CN109988605A - A kind of flexible hydrocracking process producing lube base oil - Google Patents
A kind of flexible hydrocracking process producing lube base oil Download PDFInfo
- Publication number
- CN109988605A CN109988605A CN201711468915.5A CN201711468915A CN109988605A CN 109988605 A CN109988605 A CN 109988605A CN 201711468915 A CN201711468915 A CN 201711468915A CN 109988605 A CN109988605 A CN 109988605A
- Authority
- CN
- China
- Prior art keywords
- oil
- product
- hydrocracking
- hydroisomerizing
- catalyst
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000004517 catalytic hydrocracking Methods 0.000 title claims abstract description 104
- 238000000034 method Methods 0.000 title claims abstract description 55
- 230000008569 process Effects 0.000 title claims abstract description 41
- 239000002199 base oil Substances 0.000 title claims abstract description 16
- 239000003921 oil Substances 0.000 claims abstract description 123
- 239000003054 catalyst Substances 0.000 claims abstract description 87
- 238000005336 cracking Methods 0.000 claims abstract description 74
- 239000002808 molecular sieve Substances 0.000 claims abstract description 48
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 48
- 239000003245 coal Substances 0.000 claims abstract description 31
- 238000006243 chemical reaction Methods 0.000 claims abstract description 24
- 238000002156 mixing Methods 0.000 claims abstract description 16
- 239000002283 diesel fuel Substances 0.000 claims abstract description 13
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 13
- 229910052739 hydrogen Inorganic materials 0.000 claims description 55
- 239000001257 hydrogen Substances 0.000 claims description 55
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 53
- 239000007789 gas Substances 0.000 claims description 29
- 229910052751 metal Inorganic materials 0.000 claims description 18
- 239000002184 metal Substances 0.000 claims description 18
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 16
- 238000004519 manufacturing process Methods 0.000 claims description 16
- 239000003795 chemical substances by application Substances 0.000 claims description 8
- 229910021536 Zeolite Inorganic materials 0.000 claims description 6
- 238000006555 catalytic reaction Methods 0.000 claims description 6
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 6
- 239000010457 zeolite Substances 0.000 claims description 6
- WURBVZBTWMNKQT-UHFFFAOYSA-N 1-(4-chlorophenoxy)-3,3-dimethyl-1-(1,2,4-triazol-1-yl)butan-2-one Chemical compound C1=NC=NN1C(C(=O)C(C)(C)C)OC1=CC=C(Cl)C=C1 WURBVZBTWMNKQT-UHFFFAOYSA-N 0.000 claims description 5
- 230000008859 change Effects 0.000 claims description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 claims description 4
- 239000010703 silicon Substances 0.000 claims description 4
- 229910052710 silicon Inorganic materials 0.000 claims description 4
- 241000269350 Anura Species 0.000 claims description 3
- 238000009835 boiling Methods 0.000 claims description 3
- 230000003197 catalytic effect Effects 0.000 claims description 2
- 239000011280 coal tar Substances 0.000 claims description 2
- 238000004821 distillation Methods 0.000 claims description 2
- 239000003079 shale oil Substances 0.000 claims description 2
- 239000007788 liquid Substances 0.000 abstract description 12
- 239000002994 raw material Substances 0.000 abstract description 12
- 239000000463 material Substances 0.000 abstract description 9
- 238000005194 fractionation Methods 0.000 abstract description 6
- 238000000926 separation method Methods 0.000 abstract description 4
- 239000000047 product Substances 0.000 description 142
- 238000005516 engineering process Methods 0.000 description 14
- 239000001993 wax Substances 0.000 description 14
- 239000004215 Carbon black (E152) Substances 0.000 description 11
- 229930195733 hydrocarbon Natural products 0.000 description 11
- 150000002430 hydrocarbons Chemical class 0.000 description 11
- 238000009833 condensation Methods 0.000 description 10
- 230000005494 condensation Effects 0.000 description 10
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 8
- 239000012263 liquid product Substances 0.000 description 7
- 238000002360 preparation method Methods 0.000 description 6
- 238000011160 research Methods 0.000 description 6
- 238000011161 development Methods 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 4
- 239000005977 Ethylene Substances 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000004230 steam cracking Methods 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 3
- 239000007795 chemical reaction product Substances 0.000 description 3
- 239000002131 composite material Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000006317 isomerization reaction Methods 0.000 description 2
- 230000002101 lytic effect Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000003223 protective agent Substances 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 239000011959 amorphous silica alumina Substances 0.000 description 1
