CN109988635A

CN109988635A - A kind of hydrotreating and hydrocracking combined process

Info

Publication number: CN109988635A
Application number: CN201711468862.7A
Authority: CN
Inventors: 张学辉; 刘涛; 白振民; 李宝忠; 孙士可; 刘振华
Original assignee: China Petroleum and Chemical Corp; Sinopec Dalian Research Institute of Petroleum and Petrochemicals
Current assignee: Sinopec Dalian Petrochemical Research Institute Co ltd; China Petroleum and Chemical Corp
Priority date: 2017-12-29
Filing date: 2017-12-29
Publication date: 2019-07-09
Anticipated expiration: 2037-12-29
Also published as: CN109988635B

Abstract

The invention discloses a kind of hydrotreating and hydrocracking combined process.Wax oil raw material is divided into two strands by the first hydrogenation pretreatment catalyst bed, resulting material；One material is mixed through extracting weighted BMO spaces reactor among bed out, and with LCO through hydrotreating reactor, and hydrotreating logistics carries out gas-liquid separation and fractionation obtains catalytically cracked material；Another strand of material continues through the second hydrogenation pretreatment catalyst bed, weighted BMO spaces logistics carries out hydrocracking reaction by hydrocracking catalyst bed, gained hydrocracking reaction material carries out gas-liquid separation and fractionation, obtains the hydrocracked products such as naphtha, boat coal, diesel oil and tail oil.The present invention provides a kind of on a set of hydrogenation technique device while production is hydrocracked the hydrogenation combination technique of light-end products and catalytically cracked material for the first time, heat entrained by weighted BMO spaces material can be made full use of, realizes the coupling operation of weighted BMO spaces reactor and hydrotreating reactor.

Description

A kind of hydrotreating and hydrocracking combined process

Technical field

The invention belongs to petroleum refining fields, and in particular to a kind of generation fine quality catalytic cracking raw material and high-quality be hydrocracked The hydrotreating of product and hydrocracking combined process.

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.One-stage serial hydrocracking technology uses two kinds of catalyst, That is pretreating catalyst by hydrocracking and hydrocracking catalyst, both catalyst are seated in weighted BMO spaces reactor respectively In hydrocracking reactor, the catalyst in each reactor is layering filling under normal conditions.Catalytic cracking is heavy One of the important means of oily lighting, but with the in poor quality and heaviness of catalyzed cracking processing raw material, operating condition is got over Come harsher, light-end products yield and product property are deteriorated, and hydrotreating of FCC feedstock technology not only can remove sulphur, The content of nitrogen, metal impurities can also improve the cracking performance of charging, reduce FCC operating severity, improve product distribution, mention High purpose product selectivity reduces dry gas and coke yield, improves the economy of FCC apparatus, reduces purpose product sulfur content, subtracts SOx and NOx content etc. in few regenerated flue gas.There are the sulphur and nitrogen of certain content in catalytic cracking light cycle oil (LCO), with organic The form of compound exists, and arene content is high, and the content of the above aromatic hydrocarbons of especially two rings is high, and usual LCO is recycled directly back to Continue to convert in catalytic cracking unit, catalytic cracking unit is entered back into after perhaps adding hydrogen into hydrotreater or enters Other devices are processed or directly as products.

CN101003746A, CN001955260A, CN001955257A, CN103059960A and CN001955263A are public The hydrocracking process or group technology of a kind of wax oil and catalytic cracking diesel oil Combined machining opened.Such technology can be with wax Oil and LCO are feedstock oil, are yielded products of quality by method for hydrogen cracking or combined method, and especially high-quality heavy naphtha is made For the raw material of catalytic reforming, rather than catalytically cracked material is generated, re-starts conversion without Returning catalyticing cracking device.

