Single-stage Hydrocracking.Generally with VI B race and/or group VIII metal are active component, and group VIB metal is generally Mo and/or W, and group VIII metal is generally Co And/or Ni.The carrier of the catalyst be aluminium oxide, silicon-containing alumina and molecular sieve in it is one or more, molecular sieve can also be contained, The molecular sieve can be Y type molecular sieve.With the poidometer of catalyst, group VIB tenor is calculated as 10wt% with oxide ~35wt%, group VIII metal content are calculated as 3wt%~15wt% with oxide, and molecular sieve content is 0wt%~40wt%.It is main ZHC-01, ZHC-02, ZHC-03, ZHC-04, FC-28, FC-34 that catalyst has Fushun Petrochemical Research Institute to develop are urged Agent etc., TK-925, TK-925, TK-951 etc. that Haldor Topsoe company develops, Albemarle company develops and opens KF-1023 and KF-1023 of hair etc..For hydrocracking catalyst, it is desirable that have certain hydrogenation activity and certain cracking Activity should guarantee that hydrotreating generates generate alkene and aromatic hydrocarbons in fraction in oil and hydrocracking process plus hydrogen saturation, It is required that the reaction of open loop occurs for the aromatic hydrocarbons after saturation.Conventional operating condition can be used in the operating condition being hydrocracked, generally are as follows: Reaction pressure 3.0MPa~19.0MPa, reaction temperature are 300 DEG C~450 DEG C, volume space velocity 0.2h when liquid^-1~6.0h^-1, hydrogen oil Volume ratio is 100:1~2000:1.

Single-stage hydrocracking reactor inlet described in step a can load conventional hydrogenation protecting agent, in single hop plus hydrogen The top of Cracking catalyst bed can load a small amount of hydrogenation pretreatment catalyst, and hydrogenation pretreatment catalyst is conventional wax Oily hydrogenation pretreatment catalyst.Generally using VI B race and/or group VIII metal as active component, with aluminium oxide or silicon-containing alumina For carrier, group VIB metal is generally Mo and/or W, and group VIII metal is generally Co and/or Ni.With the poidometer of catalyst, Group VIB tenor is calculated as 10wt%~35wt% with oxide, group VIII metal content with oxide be calculated as 3wt%~ 15wt%, property are as follows: specific surface is 100~650m²0.15~0.6mL/g of/g, Kong Rongwei.Main catalyst has Fushun 3936, the 3996 of Petroleum Chemical Engineering Institute's development, FF-16, FF-26, FF-36, FF-46, FF-56 series etc. adds hydrogen to locate in advance Catalyst is managed, is also possible to the function of domestic and international catalyst Co. exploitation similar to catalyst, such as HC-K, HC-P of Uop Inc., TK-555, TK-565 catalyst and KF-847, KF-848 of Akzo company of Topsoe company etc..Hydrogenation pretreatment catalyst Admission space amount accounts for total catalyst volume in single-stage hydrocracking reactor and is not more than 20%.Weighted BMO spaces operating condition can Using conventional operating condition, generally reaction pressure 3.0MPa~19.0MPa, reaction temperature is 300 DEG C~450 DEG C, when liquid Volume space velocity 0.2h^-1~6.0h^-1, hydrogen to oil volume ratio is 100:1~2000:1.

Gas-liquid separator described in step a is that single-stage hydrocracking reactor beds interlayer or catalyst bed entrance are arranged Equipment.Gas-liquid separator at least reaction stream entrance, several parts such as liquid phase conduit and gas phase conduit, wherein liquid phase conduit will Isolated liquid phase pulls out single-stage hydrocracking reactor, and isolated gas phase is introduced lower part single hop and added by gas phase conduit Hydrogen Cracking catalyst bed.

A part of single-stage hydrocracking reaction stream described in step a enters gas-liquid separation by gas-liquid separator entrance Device, the mass ratio that the Partial Liquid Phase logistics of extraction accounts for feedstock oil in terms of liquid phase is 5~95 wt%, preferably 10~80 wt%.

Separation described in step b generally comprises be hydrocracked high-pressure separator and low pressure separator separates two parts. Its high-pressure separator is isolated to be hydrocracked high pressure hydrogen-rich gas and liquid, and the isolated liquid of high-pressure separator enters Low pressure separator.Low pressure separator is by the isolated hydrocarbon-rich gas of highly pressurised liquid product and low pressure liquid product.Hydrocarbon-rich gas warp Isolated needs are hydrocracked gas product.

