CN109988614A - A kind of flexible residual hydrocracking technique - Google Patents
A kind of flexible residual hydrocracking technique Download PDFInfo
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- CN109988614A CN109988614A CN201711468990.1A CN201711468990A CN109988614A CN 109988614 A CN109988614 A CN 109988614A CN 201711468990 A CN201711468990 A CN 201711468990A CN 109988614 A CN109988614 A CN 109988614A
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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
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Abstract
The invention discloses a kind of flexible residual hydrocracking techniques.Residual oil raw material enters the first hydrotreating reaction area after mixing with hydrogen, is divided into two strands by the material after upstream protective agent and hydrotreating catalyst bed；One material is extracted out the first hydrotreating reaction area among bed, and is mixed into the second hydrotreating reaction area with LCO and is carried out hydrogenation reaction；Another strand of material continues to flow downwardly through the hydrogenation catalyst bed in downstream, and the first hydrotreating reaction material and the second hydrotreating reaction material carry out gas-liquid separation and fractionation, obtain naphtha, diesel oil and add hydrogen heavy distillat etc..The present invention provides one kind to process different material oil on a set of hydrogenation plant, flexibly to produce the hydroprocessing technique of fine quality catalytic cracking raw material.
Description
Technical field
The invention belongs to petroleum refining fields, and in particular to one kind flexibly produces high-quality urge as feedstock oil using residual oil and LCO
Change the flexible hydroprocessing technique of cracked stock.
Background technique
Fluid catalytic cracking (FCC) is one of the important means of light materialization of heavy oil, but with catalyzed cracking processing original
The in poor quality and heaviness of material, operating condition is more and more harsher, and light-end products yield and product property are deteriorated, and catalytic cracking
Raw material hydrotreating techniques not only can remove sulphur, nitrogen, metal impurities content, can also improve the cracking performance of charging, drop
Low FCC operating severity improves product distribution, improves purpose product selectivity, reduces dry gas and coke yield, improves FCC dress
The economy set reduces purpose product sulfur content, reduces SOx and NOx content etc. in regenerated flue gas.Catalytic cracking light cycle oil
(LCO) sulphur and nitrogen for containing certain content in, exist in the form of organic compound, and arene content is high, and especially two
The content of the above aromatic hydrocarbons of ring is high, and usual LCO is recycled directly back to continue to convert in catalytic cracking unit, or enters hydrotreating and fill
It sets and enters back into catalytic cracking unit after adding hydrogen, either enter other devices and process or directly as product.
CN106701189A, CN106701190A, CN106701191A and CN102732314A disclose a kind of residual oil and add
The technology of refining LCO and/or heavy-cycle oil is mixed in hydrogen treatment process, main purpose is production fine quality catalytic cracking raw material, or
The Combined machining technology that person allows LCO to recycle between residual hydrocracking device and catalytic cracking unit realizes catalytic cracking unit
Clean manufacturing, but direct hydrogenation after being mixed due to residual oil with LCO, the hydrogenation depth of LCO not can be effectively controlled, can only be with mixed
The sulfur content or nitrogen content for closing hydrogenation products (catalytically cracked material) are unfavorable for producing high-quality vapour with LCO as control target
Effective control of oil.
It is usually all that LCO directly mixes refining in conclusion comparing existing LCO hydrogen addition technology and residual hydrocracking technology
Carried out into residual hydrocracking device plus hydrogen, the hydrogenated residue that is obtained after mixed hydrogenation and plus hydrogen LCO split collectively as catalysis
Disguise the raw material set, i.e. LCO returns again to catalytic cracking unit after adding hydrogen, and due to not controlling the hydrogenation depth of LCO deliberately, catalysis is split
Change quality of gasoline and do not reach best, and without the Combined machining technology of reaction mass coupling.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of flexible residual hydrocracking technique.By from using first
The residual oil raw material oil and LCO feedstock oil are passed through at least two by extraction section reaction stream in the middle part of hydrotreating reaction area
The group technology in hydrotreating reaction area produces fine quality catalytic cracking raw material.