CN106701175A, CN102465035A and CN001896192A, which are disclosed in a kind of hydroprocessing technique, mixes refining The technology of LCO, main purpose is production fine quality catalytic cracking raw material, or LCO is allowed to split in hydrotreater and catalysis The coupling technique that makeup recycles between setting, realizes the clean manufacturing of catalytic cracking unit, but due to wax oil or residual oil etc. and LCO The hydrogenation depth of direct hydrogenation after mixing, LCO not can be effectively controlled, and cannot produce high-quality hydrocracked product.

It is usually all that LCO directly mixes refining to urging in conclusion compare existing LCO hydrogen addition technology and hydrocracking technology Change and carried out plus hydrogen in cracked stock pretreatment unit, then returns again to catalytic cracking unit or LCO mixes refining to being hydrocracked original In material oil, enter in hydrocracking unit after weighted BMO spaces and produce hydrocracked naphtha product, in same covering device with Wax oil and LCO are that feedstock oil produces high-quality hydrocracked product simultaneously and the Combined machining technology of catalytically cracked material is less, and And without the Combined machining technology of reaction mass coupling.

Summary of the invention

In view of the deficiencies of the prior art, the present invention provides a kind of hydrotreating and hydrocracking combined process.Pass through From extraction section reaction stream in the middle part of the weighted BMO spaces reactor for using hydrocracking unit, by the wax oil feedstock oil and LCO feedstock oil is hydrocracked by weighted BMO spaces-and produces high-quality hydrocracked product and high-quality with hydrotreating group technology Catalytically cracked material.

A kind of hydrotreating of the invention and hydrocracking combined process, include the following steps:

A, wax oil feedstock oil is urged under the conditions of weighted BMO spaces by the first weighted BMO spaces of weighted BMO spaces reactor first Agent bed obtains the first weighted BMO spaces logistics, this part reaction stream is divided into two parts, and a portion extraction plus hydrogen are pre- Treatment reactor；

B, the first weighted BMO spaces logistics continuation of remainder passes through weighted BMO spaces under the conditions of weighted BMO spaces in step a Second hydrogenation pretreatment catalyst bed of reactor, weighted BMO spaces logistics continue under hydrocracking condition by adding hydrogen to split Change reactor hydrocracking catalyst bed, be hydrocracked logistics separated, be fractionated to obtain be hydrocracked high pressure hydrogen-rich gas, It is hydrocracked gas product, hydrocracked naphtha product, boat product of coal is hydrocracked, is hydrocracked diesel product and hydrogen is added to split Change tail oil product；

C, the first weighted BMO spaces logistics of extraction device obtained by step a passes through under hydroprocessing conditions after mixing with LCO The hydrotreating catalyst bed of hydrotreating reactor, hydrotreating logistics are separated, are fractionated to obtain hydrotreating high pressure richness Hydrogen, hydrotreating gas, hydrotreated naphtha, hydroprocessed diesel and hydrotreating heavy oil.

Hydrotreating according to the present invention and hydrocracking combined process, wherein can also include step d: step b be obtained Be hydrocracked the hydrotreating high pressure hydrogen-rich gas mixing that high pressure hydrogen-rich gas and step c obtain after be recycled.

The impurity such as S, N, O in wax oil feedstock oil by obtaining partial removal when the first hydrogenation pretreatment catalyst bed, Aromatic hydrocarbons obtains to a certain extent plus hydrogen saturation, the logistics after extracting weighted BMO spaces material out continue through hydrogenation pretreatment catalyst Bed and hydrocracking catalyst bed obtain good hydrocracked product, are such as hydrocracked light naphthar, are hydrocracked weight Naphtha is hydrocracked boat coal, is hydrocracked diesel oil and hydrocracking tail oil etc.；Research shows that: the aromatic hydrogenation of LCO is saturated deep Degree is affected to fcc gasoline product quality, and especially mononuclear aromatics is antiknock component in gasoline, increases and adds The content of mononuclear aromatics can be increased the octane number of catalytically cracked gasoline in hydrogen LCO, and the weighted BMO spaces logistics extracted out is because Have passed through partial hydrogenation reaction, add hydrogen difficulty reduction, therefore its mix with LCO after can relatively mitigation operating condition assign It to the purpose requirement of hydrodesulfurization, hydrodenitrogeneration, and just can control the hydrogenation depth of LCO at this time, that is, meeting sulfur content Under the premise of by LCO two cycloaromatics and polycyclic aromatic hydrocarbon add hydrogen to mononuclear aromatics, rather than hydrogenation depth excessively generates ring Alkane or hydrogenation depth are insufficient and generate two cycloaromatics, and the product after such hydrotreating is re-introduced into catalytic cracking dress The content of Aromatics in Fcc Naphtha can be improved when setting, to improve the octane number of catalytically cracked gasoline.