- 210000004556 brain Anatomy 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 125000000753 cycloalkyl group Chemical group 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000004069 differentiation Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 125000003367 polycyclic group Chemical group 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000007142 ring opening reaction Methods 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Classifications
-
- 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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- 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 hydrocracking process for producing lube base oil.Material of the wax oil raw material after weighted BMO spaces is divided into two strands；One material carries out hydrocracking reaction by the hydrocracking catalyst bed containing Y type molecular sieve under hydrogenation process conditions；Another strand of material enters the hydroisomerizing Cracking catalyst bed containing heterogeneous molecular sieve after mixing with hydrocracking tail oil, and hydroisomerizing cracking reaction is carried out under hydrogenation process conditions；Gained hydrocracking reaction material and hydroisomerizing cracking reaction material carry out gas-liquid separation and fractionation respectively, obtain the naphtha, distillate and tail oil of different size, and hydrocracking tail oil is some or all of to be recycled into isocraking reactor.Present invention process can produce two or more different size naphthas, lattice boat coal, diesel oil, tail oil product, the flexible hydrocracking process for especially producing High Quality Lube Base Oils simultaneously on a set of hydrogenation technique device.
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,
Diesel oil, tail oil product especially produce the hydrocracking process of 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
Different to be divided into different types of catalyst again, main Cracking Component includes amorphous silica-alumina, Y type molecular sieve, β type molecule
Sieve, SAPO Series Molecules sieve and ZSM-5 molecular sieve etc..A group timesharing, obtained light-end products are hydrocracked using different type
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；Using the hydrocracking technology containing Y-isomery complex type molecular sieve catalysis, or
Gradation is hydrocracked skill using 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 isomeric types with containing Y-isomery complex type molecular sieve catalysis or gradation
The tail oil that type molecular sieve hydrocracking catalyst obtains can be used as the raw material of preparing ethylene by steam cracking or as high-quality lubrication
The raw material of oil base oil.When above-mentioned several hydrocracking process therefore are used alone, it can only select as needed different types of
Hydrocracking catalyst, perhaps using two kinds of hydrocracking catalyst gradations of two kinds of molecular sieve composite catalysts or selection
It uses, 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 production lube base oil flexible hydrocracking process, i.e.,
By from weighted BMO spaces product stream be divided into two parts be hydrocracked respectively with hydroisomerizing cracking, wherein being hydrocracked
The tail oil that reactor obtains is some or all of to go successively to hydroisomerizing cracker, and the wax oil feedstock oil is passed through
Y type hydrocracking catalyst is hydrocracked flexibly to be produced with heterogeneous types hydrocracking catalyst hydroisomerizing cracking combined method
The preparing ethylene by steam cracking raw material of high quality, the naphtha product of High Quality Lube Base Oils raw material and plurality of specifications and high-quality horse
Up to fuel product.
The flexible hydrocracking process 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；
B, a part of weighted BMO spaces logistics that step a is obtained is under hydrocracking condition by containing in hydrocracking reactor
The hydrocracking catalyst bed of Y zeolite catalyst, obtains being hydrocracked logistics；Logistics is hydrocracked to be separated, be fractionated,
It obtains being hydrocracked high pressure hydrogen-rich gas, is hydrocracked gas product, is hydrocracked fraction oil product and hydrocracking tail oil production
Product；
C, after the resulting another part weighted BMO spaces logistics of step a is mixed with the resulting hydrocracking tail oil of step b, adding hydrogen
Pass through the hydroisomerizing cracking containing heterogeneous types molecular sieve catalyst in hydroisomerizing cracker under the conditions of isocraking
Catalyst bed, obtains hydroisomerizing cracked-stream, and hydroisomerizing cracked-stream is separated, is fractionated to obtain hydroisomerizing cracking height
Press hydrogen-rich gas, hydroisomerizing cracked gas product, hydroisomerizing cracked distillate oil product and hydroisomerizing cracking tail oil product.