A kind of flexible residual hydrocracking technique of the invention, includes the following steps:
A, residual oil raw material oil passes through upstream protective agent and gradation in the first hydrotreating reaction area under hydroprocessing conditions first
Hydrotreating catalyst bed obtains the first hydrotreating logistics, this part reaction stream is divided into two parts, and a portion is taken out
First hydrotreating reaction area out；
B, the first hydrotreating logistics continuation of remainder is anti-by the first hydrotreating under hydroprocessing conditions in step a
The gradation hydrotreating catalyst bed in the downstream Ying Qu obtains the first hydrotreating reaction area product stream by separation, fractionation
The first hydrogenation gas product, the first hydrotreated naphtha product, the first hydrogenated diesel oil and first plus hydrogen double distilled are obtained after (or stripping)
Point；
C, in hydrotreating after the first hydrotreating logistics in the first hydrotreating reaction area of extraction obtained by step a is mixed with LCO
Under the conditions of by the gradation hydrotreating catalyst bed in the second hydrotreating reaction area, it is raw to obtain the second hydrotreating reaction area
The second hydrogenation gas product, the second hydrotreated naphtha product, second plus hydrogen are obtained after separation, fractionation (or stripping) at logistics
Diesel oil and second adds hydrogen heavy distillat.
Flexible residual hydrocracking technique according to the present invention, wherein the first hydrotreating reaction area that step b is obtained is raw
The the second hydrotreating reaction area obtained at logistics and step c is separated after generating logistics mixing, is fractionated (or stripping), is obtained
Hydrogenation gas product, hydrotreated naphtha product, hydrogenated diesel oil and plus hydrogen heavy distillat.That is, separation described in step b and step c
A set of separation and fractionating system are shared with fractionation.High pressure hydrogen-rich gas obtained by step b and step c is recycled.
The requirement of product quality, environmental requirement, technological operation etc. all carries out the raw material oil nature of catalytic cracking unit
Limitation, the especially limitation of sulfur content, and due to the difference of feedstock oil composition, the distribution of catalytic cracking product and property also have
Biggish difference；Research shows that: the aromatic hydrogenation saturation depth of LCO is affected to fcc gasoline product quality, especially
It is that mononuclear aromatics is antiknock component in gasoline, increases and the content of mononuclear aromatics in hydrogen LCO is added to can be increased catalytic cracking
The octane number of gasoline, and the first hydrotreating logistics extracted out is reacted because having already been through partial hydrogenation, adds the reduction of hydrogen difficulty, because
This its mixed with LCO after can achieve the purpose that hydrodesulfurization, hydrodenitrogeneration under the operating condition relatively mitigated, and at this time just
Can control the hydrogenation depth of LCO, i.e., under the premise of meeting sulfur content by LCO two cycloaromatics and polycyclic aromatic hydrocarbon add hydrogen extremely
Mononuclear aromatics, rather than hydrogenation depth excessively generates cycloalkane or hydrogenation depth deficiency and generates two cycloaromatics, adds in this way
Treated that the content of Aromatics in Fcc Naphtha can be improved when product is re-introduced into catalytic cracking unit for hydrogen, to mention
The octane number of high catalytically cracked gasoline.
Compared with prior art, the advantages of flexible residual hydrocracking technique of the invention, is:
It 1, include at least two gradation hydrotreating catalyst beds in the first hydrotreating reaction area in the present invention.By setting
The first processing material extraction step among specific bed is set, special operation is not necessarily to, can be realized to the first hydrotreating object
Expect effective distribution of stock, then make obtained material by hydrogenation combination technique, so as to produce good purpose product.Together
When, abstraction reaction logistics is technically also to be easily achieved among reactor bed.And in the prior art, LCO is usual
It is directly mixed into a hydrotreating reactor with residual oil raw material oil and directly produces catalytically cracked material.