Compared with prior art, hydrotreating of the invention and the advantages of hydrocracking combined process, are:

It 1, include at least two hydrogenation pretreatment catalyst beds in weighted BMO spaces reactor in the present invention.Existed by setting Pretreated material extraction step among weighted BMO spaces reactor bed is not necessarily to special operation, can be realized to adding hydrogen to locate in advance Effective distribution of material stock is managed, then makes obtained material by hydrogenation combination technique, so as to produce the mesh of different size Product.Meanwhile abstraction reaction logistics is technically also to be easily achieved among reactor bed.And in the prior art In, hydrotreating techniques and hydrocracking technology are typically only capable to produce a kind of purpose product of hydrogenation technique according to this technology.

2, the present invention among the catalyst bed of weighted BMO spaces reactor by being arranged the first weighted BMO spaces logistics Wax oil raw material is extracted reactor by the first weighted BMO spaces logistics of weighted BMO spaces by withdrawing device, and by itself and LCO Mixing is sent into the hydrotreating reactor that is separately provided and carries out hydrogenation reaction, due to the sulphur of some wax oil raw material, nitrogen Equal impurity have been hydrogenated removing, therefore further add the difficulty of hydrogen to reduce, therefore can control reaction condition to control LCO's Hydrogenation depth, i.e. the depth that two cycloaromatics and polycyclic aromatic hydrocarbon add hydrogen to be saturated in control LCO, control as far as possible by two cycloaromatics it is a lot of Cycloaromatics adds hydrogen to mononuclear aromatics, in this way will plus hydrogen after LCO reduce reaction difficulty or improve when carrying out catalytic cracking again and urge Change the arene content in cracking gasoline, improves the octane number of gasoline.

3, in the present invention, the extraction logistics itself that is obtained among weighted BMO spaces reactor hydrogenation pretreatment catalyst bed It can be directly entered in newly-installed hydrotreating reactor and be carried out instead with very high temperature and pressure, after being mixed with LCO It answers, so that this thigh be made full use of to divide heat entrained by pretreated material, realizes weighted BMO spaces reactor and hydrotreating The coupling operation of reactor.

4, in the present invention, hydrocracking reaction system is identical with the operating pressure of hydrotreating reaction system, therefore two A set of hydrogen desulphurization system and a set of hydrogen gas circulating system can be used in high pressure hydrogen-rich gas in system, to save equipment Investment and operating cost.

Detailed description of the invention

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

Wherein: 1- wax oil feedstock oil, 2- weighted BMO spaces reactor, 3- weighted BMO spaces extract logistics, 4-LCO raw material out Oil, 5- hydrocracking reactor, 6- are hydrocracked logistics, 7- hydrotreating reactor, and 8- is hydrocracked high-pressure separator, and 9- adds Hydrogen handles high-pressure separator, and 10- is hydrocracked fractionating column, 11- hydrotreating fractionating column, and 12- is hydrocracked light naphtha product, 13- is hydrocracked heavy naphtha product, and 14- is hydrocracked boat product of coal, and 15- is hydrocracked diesel product, and 16- is hydrocracked tail Oil product, 17- hydrotreated naphtha product, 18- hydroprocessed diesel product, 19- hydrotreating heavy distillate, 20- add hydrogen Cracking high-pressure separator hydrogen-rich gas, 21- hydrotreating high-pressure separator hydrogen-rich gas, 22- supplement 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 405~650 DEG C.The wax oil is former Material oil can be one of straight-run gas oil, wax tailings, deasphalted oil that PETROLEUM PROCESSING obtains etc., the coal tar obtained from coal It is wherein several mixed to be also possible to them for one of oil, coal direct liquefaction oil, ICL for Indirect Coal Liquefaction oil, synthetic oil, shale oil etc. Close oil.