Hydrocracking process 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 certain
It is obtained in degree plus hydrogen saturation, a part of weighted BMO spaces logistics continues through being hydrocracked containing Y zeolite catalyst
Cyclic hydrocarbon generating unit divides ring-opening reaction when catalyst bed, and macromolecular is cracked into small molecule, and Y type molecular sieve has preferential cracking big
The characteristics of molecule polycyclic cyclic hydrocarbon, available high normal hydrocarbon content, arene content low boat product of coal, diesel product and tail oil
Product；Another part weighted BMO spaces stream is subsequent by the hydroisomerizing Cracking catalyst containing heterogeneous types molecular sieve catalyst
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, is in addition hydrocracked
Tail oil continues hydroisomerizing cracking, can increase the isoparaffin content of tail oil product, reduces arene content and polycyclic ring
The content of alkane further increases the viscosity index (VI) of hydroisomerizing cracking tail oil.
Compared with prior art, the flexible hydrocracking process of production lube base oil of the invention the advantages of
In:
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, then adds obtained material by different
Hydrogen process, so as to flexibly produce the purpose product of different size, especially hydrocracking tail oil passes through hydroisomerizing
Available High Quality Lube Base Oils produce after the isocraking catalyst of molecular sieve containing heterogeneous types in cracker
Product.And in the prior art, although by adjusting the available a variety of light-end products of boiling range of conversion ratio and adjustment product,
Since only one hydrocracking reactor exports, a set of same fraction range of hydrocracking unit is typically only capable to a type
Light naphthar, heavy naphtha product, boat product of coal, diesel product and the tail oil product of type；If it is intended to obtaining different size
Hydrocracked product needs two sets or more of hydrocracking unit.Therefore, the present invention provides one kind for the first time and splits in a set of plus hydrogen
Two or more same fraction ranges are produced simultaneously on chemical industry process and equipment, but different size tail oil product, two or more different sizes
The hydrocracking process of boat product of coal, two or more different size diesel products and a variety of different size naphtha products.
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 be respectively fed to the hydrocracking reactor being separately provided and carry out hydrocracking reaction and enter hydroisomerizing cracking
Reactor carries out hydroisomerizing cracking reaction, and makes hydrocracking tail oil is some or all of to enter hydroisomerizing cracking reaction
Device so that method of the invention can flexibly produce different arene contents, different isomerization hydrocarbon content, different condensation point stone brain
Oil product, 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, Ke Yizhi
It taps into hydrocracking reactor and hydroisomerizing cracker and is reacted, and after hydrocracking tail oil is fractionated tower
There is higher temperature, it need to can only be entered in hydroisomerizing cracker after pump pressurization and be reacted, thus sufficiently
Using heat entrained by several strands of materials, realize that weighted BMO spaces reactor, hydrocracking reactor and hydroisomerizing cracking are anti-
Answer the coupling operation of device.
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- hydroisomerizing cracked stock logistics, 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.
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, 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；Its property is as follows: specific surface area 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 catalyst of Akzo company etc..Conventional operating condition can be used in operating condition, 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
Than for 100:1~2000:1.
Account for the weight hundred of feedstock oil in step b with level meter by the weighted BMO spaces logistics of hydrocracking catalyst bed
Divide than being 5%~95%, preferably 10%~90%.
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 or more in aluminium oxide, silicon-containing alumina and molecular sieve, preferably contains molecular sieve, and described point
Son sieve can be Y type molecular sieve.With the poidometer of catalyst, group VIB tenor is calculated as 10wt%~35wt% with oxide,
Group VIII metal content is calculated as 3wt%~15wt% with oxide, and molecular sieve content is 5wt%~80wt%.Main catalyst has
Fushun Petrochemical Research Institute develop 3824,3825,3976, FC-12, FC-24, FC-26, FC-32, FC-50 catalysis
Agent 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 hydrotreating generate oil and hydrocracking process in generate fraction in alkene and
Aromatic hydrocarbons adds hydrogen saturation, and the reaction of open loop occurs for the aromatic hydrocarbons after also requiring saturation.Routine can be used in the operating condition being hydrocracked
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 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.
Obtained hydrocracking tail oil product, can fully enter hydroisomerizing cracker in step b, can also be with
Part enters hydroisomerizing cracker.Wherein, it accounts for obtain into the tail oil of hydroisomerizing cracker and is hydrocracked tail
The weight percent of oil is 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.