2, the present invention is by being arranged the first hydrotreating among the special catalyst bed in the first hydrotreating reaction area
Logistics withdrawing device, the first hydrotreating logistics by residual oil raw material Jing Guo the first hydrotreating extract reactor, and by its
The second hydrotreating reactor be sent into and be separately provided is mixed with LCO and carries out hydrogenation reaction, since some residual oil is former
The impurity such as sulphur, nitrogen in material have been hydrogenated removing, therefore further add the difficulty of hydrogen to reduce, therefore can control reaction condition
Control the hydrogenation depth of LCO, i.e. the depth that two cycloaromatics and polycyclic aromatic hydrocarbon add hydrogen to be saturated in control LCO, control as far as possible will
The a lot of cycloaromatics of two cycloaromatics add hydrogen to mononuclear aromatics, and LCO after hydrogen will be added to carry out reducing reaction hardly possible when catalytic cracking again in this way
Arene content in degree or raising catalytically cracked gasoline, improves the octane number of gasoline, and LCO can also dilute residual oil, drops
The difficulty of low residual hydrogenation reaction.
3, in the present invention, the extraction logistics sheet that is obtained among the first hydrotreating reaction area hydrogenation pretreatment catalyst bed
Body has very high temperature and pressure, can be directly entered in newly-installed second hydrotreating reactor after mixing with LCO
It is reacted, so that this thigh be made full use of to divide heat entrained by hydrotreated material, realizes the first hydrotreating reactor
With the coupling operation of the second hydrotreating reactor.
4, in the present invention, the first hydrotreating reaction system is identical with the operating pressure of the second hydrotreating reaction system,
Therefore a set of hydrogen desulphurization system and a set of hydrogen gas circulating system can be used in the high pressure hydrogen-rich gas in two systems, if into one
Step two systems share a set of separation, fractionation (or stripping) system, then can significantly save equipment investment and operating cost.
Detailed description of the invention
Fig. 1 is principle process schematic diagram of the invention.
Fig. 2 is another principle process schematic diagram of the invention.
Wherein: logistics is extracted in 1- residual oil raw material oil, the first hydrotreating reaction of 2- area, the first hydrotreating of 3- out, and 4-LCO is former
Material oil, 5- the first hydrotreating reactor recycle hydrogen, the first hydrotreating reactor of 6- generate logistics, and the second hydrotreating of 7- is anti-
Area is answered, the second hydrotreating reactor of 8- generates logistics, the second high-pressure separator of 9-, 10- after-fractionating tower, 11- second plus hydrogen
Handle naphtha, the second hydroprocessed diesel of 12-, 13- the second hydrotreating heavy distillate, 14- the second high-pressure separator hydrogen-rich
Gas, 15- supplement hydrogen, the first high-pressure separator of 16-, the first fractionating column of 17-, the first hydrotreated naphtha of 18-, 19- first
Hydroprocessed diesel, 20- the first hydrotreating heavy distillate, 21- the first high-pressure separator hydrogen-rich gas, 22- mixed high-voltage point
From device, 23- mixing fractionating column, 24- mixed hydrogenation handles naphtha, and 25- mixed hydrogenation handles diesel oil, the processing of 26- mixed hydrogenation
Heavy distillate, 27- mixed high-voltage separator hydrogen-rich gas.
Specific embodiment
The initial boiling point of residual oil raw material described in step a is 200~450 DEG C, and the end point of distillation is 550~750 DEG C.The residual oil is former
Material oil can be one of reduced crude, decompression residuum, coking heavy oil, deasphalted oil, recycle oil that PETROLEUM PROCESSING obtains etc.,
One of coal tar, coal direct liquefaction oil, ICL for Indirect Coal Liquefaction oil, synthesis residual oil, shale oil for obtaining from coal etc., are also possible to
Their wherein several miscellas.