Wherein, the catalysis in the weighted BMO spaces reactor, according to the engagement sequence with reaction mass, positioned at upstream Agent bed is the first hydrogenation pretreatment catalyst bed, and the catalyst bed positioned at downstream is the second hydrogenation pretreatment catalyst bed Layer.

Hydrogenation pretreatment catalyst described in step a and step b is conventional wax oil hydrogenation pretreatment catalyst.Generally Using VI B race and/or group VIII metal as active component, using aluminium oxide or silicon-containing alumina as carrier, group VIB metal is generally Mo and/or W, group VIII metal are generally Co and/or Ni.With the poidometer of catalyst, group VIB tenor is in terms of oxide For 10wt%~35wt%, group VIII metal content is calculated as 3wt%~15wt% with oxide；Its property is as follows: specific surface be 100~ 650m²0.15~0.6mL/g of/g, Kong Rongwei.Main catalyst have Fushun Petrochemical Research Institute develop 3936, 3996, FF-16, the hydrogenation pretreatment catalysts such as FF-26, FF-36, FF-46, FF-56 series are also possible to domestic and international catalyst The function of company's exploitation is similar to catalyst, and such as HC-K, HC-P of Uop Inc., TK-555, TK-565 of Topsoe company are catalyzed Agent and KF-847, KF-848 of Akzo company etc..Conventional operating condition, generally reaction pressure can be used in operating condition 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.

The weight percent that the fraction of stream of extraction described in step a accounts for wax oil feedstock oil in terms of liquid phase is 5~95wt%, Preferably 10~80wt%.

Hydrocracking catalyst described in step b is conventional wax oil hydrogenation Cracking catalyst.Generally with group VIB and/ Or group VIII metal is active component, group VIB metal is generally Mo and/or W, and group VIII metal is generally Co and/or Ni.It should The carrier of catalyst contains one of aluminium oxide, silicon-containing alumina and molecular sieve or a variety of, preferably contains molecular sieve.Described Molecular sieve can be Y type molecular sieve, 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 5wt%~80wt%.Main catalyst have Fushun Petrochemical Research Institute develop 3824,3825,3976, FC-12, FC-14, FC-20, FC-24, FC-26, FC-32, FC-50 catalyst etc., HC-12, HC-14, HC-24, HC-39 of Uop Inc. Deng.For hydrocracking catalyst, it is desirable that have certain hydrogenation activity and certain lytic activity, should guarantee hydrotreating Generate alkene and aromatic hydrocarbons in fraction in oil and hydrocracking process plus hydrogen saturation is generated, also the aromatic hydrocarbons after saturation is required to open The reaction of ring.Conventional operating condition can be used in the operating condition being hydrocracked, generally are as follows: and 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 be 100:1~ 2000:1。

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.

LCO raw material described in step c is the light cycle oil of catalytic cracking unit, and initial boiling point is 100~200 DEG C, the end point of distillation It is 320~400 DEG C.The virtues such as some coker gas oils, ethylene cracking tar, coal tar can also be blended in the LCO feedstock oil High one or more of the diesel oil distillate of hydrocarbon content.

