CN109988642A - Produce the flexible method for hydrogen cracking of lube base oil - Google Patents
Produce the flexible method for hydrogen cracking of lube base oil Download PDFInfo
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- CN109988642A CN109988642A CN201711469386.0A CN201711469386A CN109988642A CN 109988642 A CN109988642 A CN 109988642A CN 201711469386 A CN201711469386 A CN 201711469386A CN 109988642 A CN109988642 A CN 109988642A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of flexible method for hydrogen cracking for producing lube base oil.Material of the wax oil raw material after weighted BMO spaces is divided into two parts；A part of material through the isolated gas phase of high pressure hot separator and liquid phase, another part material mixed with hot high score gas phase and recycle hydrogen after by the hydrocracking catalyst bed containing Y type molecular sieve；After hot high score liquid phase is mixed with hydrocracking tail oil and recycle hydrogen, pass through the hydroisomerizing Cracking catalyst bed containing isocraking type molecular sieve；Hydrocracking reaction product and hydroisomerizing cracked reaction product carry out gas-liquid separation and fractionation respectively, obtain the distillate and tail oil of different size, and hydrocracking tail oil is some or all of to be recycled into isocraking reactor.The present invention provides one kind on a set of hydrogenation technique device for the first time while producing two or more different size naphthas, boat coal, diesel oil, tail oil product, especially produces the flexible method for hydrogen cracking of High Quality Lube Base Oils.
Description
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 method for hydrogen cracking of diesel oil, tail oil product, especially High Quality Lube Base Oils.
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.Hydrocracking technology uses two kinds of catalysis
Agent, pretreating catalyst by hydrocracking and hydrocracking catalyst, wherein hydrocracking catalyst is according to using Cracking Component
It is different can be divided into different types of catalyst again, main Cracking Component includes amorphous silica-alumina, Y type molecular sieve, β type point
Son sieve, SAPO Series Molecules sieve and ZSM-5 molecular sieve etc..A group timesharing, obtained light oil are hydrocracked using different type
Product composition and property also have biggish difference, and the composition and property of tail oil also have biggish difference.
CN103055922B discloses a kind of preparation method of body phase hydrocracking catalyst, CN105018139B,
CN001293228A, CN001508225A and CN104611020B a kind of all disclosed high-output qulified industrial chemicals of low energy consumption add
The method that gradation uses two kinds of different Y type molecular sieves in hydrogen cracking method.Such technology can be using wax oil as feedstock oil, by making
Yielded products of quality with the method for hydrogen cracking containing Y type molecular sieve hydrocracking catalyst, wherein in tail oil Determination of Alkane Content it is high,
BMCI value is low, is the raw material of quality steam cracking ethylene preparation, but the product for being hydrocracked each obtained fraction only has
A kind of specification.
CN105582992A discloses a kind of hydroisomerisation catalysts and its preparation method and application, and a kind of plus hydrogen
Cracking tail oil hydroisomerization process, such technology can using wax oil as feedstock oil, by using contain heterogeneous types molecular sieve
The method for hydrogen cracking of hydrocracking catalyst yields products of quality, and wherein isomery content height, condensation point are low in tail oil, viscosity index (VI)
Height, the product for being the raw material of High Quality Lube Base Oils, but being hydrocracked each obtained fraction only have 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 US4837396A discloses a kind of preparation of complex type molecular sieve catalysis.Such technology can using wax oil as feedstock oil,
By using the method for hydrogen cracking containing Y type molecular sieve and heterogeneous types molecular sieve complex type molecular sieve hydrocracking catalyst
Various high-quality hydrocracked products are produced, but the product of each fraction only has a kind of specification.
CN001169919C is disclosed a kind of to be raised productivity and improved the quality the method for diesel oil by distillate.Such technology can be with wax oil
Feedstock oil, while being catalyzed using containing Y zeolite catalyst and containing two kinds of heterogeneous types molecular sieve hydrocracking catalyst
The method for hydrogen cracking of agent produces various high-quality hydrocracked products, but the product of each fraction only has a kind of specification.