Fractionation described in step b carries out in being hydrocracked fractionating column system.Low pressure liquid product divides in fractionating column It evaporates to obtain and is hydrocracked light naphtha product, is hydrocracked heavy naphtha product, is hydrocracked boat product of coal, is hydrocracked diesel oil Product and hydrocracking tail oil product.

Single hop hydroisomerizing Cracking catalyst described in step c is conventional wax oil hydrogenation isocraking catalyst.Generally Using group VIB and/or group VIII metal as active component, group VIB metal is generally Mo and/or W, and group VIII metal is generally Co and/or Ni.The carrier of the catalyst is one or more in aluminium oxide, silicon-containing alumina and molecular sieve, preferably containing molecule Sieve, the molecular sieve can be beta molecular sieve, Sapo type molecular sieve etc..With the poidometer of catalyst, group VIB metal contains Amount is calculated as 10wt%~35wt% with oxide, and group VIII metal content is calculated as 3wt%~15wt% with oxide, and molecular sieve content is 2wt%~40wt%.The FC-14 etc. that main catalyst has Fushun Petrochemical Research Institute to develop.It is urged for being hydrocracked For agent, it is desirable that have certain hydrogenation activity and certain lytic activity, should guarantee alkene and aromatic hydrocarbons in reaction mass plus Hydrogen saturation, also requires linear paraffin that isomerization reaction occurs.Conventional operating condition can be used in the operating condition of hydroisomerizing cracking, Generally are as follows: reaction pressure 3.0MPa~19.0MPa, reaction temperature are 300 DEG C~450 DEG C, volume space velocity 0.2h when liquid^-1~ 6.0h^-1, hydrogen to oil volume ratio is 100:1~2000:1.

Separation described in step c carries out in hydroisomerizing cracking high-pressure separator and low pressure separator.Wherein plus hydrogen The isolated hydroisomerizing cracking high pressure hydrogen-rich gas of isocraking high-pressure separator and liquid, high-pressure separator are isolated Liquid enters low pressure separator.Low pressure separator is by the isolated hydrocarbon-rich gas of highly pressurised liquid product and low pressure liquid product.It is rich Appropriate hydrocarbon gas is isolated to the hydroisomerizing cracked gas product of needs.

Fractionation described in step c carries out in hydroisomerizing cracking fractionating column system.Low pressure liquid product is in fractionating column Middle fractionation obtains hydroisomerizing cracking light naphtha product, hydroisomerizing cracking heavy naphtha product, hydroisomerizing cracking boat coal Product, hydroisomerizing cracked diesel oil product and hydroisomerizing cracking tail oil product.

Gas product and hydroisomerizing cracked gas product are hydrocracked described in step b and step c individually to be made For product, mixed gas product can also be mixed into.

It is hydrocracked light naphtha product described in step b and step c and hydroisomerizing cracking light naphtha product can Mixing light naphtha product can also be mixed into separately as product.

It is hydrocracked heavy naphtha product described in step b and step c and hydroisomerizing cracking heavy naphtha product can Mixing heavy naphtha product can also be mixed into separately as product.

Described in step b and step c being hydrocracked boat product of coal and hydroisomerizing cracking boat product of coal can be independent As product, mixing boat product of coal can also be mixed into.

Diesel product and hydroisomerizing cracked diesel oil product are hydrocracked described in step b and step c individually to be made For product, mixed diesel product can also be mixed into.

Hydrocracking tail oil described in step b is separately as product.

Hydroisomerizing cracking tail oil described in step c is separately as product.

It can be used directly as recycle hydrogen after the mixing of high pressure hydrogen-rich gas described in step d, also can choose and pass through It is recycled after desulphurization of recycle hydrogen system removing hydrogen sulfide.