Step a, protective agent, hydrotreating catalyst described in step b and step c are that conventional residual hydrogenation series is urged
Agent mainly includes hydrogenation protecting agent, hydrodemetallization agent, Hydrobon catalyst, removal of ccr by hydrotreating catalyst etc..Hydrogen is added to urge
Hydrogenation active component is one or more of Co, Mo, W, Ni in agent, and the weight content in terms of oxide is 5%~70%, is added
The carrier of hydrogen catalyst is generally aluminium oxide, amorphous silicon aluminium, silica, titanium oxide etc., while can contain other auxiliary agents, such as
P, Si, B, Ti, Zr etc..Commercial catalyst can be used, can also be prepared by this field existing method.Hydrogenation active component is oxygen
The catalyst for changing state, carries out conventional vulcanizing treatment before the use, hydrogenation active component is made to be converted into sulphided state.Business plus hydrogen
Catalyst mainly has, as the FZC-1 series protective agent of Fushun Petrochemical Research Institute (FRIPP) development, FZC-2 series are de-
Metallic catalyst, FZC-3 series desulphurization catalyst, FZC-4 series take off the hydrogenation catalysts such as carbon residue catalyst, Inst Francais Du Petrole
The hydrogenation catalysts such as HMC945, HMC841, the RF catalyst series and R catalyst series of Uop Inc.'s exploitation, AKZO company
KFR series is participated in, the HT catalyst series of Axen company exploitation and the TK catalyst series etc. of Haldor Topsoe company exploitation
Hydrogenation catalyst step.Catalyst system described in step b and step c can be used identical catalyst grade and match system, can also
Match system with different catalyst grades.In terms of feedstock oil and hydrogen mixture flow direction, the principle of catalyst grading loading is,
Granularity is descending, and catalyst activity is from low to high.
Operating condition described in step a can be used conventional operating condition, and generally reaction pressure 5.0MPa~
19.0MPa, reaction temperature are 300 DEG C~450 DEG C, volume space velocity 0.05h when liquid-1~5.0h-1, hydrogen to oil volume ratio be 100:1~
2000:1。
A reactor can be set in first hydrotreating reaction area described in step a, and more reactors also can be set,
Such as 2 ~ 8.
It is Hydrodemetalation catalyst and plus hydrogen that catalyst position is corresponded to when the part reaction stream of extraction described in step a
Any position between de- carbon residue catalyst bed, it can be connected with Hydrobon catalyst portion for Hydrodemetalation catalyst
Position, can be inside Hydrobon catalyst bed, is also possible to Hydrobon catalyst and is connected with removal of ccr by hydrotreating catalyst
Position.
The mass ratio that the fraction of stream of extraction described in step a accounts for residual oil raw material oil in terms of liquid phase is 5~90wt%, excellent
It is selected as 10~50wt%.
Operating condition described in step b can be used conventional operating condition, and generally reaction pressure 5.0MPa~
19.0MPa, reaction temperature are 300 DEG C~450 DEG C, volume space velocity 0.05h when liquid-1~5.0h-1, hydrogen to oil volume ratio be 100:1~
2000:1。
Separation described in step b generally comprises the first hydrotreating high-pressure separator and low pressure separator separates two
Point.The isolated hydrotreating high pressure hydrogen-rich gas of its high-pressure separator and liquid, the isolated liquid of high-pressure separator
Into 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
Body is isolated to the hydrotreating gaseous product of needs.
Fractionation described in step b (or stripping) carries out in hydrotreating fractionating column (or stripper) system.Low pressure liquid
Body product is fractionated in fractionating column obtains the first hydrotreated naphtha product, the first hydroprocessed diesel and the first hydrotreating
Heavy distillat.
LCO raw material described in step c is the light cycle oil of catalytic cracking unit, and initial boiling point is 100 DEG C~200 DEG C, is evaporated eventually
Point is 320 DEG C~400 DEG C.Some coker gas oils, ethylene cracking tar, coal tar can also be blended in the LCO feedstock oil
High one or more of the diesel oil distillate of equal arene contents.
It is 5:95 ~ 40:60 that the weight ratio of liquid phase stream and LCO raw material in logistics is extracted in first hydrotreating described in step c, which out,
It is preferred that 10:90 ~ 30:70.
A reactor can be set in first hydrotreating reaction area described in step c, and more reactors also can be set,
Such as 2 ~ 8.
Operating condition described in step c can be used conventional operating condition, and generally reaction pressure 5.0MPa~
19.0MPa, reaction temperature are 300 DEG C~450 DEG C, preferably 320 DEG C~410 DEG C, volume space velocity 0.2h when liquid-1~6.0h-1,
Hydrogen to oil volume ratio is 100:1~2000:1.
Separation described in step c carries out in the second hydrotreating high-pressure separator and low pressure separator.Wherein plus hydrogen
The isolated hydrotreating high pressure hydrogen-rich gas of high-pressure separator and liquid are handled, 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
Second hydrotreating gaseous product of isolated needs.