In conclusion the existing hydrocracking technology using two kinds of different type molecular sieve catalysts of comparison, uses Y type
The hydrocracking technology of molecular sieve hydrocracking catalyst, obtained heavy naphtha product sulfur content is low, virtue dive it is relatively high,
Navigating, product of coal smoke point is relatively high, and diesel product sulfur content is low, and Cetane number is high, but condensation point is relatively high, tail oil product virtue
Hydrocarbon content is low, and density is relatively small, and BMCI value is relatively low, but condensation point is very high, and typically larger than 30 DEG C；Use heterogeneous types
The hydrocracking technology of molecular sieve hydrocracking catalyst, obtained heavy naphtha product sulfur content is low, and virtue is latent relatively slightly lower,
Diesel product sulfur content is low, and condensation point is low, but Cetane number is relatively slightly lower, and tail oil density is relatively large, but isomery hydrocarbon content
Height, condensation point is very low, and usually less than 0 DEG C；Use the hydrocracking technology of the complex type molecular sieve catalysis of isomery containing Y-, Huo Zheji
Skill is hydrocracked with use hydrocracking catalyst containing Y type molecular sieve and the molecular sieve hydrocracking catalyst containing heterogeneous types
Art, obtained tail oil property is between using Y type molecular sieve hydrocracking catalyst and heterogeneous types molecular sieve is used to split
Change between catalyst.Above-mentioned hydrocracking process technology, the hydrocracking tail oil differentiation of product produced in identical conversion ratio
It is larger, wherein being the quality raw materials of preparing ethylene by steam cracking using the tail oil of Y zeolite catalyst, use heterogeneous types molecule
The tail oil of sieve catalyst is can directly to produce High Quality Lube Base Oils or the raw material as High Quality Lube Base Oils, is made
Using hydrocracking catalyst containing Y type molecular sieve and contain heterogeneous types with the complex type molecular sieve catalysis of isomery containing Y- or gradation
The tail oil that molecular sieve hydrocracking catalyst obtains can be used as the raw material of preparing ethylene by steam cracking or as high-quality lubricating oil
The raw material of base oil.When above-mentioned several hydrocracking process therefore are used alone, different types of add can only be selected as needed
Hydrogen Cracking catalyst is perhaps made using two kinds of hydrocracking catalyst gradations of two kinds of molecular sieve composite catalysts or selection
With, but these techniques can only produce a kind of tail oil product of property, 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 method for hydrogen cracking for producing lube base oil,
I.e. by being divided into two parts from weighted BMO spaces product stream, a portion enters high pressure hot separator, isolated gas
Body is mixed with remaining a part and is hydrocracked, and isolated liquid is mixed with hydrocracking tail oil and hydrogen to be added
The wax oil feedstock oil is hydrocracked by Y type hydrocracking catalyst and is hydrocracked with heterogeneous types by hydrogen isocraking
Catalyst hydrogenation isocraking combined method flexibly produces preparing ethylene by steam cracking raw material, the High Quality Lube Base Oils of high quality
The naphtha product and high-quality automotive fuel product of raw material and plurality of specifications.
The flexible method for hydrogen cracking of production lube base oil of the invention, includes the following steps:
A, wax oil feedstock oil enters weighted BMO spaces reactor under the conditions of weighted BMO spaces first and is urged by weighted BMO spaces
Agent bed obtains weighted BMO spaces logistics, this part reaction stream is divided into two parts, and a portion enters thermal high separation
The isolated gas phase of device and liquid phase；
B, another part weighted BMO spaces logistics that step a is obtained and the isolated gaseous stream of high pressure hot separator are adding hydrogen
By the hydrocracking catalyst bed containing Y zeolite catalyst in hydrocracking reactor under cracking conditions, added
Hydrogen cracked-stream；Logistics is hydrocracked to be separated, be fractionated to obtain and be hydrocracked high pressure hydrogen-rich gas, be hydrocracked gas product,
It is hydrocracked fraction oil product and hydrocracking tail oil product；
C, after liquid phase stream obtained by step a is mixed with hydrocracking tail oil obtained by step b and recycle hydrogen, in hydroisomerizing cracking item
By the hydroisomerizing Cracking catalyst bed containing heterogeneous types molecular sieve catalyst under part, hydroisomerizing cracking object is obtained
Stream, hydroisomerizing cracked-stream are separated, are fractionated to obtain hydroisomerizing cracking high pressure hydrogen-rich gas, the production of hydroisomerizing cracked gas
Product, hydroisomerizing cracked distillate oil product and hydroisomerizing cracking tail oil product.