In conjunction with Fig. 1, method of the invention is specific as follows: feedstock oil 1 is mixed into single-stage hydrocracking recycle hydrogen 25 first Enter single-stage hydrocracking reactor 2, by the reaction stream of the first Catalyst For Single-stage Hydrocracking bed through gas-liquid separator 23 extraction hydroisomerizing cracked liquid feed streams 4, the logistics after extracting hydroisomerizing cracked stock logistics 4 out goes successively to subsequent Catalyst For Single-stage Hydrocracking bed, single-stage hydrocracking generate logistics 3 and carry out gas-liquid point into high-pressure separator 8 is hydrocracked From isolated liquid enters fractionation in fractionating column 10 and obtains being hydrocracked light naphtha product 12, is hydrocracked scheelite brain Oil product 13 is hydrocracked boat product of coal 14, is hydrocracked diesel product 15 and hydrocracking tail oil product 16, and hydroisomerizing is split Change after feed stream 4 is mixed with single hop isocraking recycle hydrogen 24 and enter hydroisomerizing cracker 5, is split by hydroisomerizing The product stream for changing catalyst bed, which enters in hydroisomerizing cracking high-pressure separator 9, carries out gas-liquid separation, isolated liquid Body enters fractionation in fractionating column 11 and obtains hydroisomerizing cracking light naphtha product 17, hydroisomerizing cracking heavy naphtha product 18, hydroisomerizing cracking boat product of coal 19, hydroisomerizing cracked diesel oil product 20 and hydroisomerizing cracking tail oil product 21, add hydrogen Cracking light naphtha product 12 and hydroisomerizing cracking light naphtha product 17 can obtain after can also mixing separately as product To mixing light naphtha product, it is hydrocracked heavy naphtha product 13 and hydroisomerizing cracking heavy naphtha product 18 can be independent As product, mixing heavy naphtha product is obtained after can also mixing, and is hydrocracked boat product of coal 14 and hydroisomerizing cracking boat Product of coal 19 can obtain mixing boat product of coal, be hydrocracked diesel product 15 and add separately as product after can also mixing Hydrogen isocraking diesel product 20 can obtain mixed diesel product, be hydrocracked height separately as product after can also mixing Through recycling after the isolated mixing of gas 7 of the gas 6 and hydroisomerizing cracking high-pressure separator 9 for pressing separator 8 isolated It is mixed with supplement hydrogen 22 as recycle hydrogen after hydrogen compressor pressurization.

Illustrate the present invention program and effect below by embodiment.

Embodiment 1-3

Protective agent FZC-100, FZC-105 and FZC106 are China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute The hydrogenation protecting agent of development and production；Catalyst FF-56 is China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute The hydrotreating catalyst of development and production；Catalyst FC-28 is that Sinopec Group Fushun petrochemical industry is ground The Catalyst For Single-stage Hydrocracking for studying carefully institute's development and production, contains Y type molecular sieve；Catalyst Z HC-02 is Sinopec's share The Catalyst For Single-stage Hydrocracking of Fushun Petrochemical Research Institute, Co., Ltd development and production is free of molecular sieve；Catalyst FC-14 For the single hop hydroisomerizing Cracking catalyst of China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute's development and production, Contain beta molecular sieve.

The main character of 1 wax oil feedstock oil of table

2 process conditions of table

3 test result of table

Using single-stage hydrocracking technique of the invention it can be seen from embodiment, by out of single-stage hydrocracking reactor It extracts a part of liquid reactions logistics out, and is realized using Catalyst For Single-stage Hydrocracking and single hop hydroisomerizing Cracking catalyst The purpose of heterogeneity hydrocracked product is produced, production method is flexible.

Claims (14)

1. a kind of flexible single-stage hydrocracking technique, includes the following steps:

A, wax oil feedstock oil adds hydrogen to split under the conditions of single-stage hydrocracking by single-stage hydrocracking reactor top single hop first Change catalyst bed, obtains the first single-stage hydrocracking logistics, this part reaction stream is divided into two parts, and a portion passes through Gas-liquid separator, separating obtained liquid stream extract single-stage hydrocracking reactor out；

B, the first single-stage hydrocracking logistics of remainder continues under hydrocracking condition by being hydrocracked instead in step a The Catalyst For Single-stage Hydrocracking bed of device lower part is answered, single-stage hydrocracking logistics is separated, is fractionated to obtain single-stage hydrocracking High pressure hydrogen-rich gas, single-stage hydrocracking gas products, single-stage hydrocracking naphtha product, single-stage hydrocracking boat coal produce Product, single-stage hydrocracking diesel product and single-stage hydrocracking tail oil product；

C, the first single-stage hydrocracking logistics of extraction device obtained by step a passes through list under single hop hydroisomerizing cracking conditions The single hop hydroisomerizing Cracking catalyst bed containing heterogeneous types molecular sieve catalyst of section hydroisomerizing cracker, it is single Section hydroisomerizing cracked-stream is separated, is fractionated to obtain single hop hydroisomerizing cracking high pressure hydrogen-rich gas, single hop hydroisomerizing is split Change gas products, single hop hydroisomerizing cracked naphtha product, single hop hydroisomerizing cracking boat product of coal, single hop hydroisomerizing to split Change diesel product and single hop hydroisomerizing cracking tail oil product.