Fractionation described in step c (or stripping) carries out in second hydrotreating fractionating column (or stripper) system.It is low
Press liquid product is fractionated in fractionating column obtains the second hydrotreated naphtha product, the second hydroprocessed diesel and second plus hydrogen
Heavy distillate.
Described in first hydrotreating gas products and step c described in step b and the second hydrotreating gas products can be with
Separately as product, mixed gas product can also be mixed into.
First hydrotreated naphtha product described in step b and step c and the second hydrotreated naphtha product can
Mixing naphtha product can also be mixed into separately as product.
First hydroprocessed diesel described in step b and step c and the second hydroprocessed diesel can be separately as productions
Product can also mix the feedstock oil as catalytic cracking unit.
First hydrotreating heavy distillat described in step b and step c and the second hydrotreating heavy distillat mixing are used as and urge
Change the feedstock oil of cracking unit.
Step b, separation described in step c can mixed hydrogenation handle high-pressure separator and mixing low pressure separator in into
Row, i.e., the generation logistics of two hydrotreating reactors are mixed into the same hydrotreating high-pressure separator and the same low pressure
Separator.The wherein isolated mixed hydrogenation processing high pressure hydrogen-rich gas of mixed hydrogenation processing high-pressure separator and mixing liquid,
The isolated mixing liquid of mixed high-voltage separator enters mixing low pressure separator.Mixing low pressure separator produces highly pressurised liquid
The isolated mixing hydrocarbon-rich gas of object and mixing low pressure liquid product.Mixing hydrocarbon-rich gas is isolated to the mixed hydrogenation of needs
Processing gas product.
Equally, step b, fractionation described in step c (or stripping) can handle fractionating column (or mixing stripping in mixed hydrogenation
Tower) it carries out in system.The fractionation in mixing fractionating column of mixing low pressure liquid product obtains mixed hydrogenation processing naphtha product, mixes
Close hydroprocessed diesel and mixed hydrogenation heavy distillate.
Obtained mixed high-voltage hydrogen-rich gas can be used directly as recycle hydrogen, also be can choose and passed through recycle hydrogen de
It is recycled after sulphur system removing hydrogen sulfide.
In the present invention, the hydrogenation process in second hydrotreating reaction area includes the two reaction ranks successively carried out
Section, first stage of reaction carries out in the catalyst bed A containing hydrotreating catalyst, second stage of reaction containing plus hydrogen
It handles in the catalyst bed B of catalyst and carries out.It can also include that LCO feedstock oil is cut into light fraction and double distilled in the present invention
The process divided, the temperature of the cutting are 245 ~ 300 DEG C.First weighted BMO spaces object of the heavy distillat and step a extraction
By catalyst bed A after stream mixing, catalyst bed A gained hydrotreating logistics passes through catalysis after mixing with the light fraction
Agent bed B.
Further, in the second hydrotreating reaction area second stage of reaction reaction temperature y2Lower than first stage of reaction
Reaction temperature y1, preferably y2Compare y1Low 5-20 DEG C.
It is anti-by more hydrotreating catalysts in the cutting gained heavy distillat of LCO feedstock oil based on polycyclic aromatic hydrocarbon
It answers, can achieve the purpose of control aromatic hydrogenation depth, and double ring arene passes through less hydrotreating catalyst in light fraction
Reaction, can achieve the purpose that control aromatic hydrogenation depth simultaneously with heavy distillat, i.e. LCO after hydrotreating meets sulfur content
Double ring arene and polycyclic aromatic hydrocarbon moderately add hydrogen to mononuclear aromatics simultaneously, can satisfy sulfur content after further catalytic cracking and want
The catalytically cracked gasoline asked, and the octane number of gasoline can be improved.In addition, the second hydrotreating reaction area internal catalyst bed floor
B lower than catalyst bed A at a temperature of operated, be also beneficial to double ring arene add hydrogen saturation be converted into mononuclear aromatics reaction
Progress.
In the present invention, the catalyst bed A and catalyst bed B be can be set in a hydrotreating reactor
It is interior, or can be separately positioned in more than two hydrotreating reactors.First way is preferably used in the present invention.