Method for hydrogen cracking according to the present invention, wherein can also include step d: what step b was obtained be hydrocracked high pressure
It is recycled after the hydroisomerizing cracking high pressure hydrogen-rich gas mixing that hydrogen-rich gas and step c are obtained.
In the present invention, be hydrocracked described in step b fraction oil product generally include to be hydrocracked light naphtha product,
It is hydrocracked heavy naphtha product, be hydrocracked boat product of coal and is hydrocracked diesel product.Equally, add described in step c
Hydrogen isocraking fraction oil product generally includes hydroisomerizing cracking light naphtha product, hydroisomerizing cracking heavy naphtha produces
Product, hydroisomerizing cracking boat product of coal and hydroisomerizing cracked diesel oil product
The impurity such as S, N, O in wax oil feedstock oil are effectively removed when passing through hydrogenation pretreatment catalyst, and aromatic hydrocarbons is to a certain degree
On obtain plus hydrogen saturation, the gaseous stream that a part of weighted BMO spaces logistics is obtained through gas-liquid separation adds hydrogen to locate in advance with another part
Cyclic hydrocarbon generating unit separates when continuing through the hydrocracking catalyst bed containing Y zeolite catalyst after reason logistics mixing
Ring reaction, macromolecular are cracked into small molecule, and Y type molecular sieve has the characteristics that preferentially to crack the polycyclic cyclic hydrocarbon of macromolecular, can obtain
To the low boat product of coal of high normal hydrocarbon content, arene content, diesel product and tail oil product；The liquid phase obtained through gas-liquid separator
Logistics is subsequent by the hydroisomerizing Cracking catalyst containing heterogeneous types molecular sieve catalyst after mixing with hydrocracking tail oil
The continuous isomery that carries out is hydrocracked, because heterogeneous types molecular sieve has the characteristics that isomery and cracking, available high isomery hydrocarbon content
Isocraking product, the condensation point of especially diesel product is low, the condensation point of tail oil product is low, and viscosity index (VI) is high, hydrocracking tail oil
Continue hydroisomerizing cracking, the isoparaffin content of tail oil product can be increased and reduces arene content and polycyclic ring alkane
Content, the viscosity index (VI) of hydroisomerizing cracking tail oil is further increased, additionally, due to hydroisomerizing cracking reaction in low NH3With
Low H2It is carried out under S environment, required reaction temperature is very low, it is only necessary to hydroisomerizing cracking can be met after recycle hydrogen cooling
The requirement of reaction temperature.
Compared with prior art, the present invention produces the advantages of lube base oil flexible method for hydrogen cracking and is:
1, in the present invention, the weighted BMO spaces logistics that weighted BMO spaces reactor obtains directly is divided into two parts, nothing in pipeline
Special operation is needed, effective distribution to weighted BMO spaces material stock can be realized, a portion can after high pressure hot separator
To obtain gas phase and liquid phase, then make the mixed material of obtained liquid phase material and gaseous phase materials and another hydrotreated material
It is especially hydrocracked by different hydrocracking process so as to flexibly produce the purpose product of different size respectively
Tail oil passes through available excellent after the isocraking catalyst of molecular sieve containing heterogeneous types in hydroisomerizing cracker
Matter lube base oil product.And in the prior art, although the boiling range by adjusting conversion ratio and adjustment product is available
A variety of light-end products, but since only one hydrocracking reactor exports, a set of same fraction of hydrocracking unit
Range is typically only capable to a type of light naphthar, heavy naphtha product, boat product of coal, diesel product and tail oil product；If
Want to obtain the hydrocracked product of different size, needs two sets or more of hydrocracking unit.Therefore, the present invention provides for the first time
One kind producing two or more same fraction ranges simultaneously on a set of hydrocracking process device, but different size tail oil produces
Product, two or more different sizes boat product of coal, two or more different size diesel products and a variety of different size naphtha products
Hydrocracking process.