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.
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 hydroisomerizing cracked stock logistics 5, adds hydrogen
Cracked stock logistics 4 and hydrogen are mixed into hydrocracking reactor 6, are hydrocracked by hydrocracking catalyst bed
Logistics 7 is hydrocracked logistics 7 into high-pressure separator 10 is hydrocracked and carries out gas-liquid separation, and isolated liquid, which enters, to be divided
Fractionation in tower 12 is evaporated to obtain being hydrocracked light naphtha product 14, be hydrocracked heavy naphtha product 15, be hydrocracked boat coal production
Product 16 are hydrocracked diesel product 17 and hydrocracking tail oil product 18, hydroisomerizing cracked stock logistics 5 and are hydrocracked tail
Continue to be mixed into hydroisomerizing cracker 8 with hydrogen after 18 mixing of oil, be obtained by hydroisomerizing Cracking catalyst bed
To hydroisomerizing cracked-stream 9, hydroisomerizing cracked-stream 9, which enters, carries out gas-liquid point in hydroisomerizing cracking high-pressure separator 11
Enter in fractionating column 12 that fractionation obtains hydroisomerizing cracking light naphtha product 19, hydroisomerizing is split from, isolated liquid
Change heavy naphtha product 20, hydroisomerizing cracking boat product of coal 21, hydroisomerizing cracked diesel oil product 22 and hydroisomerizing cracking
Tail oil product 23, is hydrocracked light naphtha product 14 and hydroisomerizing cracking light naphtha product 19 can be separately as production
Product obtain mixing light naphtha product, are hydrocracked heavy naphtha product 15 and hydroisomerizing cracking scheelite after can also mixing
Naphtha product 20 can obtain mixing heavy naphtha product, be hydrocracked boat product of coal separately as product after can also mixing
16 and hydroisomerizing cracking boat product of coal 21 can separately as product, be obtained after can also mixing mixing boat product of coal, add hydrogen
Cracked diesel oil product 17 and hydroisomerizing cracked diesel oil product 22 can obtain mixing bavin separately as product after can also mixing
Oil product, is hydrocracked the isolated gas 24 of high-pressure separator 10 and hydroisomerizing cracking high-pressure separator 11 is isolated
Gas 25 mix after after circulating hydrogen compressor is pressurized with supplement hydrogen 24 mix be used as recycle hydrogen.
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 process conditions of table
3 test result of table
Using flexible hydrocracking process of the invention it can be seen from embodiment, by by weighted BMO spaces reactant flow point
At two parts, using some or all of progress hydroisomerizing cracking of hydrocracking tail oil, while hydrocracking catalyst is used
Production heterogeneity hydrocracked product is realized with hydroisomerizing Cracking catalyst, it is particularly possible to produce high-quality lube base
Oil, production method are flexible.
Claims (14)
1. a kind of flexible hydrocracking process 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；
B, a part of weighted BMO spaces logistics that step a is obtained is under hydrocracking condition by containing in hydrocracking reactor
The hydrocracking catalyst bed of Y zeolite catalyst, obtains being hydrocracked logistics；Logistics is hydrocracked to be separated, be fractionated
It obtains being hydrocracked high pressure hydrogen-rich gas, is hydrocracked gas product, is hydrocracked fraction oil product and hydrocracking tail oil production
Product；
C, after the resulting another part weighted BMO spaces logistics of step a is mixed with the resulting hydrocracking tail oil of step b, adding hydrogen
Pass through the hydroisomerizing cracking containing heterogeneous types molecular sieve catalyst in hydroisomerizing cracker under the conditions of isocraking
Catalyst bed, obtains hydroisomerizing cracked-stream, and hydroisomerizing cracked-stream is separated, is fractionated to obtain hydroisomerizing cracking height
Press hydrogen-rich gas, hydroisomerizing cracked gas product, hydroisomerizing cracked distillate oil product and hydroisomerizing cracking tail oil product.
2. flexible hydrocracking process 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 hydrocracking process 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 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 page
At least one of shale oil.