Hydrotreating catalyst described in step c is conventional wax oil hydrogenation processing catalyst.Generally with VI B race and/ Or group VIII metal is active component, using aluminium oxide or silicon-containing alumina as carrier, group VIB metal is generally Mo and/or W, Group VIII metal is generally Co and/or Ni.With the poidometer of catalyst, group VIB tenor with oxide be calculated as 10wt%~ 35wt%, group VIII metal content are calculated as 3wt%~15wt% with oxide；Its property is as follows: specific surface is 100~650m²/ g, 0.15~0.6mL/g of Kong Rongwei.Main catalyst has 3936,3996, FF- that Fushun Petrochemical Research Institute develops 14, the hydrotreating catalysts such as FF-16, FF-24, FF-26, FF-36, FF-46, FF-56 series are also possible to be catalyzed both at home and abroad The function of agent company exploitation is similar to catalyst, and such as HC-K, HC-P of Uop Inc., TK-555, TK-565 of Topsoe company are catalyzed Agent and KF-847, KF-848 of Akzo company etc..Conventional operating condition, generally reaction pressure can be used in operating condition 3.0MPa~19.0MPa, reaction temperature are 300 DEG C~450 DEG C, preferably 320 DEG C~410 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 hydrotreating high-pressure separator and low pressure separator.Wherein hydrotreating The isolated hydrotreating high pressure hydrogen-rich gas of high-pressure separator and liquid, the isolated liquid of high-pressure separator enter 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 is through separating The hydrotreating gaseous product needed.

Fractionation described in step c carries out in hydrotreating fractionating column system.Low pressure liquid product divides in fractionating column It evaporates to obtain hydrotreated naphtha product, hydroprocessed diesel and hydrotreating heavy distillate.

It is hydrocracked gas product described in step b and step c and hydrotreating gas products can be separately as production Product can also be mixed into mixed gas product.

It is hydrocracked light naphtha product described in step b and step c and hydrotreated naphtha product can be independent As product, mixing naphtha product can also be mixed into.

Be hydrocracked heavy naphtha product of the step b with described in can be separately as product.

Boat product of coal is hydrocracked described in step b can be separately as product.

Diesel product is hydrocracked described in step b can be separately as product.

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

Hydroprocessed diesel described in step c can be separately as product, can also be mixed with hydrotreating heavy distillate Cooperation is the feedstock oil of catalytic cracking unit.

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 the present invention, two hydrotreating catalyst beds are preferably comprised in the hydrotreating reactor, i.e., first adds Hydrogen handles catalyst bed and the second hydrotreating catalyst bed (dividing according to reaction mass engagement sequence).Increase simultaneously LCO raw material is carried out to the process of distillation cutting, LCO feedstock oil is preferably divided into gently and again two parts according to fraction, fraction segmentation Temperature spot be 245 ~ 300 DEG C, i.e., the fraction range of light fraction be initial boiling point to cut-point temperature, the fraction range of heavy distillat is Cut-point temperature is to the end point of distillation.After LCO heavy distillat is mixed with the weighted BMO spaces reaction stream that weighted BMO spaces reactor is extracted out By the first hydrotreating catalyst bed in hydrotreating reactor, then the first hydrotreating reaction material and LCO are light Fraction mixing passes through the second hydrotreating catalyst bed.It is more due to based on polycyclic aromatic hydrocarbon, passing through in LCO heavy distillat Hydrotreating catalyst reaction, can achieve control aromatic hydrogenation depth purpose, and in LCO light fraction double ring arene pass through compared with The hydrotreating catalyst reaction of few degree, can achieve the purpose that control aromatic hydrogenation depth with LCO heavy distillat simultaneously, i.e., plus Hydrogen treated LCO while meeting sulfur content double ring arene and polycyclic aromatic hydrocarbon moderately plus hydrogen is to mononuclear aromatics, into one It can satisfy the catalytically cracked gasoline of sulfur content requirement after step catalytic cracking, and the octane number of gasoline can be improved.

In the present invention, the first hydrogenation pretreatment catalyst bed and the setting of the second hydrogenation pretreatment catalyst bed In a weighted BMO spaces reactor, or it is separately positioned in more than two weighted BMO spaces reactors.In the present invention It is preferred that using first way.