2, the present invention is directly isolated to obtain two parts by the weighted BMO spaces logistics in weighted BMO spaces reactor outlet
Logistics, and through the isolated gas phase of high pressure hot separator and liquid phase, liquid phase stream is as one raw material, gaseous stream and another portion
The mixture flow of point hydrotreating logistics as one raw material, and be respectively fed to the hydrocracking reactor being separately provided into
Row hydrocracking reaction and entrance hydroisomerizing cracker carry out hydroisomerizing cracking reaction, and make hydrocracking tail oil
It is some or all of to enter hydroisomerizing cracker, contain so that method of the invention can flexibly produce different aromatic hydrocarbons
Amount, different isomerization hydrocarbon content, the naphtha product of different condensation points, boat product of coal, diesel product and tail oil product.
3, in the present invention, in the product that two cracker logistics are fractionated, by containing Y zeolite catalyst
The heavy naphtha virtue obtained after being hydrocracked is dived, and relatively high, boat product of coal smoke point is relatively high, diesel product Cetane number phase
To higher, tail oil product paraffinicity is high, BMCI value is relatively low；Add by part containing heterogeneous types molecular sieve catalyst
After hydrogen isocraking, especially hydrocracking tail oil is continued through containing after heterogeneous types molecular sieve catalyst hydroisomerizing cracking
The naphtha isomery hydrocarbon content arrived is high, boat product of coal freezing point is low, and diesel product condensation point is low, and tail oil product hydrocarbon isomer content is high, viscous
Degree index is big, condensation point is low；Arene content is low in hydrocracking tail oil, can be improved after continuing hydroisomerizing cracking plus hydrogen is different
The viscosity index (VI) of structure cracking tail oil；Therefore by this technique can meet respectively production different size naphtha, boat product of coal,
The needs of diesel product and tail oil product.
4, in the present invention, the liquid itself that weighted BMO spaces reactor obtains has very high temperature and pressure, is divided into
Two parts material, a portion material also have very high temperature through high pressure hot separator gas phase obtained after separation and liquid phase
And pressure, the influence that another part weighted BMO spaces material and high pressure hot separator obtain can be directly entered hydrocracking reaction
Device is reacted, and hydrocracking tail oil also has higher temperature after being fractionated tower, only need to can enter it after pump pressurization
It is reacted in hydroisomerizing cracker, and is not all had in the isolated liquid phase and hydrocracking tail oil of high pressure hot separator
There is NH3, temperature needed for hydroisomerizing cracking reaction can be greatly lowered in this way, i.e. mixing liquid material and recycle hydrogen are mixed
The requirement for being just able to satisfy hydroisomerizing cracking reaction temperature is closed, therefore weighted BMO spaces reactor may be implemented, be hydrocracked instead
Answer the coupling operation of device Yu hydroisomerizing cracker.
Detailed description of the invention
Fig. 1 is principle process schematic diagram of the invention.
Wherein: 1- feedstock oil, 2- weighted BMO spaces reactor, 3- weighted BMO spaces logistics, 4- hydrocracking raw material logistics,
5- high pressure hot separator feed stream, 6- hydrocracking reactor, 7- are hydrocracked logistics, 8- hydroisomerizing cracker,
9- hydroisomerizing cracked-stream, 10- are hydrocracked high-pressure separator, 11- hydroisomerizing cracking high-pressure separator, and 12- adds hydrogen to split
Change fractionating column, 13- hydroisomerizing cracking fractionating column, 14- is hydrocracked light naphtha product, and 15- is hydrocracked heavy naphtha production
Product, 16- are hydrocracked boat product of coal, and 17- is hydrocracked diesel product, 18- hydrocracking tail oil product, and 19- hydroisomerizing is split
Change light naphtha product, 20- hydroisomerizing cracking heavy naphtha product, 21- hydroisomerizing cracking boat product of coal, 22- add hydrogen different
Structure cracked diesel oil product, 23- hydroisomerizing cracking tail oil product, 24- are hydrocracked high-pressure separator hydrogen-rich gas, and 25- adds hydrogen
Isocraking high-pressure separator hydrogen-rich gas, 26- supplement hydrogen, 27- high pressure hot separator, 28- high pressure hot separator liquid phase, 29-
High pressure hot separator gas phase.
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 400~650 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.