5. flexible hydrocracking process 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 hydrocracking process 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 hydrocracking process described in accordance with the claim 1, which is characterized in that pass through hydrocracking catalyst in step b
The weighted BMO spaces logistics of agent bed accounts for the weight ratio of feedstock oil with level meter as 5%~95%.
8. flexible hydrocracking process described in accordance with the claim 1, 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 hydrocracking process 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 hydrocracking process 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 hydrocracking process 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.
12. flexible hydrocracking process 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%.
13. flexible hydrocracking process 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.
14. flexible hydrocracking process 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711468915.5A CN109988605B (en) | 2017-12-29 | 2017-12-29 | Flexible hydrocracking process for producing lubricating oil base oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711468915.5A CN109988605B (en) | 2017-12-29 | 2017-12-29 | Flexible hydrocracking process for producing lubricating oil base oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109988605A true CN109988605A (en) | 2019-07-09 |
| CN109988605B CN109988605B (en) | 2021-07-09 |
Family
ID=67109020
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711468915.5A Active CN109988605B (en) | 2017-12-29 | 2017-12-29 | Flexible hydrocracking process for producing lubricating oil base oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109988605B (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101724457A (en) * | 2008-10-29 | 2010-06-09 | 中国石油化工股份有限公司 | Hydrogenation combined method for diesel oil |
| CN103387847A (en) * | 2012-05-10 | 2013-11-13 | 中国石油化工股份有限公司 | Production method of lube base oil |
| CN103627433A (en) * | 2012-08-23 | 2014-03-12 | 中国石油化工股份有限公司 | Hydrogenation method for producing lubricant basic oil with low pour point and high viscosity index |
-
2017
- 2017-12-29 CN CN201711468915.5A patent/CN109988605B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101724457A (en) * | 2008-10-29 | 2010-06-09 | 中国石油化工股份有限公司 | Hydrogenation combined method for diesel oil |
| CN103387847A (en) * | 2012-05-10 | 2013-11-13 | 中国石油化工股份有限公司 | Production method of lube base oil |
| CN103627433A (en) * | 2012-08-23 | 2014-03-12 | 中国石油化工股份有限公司 | Hydrogenation method for producing lubricant basic oil with low pour point and high viscosity index |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109988605B (en) | 2021-07-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109988629B (en) | Wax oil hydrocracking method and system | |
| CN109988606B (en) | Flexible reverse hydrocracking process | |
| CN109988609B (en) | Flexible shale oil hydrocracking process | |
| CN109988641B (en) | Flexible shale oil hydrocracking process | |
| CN109988648A (en) | A kind of flexibly production H-G hydrocracking technique | |
| CN109988623B (en) | Flexible reverse hydrocracking process | |
| CN109988610A (en) | A kind of flexible two-segment hydrocracking method | |
| CN109988620A (en) | Produce the flexible hydrocracking process of lube base oil | |
| CN109988642A (en) | Produce the flexible method for hydrogen cracking of lube base oil | |
| CN109988621A (en) | Flexible hydrocracking process | |
| CN109988611A (en) | The flexibly hydrocracking process of production diesel oil | |
| CN109988605A (en) | A kind of flexible hydrocracking process producing lube base oil | |
| CN109988640A (en) | A kind of flexible hydrocracking process | |
| CN109988636B (en) | Flexible single stage hydrocracking process | |
| CN109988618B (en) | Flexible single-stage two-agent hydrocracking process | |
| CN109988628A (en) | A kind of flexible single-stage hydrocracking technique | |
| CN109988647B (en) | Flexible single-stage two-agent hydrocracking process | |
| CN109988617A (en) | Flexible two-segment hydrocracking method | |
| CN109988635A (en) | A kind of hydrotreating and hydrocracking combined process | |
| CN109988607A (en) | Flexible two-stage reforming technique | |
| CN109988603A (en) | Produce the hydrogenation coupling process of low freezing point diesel fuel | |
| CN109988625A (en) | A kind of hydrofinishing and hydrocracking combined process | |
| CN109988626B (en) | Flexible two-stage hydrocracking process | |
| CN109988601A (en) | A kind of hydrogenation technique of flexible production low freezing point diesel fuel | |
| CN109988599A (en) | A kind of flexible hydrogenation modifying process of poor ignition quality fuel |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20231018 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. |
|
| TR01 | Transfer of patent right |