Equally, the first hydrotreating catalyst bed and the setting of the second hydrotreating catalyst bed add at one In hydrogen treatment reactor, or it is separately positioned in more than two hydrotreating reactors.First is preferably used in the present invention Kind mode.

In conjunction with Fig. 1, method of the invention wax oil feedstock oil 1 specific as follows is mixed into weighted BMO spaces with recycle hydrogen first Reactor 2 extracts logistics 3, extraction out by extracting weighted BMO spaces in the reaction stream of the first hydrogenation pretreatment catalyst bed out Weighted BMO spaces extract the logistics after logistics 3 out after the second hydrogenation pretreatment catalyst bed, go successively to hydrocracking reaction Device 5 is hydrocracked and generates logistics 6 into the progress gas-liquid separation of high-pressure separator 8 is hydrocracked, and isolated liquid, which enters, to be divided Fractionation in tower 10 is evaporated to obtain being hydrocracked light naphtha product 12, be hydrocracked heavy naphtha product 14, be hydrocracked boat coal production Product 14 are hydrocracked diesel product 15 and hydrocracking tail oil product 16, and weighted BMO spaces extract logistics 3 out and LCO feedstock oil 4 is mixed Enter hydrotreating reactor 7 after conjunction, the separation of hydrotreating high pressure is entered by the product stream of hydrotreating catalyst bed Gas-liquid separation is carried out in device 9, isolated liquid enters fractionation in fractionating column 11 and obtains hydrotreated naphtha product 17, adds Hydrogen processing diesel product 18, hydrotreating heavy distillat 19 are hydrocracked the isolated gas 20 of high-pressure separator 8 and add at hydrogen The isolated gas 21 of reason high-pressure separator 9 is mixed with supplement hydrogen 22 as circulation after circulating hydrogen compressor is pressurized after mixing Hydrogen.

Illustrate the present invention program and effect below by embodiment.

Embodiment 1-4

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-32 is that Sinopec Group Fushun petrochemical industry is ground The hydrocracking catalyst for studying carefully institute's development and production, contains Y type molecular sieve；Catalyst FF-24 is that Sinopec's share is limited The hydrotreating catalyst of Fushun Petrochemical Research Institute, company development and production.

The main character of 1 wax oil feedstock oil of table

	Wax oil 1	Wax oil 2	LCO
				Density, g/cm³	0.901	0.921	0.932
Fraction range, DEG C	320~545	345~575	156~370
				Sulfur content, wt%	1.15	2.23	1.3
Nitrogen content, wt%	0.127	0.082	0.09
				Arene content, wt%	—	—	91.2

2 process conditions of table

2 process conditions of continued

Wherein, LCO light fraction and heavy distillat segmentation temperature are 270 DEG C.

3 test result of table

Using hydrotreating of the invention and hydrocracking combined process it can be seen from embodiment, by from weighted BMO spaces A part of reaction stream of extraction in reactor, extraction logistics and LCO mixed hydrogenation process for producing fine quality catalytic cracking raw material, it is remaining Weighted BMO spaces logistics continues weighted BMO spaces and hydrocracking catalyst produces the purpose of high-quality hydrocracked product, producer Formula is flexible.

Claims

1. a kind of hydrotreating and hydrocracking combined process, include the following steps:

2. group technology described in accordance with the claim 1, which is characterized in that root further includes step d: step b is obtained plus hydrogen is split It is recycled after changing the hydrotreating high pressure hydrogen-rich gas mixing that high pressure hydrogen-rich gas and step c are obtained.

3. group technology described in accordance with the claim 1, which is characterized in that the initial boiling point of the wax oil raw material is 100~400 DEG C, the end point of distillation is 405~650 DEG C.

4. group technology described in accordance with the claim 3, which is characterized in that the wax oil feedstock oil is selected from straight-run gas oil, coke Change at least one of wax oil, deasphalted oil, coal tar, coal direct liquefaction oil, ICL for Indirect Coal Liquefaction oil, synthetic oil and shale oil.