Hydrogenation pretreatment catalyst described in step a is conventional wax oil hydrogenation pretreatment catalyst.Generally with VI B race
And/or group VIII metal be active component, using aluminium oxide or silicon-containing alumina as carrier, group VIB metal be generally Mo and/or
W, group VIII metal are generally Co and/or Ni.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 property is as follows: specific surface is 100~650m2/
0.15~0.6mL/g of g, Kong Rongwei.Main catalyst has 3936,3996, FF- that Fushun Petrochemical Research Institute develops
16, the hydrogenation pretreatment catalysts such as FF-26, FF-36, FF-46, FF-56 series are also possible to domestic and international catalyst Co. exploitation
Function similar to catalyst, such as HC-K, HC-P of Uop Inc., TK-555, TK-565 catalyst and Akzo of Topsoe company
KF-847, KF-848 etc. of company.Conventional operating condition can be used in operating condition, 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。
It is 5%~95%, preferably 10%~90% that gained liquid phase stream, which accounts for the weight percent of feedstock oil, in step a.
High pressure hot separator described in step a is typical separators, and operating pressure is reaction pressure, and temperature is plus hydrogen is located in advance
Stream outlet temperature is managed, or is no more than 50 DEG C lower than outlet temperature.
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.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, and molecular sieve content is 5wt%~80wt%.It is main to urge
Agent has the 3824 of Fushun Petrochemical Research Institute's development, 3825,3976, FC-12, FC-24, FC-26, FC-32, FC-
50 catalyst etc., HC-12, HC-14, HC-24, HC-39 etc. of Uop Inc..For hydrocracking catalyst, it is desirable that have
Certain hydrogenation activity and certain lytic activity should guarantee that hydrotreating generates in oil and hydrocracking process and generate in fraction
Alkene and aromatic hydrocarbons plus hydrogen saturation, the aromatic hydrocarbons after also requiring saturation the reaction of open loop occurs.The operating condition being hydrocracked can adopt
With conventional operating condition, generally are as follows: reaction pressure 3.0MPa~19.0MPa, reaction temperature are 300 DEG C~450 DEG C, body when liquid
Product air speed 0.2h-1~6.0h-1, hydrogen to oil volume ratio is 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.
Hydrocracking tail oil product described in step b, can fully enter hydroisomerizing cracker, can also portion
Divide and enter hydroisomerizing cracker, the tail oil into hydroisomerizing cracker accounts for obtain hydrocracking tail oil weight
10% ~ 100%, preferably 20% ~ 100%.
Hydroisomerizing Cracking catalyst described in step c is conventional wax oil hydrogenation isocraking catalyst.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 contains one of aluminium oxide, silicon-containing alumina and molecular sieve or a variety of, preferably contains and divides
Son sieve, the molecular sieve can be beta molecular sieve, Sapo type molecular sieve etc..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 5wt%~80wt%.FC-14, FC-20 etc. that main catalyst has Fushun Petrochemical Research Institute to develop.For adding
For hydrogen Cracking catalyst, it is desirable that have certain hydrogenation activity and certain lytic activity, should guarantee in reaction mass alkene and
Aromatic hydrocarbons adds hydrogen saturation, also requires linear paraffin that isomerization reaction occurs.The operating condition of hydroisomerizing cracking can be used conventional
Operating condition, generally are as follows: reaction pressure 3.0MPa~19.0MPa, reaction temperature are 300 DEG C~450 DEG C, volume space velocity when liquid
0.2h-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.
Light naphtha product and hydroisomerizing cracking light naphtha product are hydrocracked described in step b and step c
Mixing light naphtha product can also be mixed into separately as product.
Heavy naphtha product and hydroisomerizing cracking heavy naphtha product are hydrocracked described in step b and step c
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.
Described in step b and step c be hydrocracked diesel product and hydroisomerizing cracked diesel oil product can be independent
As product, mixed diesel product can also be mixed into.