2. hydrocracking process described in accordance with the claim 1, which is characterized in that further include step d: the single hop that step b is obtained It is recycled after being hydrocracked the single hop hydroisomerizing cracking high pressure hydrogen-rich gas mixing that high pressure hydrogen-rich gas and step c are obtained.

3. hydrocracking process described in accordance with the claim 1, which is characterized in that the initial boiling point of the wax oil raw material be 100~ 400 DEG C, the end point of distillation is 405~600 DEG C.

4. hydrocracking process described in accordance with the claim 3, which is characterized in that the wax oil feedstock oil is selected from straight run wax Oil, wax tailings, deasphalted oil, catalytic cycle oil, coal tar, coal direct liquefaction oil, ICL for Indirect Coal Liquefaction oil, synthetic oil and shale At least one of oil.

5. hydrocracking process described in accordance with the claim 1, which is characterized in that the Catalyst For Single-stage Hydrocracking is with VI B race and/or group VIII metal are active component, and catalyst carrier contains one in aluminium oxide, silicon-containing alumina and molecular sieve Kind is a variety of, and the molecular sieve is Y type molecular sieve.

6. hydrocracking process according to claim 5, which is characterized in that with the poidometer of catalyst, group VIB metal Content is calculated as 10wt%~35wt% with oxide, and group VIII metal content is calculated as 3wt%~15wt%, molecular sieve content with oxide For 0wt%~40wt%.

7. hydrocracking process described in accordance with the claim 1, which is characterized in that the single-stage hydrocracking condition are as follows: anti- Answer pressure 3.0MPa~19.0MPa, reaction temperature is 300 DEG C~450 DEG C, volume space velocity 0.2h when liquid^-1~6.0h^-1, hydrogen oil body Product is than being 100:1~2000:1.

8. hydrocracking process described in accordance with the claim 1, which is characterized in that the reaction of single-stage hydrocracking described in step a Device entrance loads hydrogenation protecting agent, loads hydrogenation pretreatment catalyst in the top of Catalyst For Single-stage Hydrocracking bed.

9. hydrocracking process according to claim 8, which is characterized in that the hydrogenation pretreatment catalyst is with VI B Race and/or group VIII metal are active component, using aluminium oxide or silicon-containing alumina as carrier；With the poidometer of catalyst, the VIth B Race's tenor is calculated as 10wt%~35wt% with oxide, and group VIII metal content is calculated as 3wt%~15wt% with oxide；Its property Matter is as follows: specific surface is 100~650m²0.15~0.6mL/g of/g, Kong Rongwei.

10. hydrocracking process according to claim 8, which is characterized in that hydrogenation pretreatment catalyst admission space amount The percentage by volume of total catalyst volume in single-stage hydrocracking reactor is accounted for no more than 20%.

11. hydrocracking process according to claim 8, which is characterized in that the operating condition of the weighted BMO spaces are as follows: Reaction pressure 3.0MPa~19.0MPa, reaction temperature are 300 DEG C~450 DEG C, volume space velocity 0.2h when liquid^-1~6.0h^-1, hydrogen oil Volume ratio is 100:1~2000:1.

12. hydrocracking process described in accordance with the claim 1, which is characterized in that the Partial Liquid Phase logistics extracted out in step a with The mass ratio that liquid phase meter accounts for feedstock oil is 5~95 wt%, preferably 10~80 wt%.

13. hydrocracking process described in accordance with the claim 1, which is characterized in that the single hop hydroisomerizing cracking catalysis Using group VIB and/or group VIII metal as active component, catalyst carrier contains aluminium oxide/silicon-containing alumina and molecular sieve for agent, The molecular sieve is beta molecular sieve, Sapo type molecular sieve；With the poidometer of catalyst, group VIB tenor is with oxide Be calculated as 10wt%~35wt%, group VIII metal content is calculated as 3wt%~15wt% with oxide, molecular sieve content be 2wt%~ 40wt%。

14. hydrocracking process described in accordance with the claim 1, which is characterized in that the hydroisomerizing cracking conditions are as follows: anti- Answer pressure 3.0MPa~19.0MPa, reaction temperature is 300 DEG C~450 DEG C, volume space velocity 0.2h when liquid^-1~6.0h^-1, hydrogen oil body Product is than being 100:1~2000:1.