5. group technology described in accordance with the claim 1, which is characterized in that the initial boiling point of the LCO is 100~200 DEG C, eventually Evaporate a little is 320~400 DEG C.

6. group technology described in accordance with the claim 1, which is characterized in that also blend coker gas oil in the LCO, ethylene is split Solve at least one of tar and coal tar.

7. group technology described in accordance with the claim 1, which is characterized in that the hydrogenation pretreatment catalyst with VI B race and/ Or group VIII metal is active component, using aluminium oxide or silicon-containing alumina as carrier；With the poidometer of catalyst, group VIB gold Belong to content and 10wt%~35wt% is calculated as with oxide, group VIII metal content is calculated as 3wt%~15wt% with oxide；Its property is such as Under: specific surface is 100~650m²0.15~0.6mL/g of/g, Kong Rongwei.

8. group technology described in accordance with the claim 1, which is characterized in that the 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 to oil volume ratio is 100:1~2000:1.

9. group technology described in accordance with the claim 1, which is characterized in that the fraction of stream extracted out in step a is accounted in terms of liquid phase The weight percent of wax oil feedstock oil is 5~95 wt%, preferably 10~80 wt%.

10. group technology described in accordance with the claim 1, which is characterized in that the hydrocracking catalyst is with group VIB And/or group VIII metal is active component, catalyst carrier contains one of aluminium oxide, silicon-containing alumina and molecular sieve or more Kind, the molecular sieve is Y type molecular sieve, beta molecular sieve or Sapo type molecular sieve.

11. group technology according to claim 10, which is characterized in that 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 5wt%~80wt%.

12. group technology described in accordance with the claim 1, which is characterized in that the hydrocracking condition 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.

13. group technology described in accordance with the claim 1, which is characterized in that the hydrotreating catalyst with VI B race and/ Or group VIII metal is active component, using aluminium oxide or silicon-containing alumina as carrier；With the poidometer of catalyst, group VIB gold Belong to content and 10wt%~35wt% is calculated as with oxide, group VIII metal content is calculated as 3wt%~15wt% with oxide；Its property is such as Under: specific surface is 100~650m²0.15~0.6mL/g of/g, Kong Rongwei.

14. group technology described in accordance with the claim 1, which is characterized in that the hydroprocessing condition are as follows: reaction pressure 3.0MPa~19.0MPa, reaction temperature are 300 DEG C~450 DEG C, preferably 320 DEG C~410 DEG C, volume space velocity 0.2h when liquid^-1~ 6.0h^-1, hydrogen to oil volume ratio is 100:1~2000:1.

15. group technology described in accordance with the claim 1, which is characterized in that the hydrotreating reactor include there are two plus Hydrogen handles catalyst bed, i.e. the first hydrotreating catalyst bed and the second hydrotreating catalyst bed.

16. group technology according to claim 15, which is characterized in that the method also includes: LCO raw material is cut into LCO light fraction and LCO heavy distillat, the temperature of the cutting are 245 ~ 300 DEG C；The LCO heavy distillat is reacted with weighted BMO spaces Pass through the first hydrotreating catalyst in hydrotreating reactor after the first weighted BMO spaces reaction stream mixing of device extraction Bed, the first hydrotreating reaction material are mixed with LCO light fraction through the second hydrotreating catalyst bed.

17. group technology described in accordance with the claim 1, which is characterized in that the first hydrogenation pretreatment catalyst bed It is arranged in a weighted BMO spaces reactor with the second hydrogenation pretreatment catalyst bed, or is separately positioned on two or more Weighted BMO spaces reactor in.

18. according to group technology described in claim 15 or 16, which is characterized in that the first hydrotreating catalyst bed Layer and the second hydrotreating catalyst bed are arranged in a hydrotreating reactor, or are separately positioned on more than two In hydrotreating reactor.