A part of in hydrocracking tail oil described in step b can be 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: it is anti-that feedstock oil 1 is mixed into weighted BMO spaces with recycle hydrogen first
Device 2 is answered, weighted BMO spaces logistics 3 is divided into two parts, hydrocracking raw material logistics 4 and high pressure hot separator feed stream 5, and heat is high
Press separator feed stream 5 isolated high pressure hot separator liquid phase 28 and high pressure hot separator gas in high pressure hot separator 27
Phase 29, hydrocracking raw material logistics 4 and high pressure hot separator gas phase 29 and recycle hydrogen are mixed into hydrocracking reactor 6, warp
Hydrocracking catalyst bed is crossed to obtain being hydrocracked logistics 7, be hydrocracked logistics 7 enter be hydrocracked high-pressure separator 10 into
Row gas-liquid separation, isolated liquid enter fractionation in fractionating column 12 and obtain being hydrocracked light naphtha product 14, hydrogen is added to split
Change heavy naphtha product 15, is hydrocracked boat product of coal 16, is hydrocracked diesel product 17 and hydrocracking tail oil product 18, heat
High-pressure separator liquid phase 28 and hydrocracking tail oil 18 and recycle hydrogen are mixed into hydroisomerizing cracker 8, by adding hydrogen
Isocraking catalyst bed obtains hydroisomerizing cracked-stream 9, and hydroisomerizing cracked-stream 9 enters hydroisomerizing cracking high pressure
Gas-liquid separation is carried out in separator 11, isolated liquid enters fractionation in fractionating column 13 and obtains hydroisomerizing cracking pumice brain
Oil product 19, hydroisomerizing cracking heavy naphtha product 20, hydroisomerizing cracking boat product of coal 21, hydroisomerizing cracked diesel oil produce
Product 22 and hydroisomerizing cracking tail oil product 23, are hydrocracked light naphtha product 14 and hydroisomerizing cracking light naphtha product
19 can obtain mixing light naphtha product, be hydrocracked 15 He of heavy naphtha product separately as product after can also mixing
Hydroisomerizing cracking heavy naphtha product 20 can obtain mixing heavy naphtha product separately as product after can also mixing,
Being hydrocracked boat product of coal 16 and hydroisomerizing cracking boat product of coal 21 can be mixed after can also mixing separately as product
Boat product of coal is closed, being hydrocracked diesel product 17 and hydroisomerizing cracked diesel oil product 22 can be separately as product, can also be with
Mixed diesel product is obtained after mixing, is hydrocracked the isolated gas 24 of high-pressure separator 10 and hydroisomerizing cracking high pressure
The isolated gas 25 of separator 11 is mixed with supplement hydrogen 26 as recycle hydrogen after circulating hydrogen compressor is pressurized after mixing.
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-32 is that Sinopec Group Fushun petrochemical industry is ground
The catalyst for hydro-upgrading for studying carefully institute's development and production, contains Y type molecular sieve；Catalyst FC-20 is that Sinopec's share is limited
The hydroisomerizing Cracking catalyst of Fushun Petrochemical Research Institute, company development and production, contains beta molecular sieve.
The main character of 1 wax oil feedstock oil of table
2 embodiment process conditions of table
3 embodiment test result of table
Coupling technique is hydrocracked using of the invention it can be seen from embodiment, by will be divided into weighted BMO spaces logistics
Two parts, a portion logistics enter the isolated gas phase of high pressure hot separator and liquid phase, high pressure hot separator liquid phase and another
A part of weighted BMO spaces logistics passes through hydroisomerizing cracking catalysis by hydrocracking catalyst, high pressure hot separator liquid phase
Agent, while hydrocracking tail oil is some or all of by hydroisomerizing Cracking catalyst, i.e., adds hydrogen by using different type
Cracking catalyst produces heterogeneity hydrocracked product to realize, it is particularly possible to the purpose of High Quality Lube Base Oils is produced,
Production method is flexible.
Claims (14)
1. a kind of flexible method for hydrogen cracking for producing lube base oil, includes the following steps:
A, wax oil feedstock oil enters weighted BMO spaces reactor under the conditions of weighted BMO spaces first and is urged by weighted BMO spaces
Agent bed obtains weighted BMO spaces logistics, this part reaction stream is divided into two parts, and a portion enters thermal high separation
The isolated gas phase of device and liquid phase；
B, another part weighted BMO spaces logistics that step a is obtained and the isolated gaseous stream of high pressure hot separator are adding hydrogen
By the hydrocracking catalyst bed containing Y zeolite catalyst in hydrocracking reactor under cracking conditions, added
Hydrogen cracked-stream；Logistics is hydrocracked to be separated, be fractionated to obtain and be hydrocracked high pressure hydrogen-rich gas, be hydrocracked gas product,
It is hydrocracked fraction oil product and hydrocracking tail oil product；
C, after liquid phase stream obtained by step a is mixed with hydrocracking tail oil obtained by step b and recycle hydrogen, in hydroisomerizing cracking item
By the hydroisomerizing Cracking catalyst bed containing heterogeneous types molecular sieve catalyst under part, hydroisomerizing cracking object is obtained
Stream, hydroisomerizing cracked-stream are separated, are fractionated, and hydroisomerizing cracking high pressure hydrogen-rich gas, hydroisomerizing cracked gas are obtained
Product, hydroisomerizing cracked distillate oil product and hydroisomerizing cracking tail oil product.
2. flexible method for hydrogen cracking described in accordance with the claim 1, which is characterized in that further include step d: step b is obtained
It is recycled after being hydrocracked the hydroisomerizing cracking high pressure hydrogen-rich gas mixing that high pressure hydrogen-rich gas and step c are obtained.
3. flexible method for hydrogen cracking described in accordance with the claim 1, which is characterized in that the initial boiling point of the wax oil feedstock oil is
100~400 DEG C, the end point of distillation is 405~650 DEG C.
4. flexible method for hydrogen cracking 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 page
At least one of shale oil.
5. flexible method for hydrogen cracking 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 are active component, using aluminium oxide or silicon-containing alumina as carrier；With the poidometer of catalyst,
VI B race tenor is calculated as 10wt%~35wt% with oxide, and group VIII metal content is calculated as 3wt%~15wt% with oxide；
Its property is as follows: specific surface area is 100~650m20.15~0.6mL/g of/g, Kong Rongwei.
6. flexible method for hydrogen cracking described in accordance with the claim 1, 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 to oil volume ratio is 100:1~2000:1.
7. flexible method for hydrogen cracking described in accordance with the claim 1, which is characterized in that gained liquid phase stream accounts for original in step a
The weight percent of material oil is 5%~95%, preferably 10%~90%.
8. flexible method for hydrogen cracking according to claim 7, which is characterized in that enter hydroisomerizing cracking in step c
The hydrocracking tail oil of reactor accounts for 10%~100% of hydrocracking tail oil weight obtained by step b, and preferably 20%~100%.
9. flexible method for hydrogen cracking described in accordance with the claim 1, which is characterized in that the hydrocracking catalyst is with
VI B race and/or group VIII metal are active component；Catalyst carrier contains Y molecular sieve；With the poidometer of catalyst, group VIB
Tenor is calculated as 10wt%~35wt% with oxide, and group VIII metal content is calculated as 3wt%~15wt%, Y molecule with oxide
Sieve content is 5wt%~80wt%.
10. flexible method for hydrogen cracking described in accordance with the claim 1, which is characterized in that the 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.
11. flexible method for hydrogen cracking described in accordance with the claim 1, which is characterized in that the hydroisomerizing cracking catalysis
Using group VIB and/or group VIII metal as active component, catalyst carrier contains molecular sieve for agent, and the molecular sieve is β type molecule
Sieve or Sapo type molecular sieve；With the poidometer of catalyst, group VIB tenor is calculated as 10wt%~35wt% with oxide, the
VIII race's tenor is calculated as 3wt%~15wt% with oxide, and molecular sieve content is 5wt%~80wt%.
12. flexible method for hydrogen cracking described in accordance with the claim 1, which is characterized in that the hydroisomerizing cracking conditions
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. flexible method for hydrogen cracking described in accordance with the claim 1, which is characterized in that be hydrocracked and evaporate described in step b
Dividing oil product includes being hydrocracked light naphtha product, being hydrocracked heavy naphtha product, be hydrocracked boat product of coal and add hydrogen
Cracked diesel oil product.
14. flexible method for hydrogen cracking described in accordance with the claim 1, which is characterized in that hydroisomerizing described in step c is split
Changing fraction oil product includes that hydroisomerizing cracking light naphtha product, hydroisomerizing cracking heavy naphtha product, hydroisomerizing are split
Change boat product of coal and hydroisomerizing cracked diesel oil product.
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Effective date of registration: 20230911 Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec (Dalian) Petrochemical Research Institute Co.,Ltd. Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: DALIAN RESEARCH INSTITUTE OF PETROLEUM AND PETROCHEMICALS, SINOPEC Corp. |