In conjunction with Fig. 1, method of the invention is specific as follows: residual oil raw material oil 1 is mixed into first plus hydrogen with recycle hydrogen 5 first
Treatment reactor area extracts logistics 3, extraction out by extracting hydrotreating in the reaction stream of the first hydrotreating catalyst bed out
Logistics after hydrotreating extraction logistics 3 goes successively to the hydrotreating catalyst bed of lower part, the hydrotreating extraction of extraction
Logistics 3 enters the second hydrotreating reactor area after mixing with LCO feedstock oil 4, passes through the generation of hydrotreating catalyst bed
Logistics 8, which enters in the second high-pressure separator 9, carries out gas-liquid separation, and isolated liquid, which enters in after-fractionating tower 10, to be fractionated
It is anti-to the second hydrotreated naphtha 11, the second hydroprocessed diesel 12, the second hydrotreating heavy distillat 13, the first hydrotreating
It answers device production logistics 6 to enter in the first high-pressure separator 16 and carries out gas-liquid separation, isolated liquid enters the first fractionating column
Fractionation obtains the first hydrotreated naphtha 18, the first hydroprocessed diesel 19, the first hydrotreating heavy distillat 20, second in 17
The second isolated hydrogen-rich gas 14 of high-pressure separator 9 and isolated the first hydrogen-rich gas 21 of the first high-pressure separator 16
It is further mixed with supplement hydrogen 15 as recycle hydrogen after circulating hydrogen compressor is pressurized after mixing.
Illustrate the present invention program and effect below by embodiment.
Embodiment 1-4
Concrete condition of the invention is further illustrated below by embodiment.The protection developed and produced using FRIPP
Agent, catalyst for demetalation, desulphurization catalyst, de- carbon residue catalyst combination FZC catalyst series system carried out experimental study.
The main character of table 1 residual oil raw material oil
2 process conditions of table
2 process conditions of continued
3 test result of table
Wherein, the cutting temperature of LCO light fraction and LCO heavy distillat is 270 DEG C.
Using flexible residual hydrocracking technique of the invention it can be seen from embodiment, by from the first hydrotreating
A part of reaction stream of extraction in reaction zone, extraction logistics and LCO mixed hydrogenation process for producing fine quality catalytic cracking raw material, extraction
Residue after logistics adds hydrogen reason logistics continuation hydrotreating to produce high-quality naphtha, hydrogenated diesel oil and the purpose for adding hydrogen heavy distillat,
Fine quality catalytic cracking raw material is provided, production method is flexible.
Claims (18)
1. a kind of flexible residual hydrocracking technique, includes the following steps:
A, residual oil raw material oil passes through upstream protective agent and gradation in the first hydrotreating reaction area under hydroprocessing conditions first
Hydrotreating catalyst bed obtains the first hydrotreating logistics, this part reaction stream is divided into two parts, and a portion is taken out
First hydrotreating reaction area out；
B, the first hydrotreating logistics continuation of remainder is anti-by the first hydrotreating under hydroprocessing conditions in step a
The gradation hydrotreating catalyst bed in the downstream Ying Qu obtains the first hydrotreating reaction area product stream by separation, fractionation
After obtain the first hydrogenation gas product, the first hydrotreated naphtha product, the first hydrogenated diesel oil and first plus hydrogen heavy distillat；
C, in hydrotreating after the first hydrotreating logistics in the first hydrotreating reaction area of extraction obtained by step a is mixed with LCO
Under the conditions of by the gradation hydrotreating catalyst bed in the second hydrotreating reaction area, it is raw to obtain the second hydrotreating reaction area
The second hydrogenation gas product, the second hydrotreated naphtha product, the second hydrogenated diesel oil and are obtained after separating, being fractionated at logistics
Two add hydrogen heavy distillat.
2. hydroprocessing technique described in accordance with the claim 1, which is characterized in that the initial boiling point of the residual oil raw material be 200~
450 DEG C, the end point of distillation is 550~750 DEG C.
3. hydroprocessing technique according to claim 2, which is characterized in that the residual oil raw material oil is selected from normal pressure slag
Oil, decompression residuum, coking heavy oil, deasphalted oil, recycle oil, coal tar, coal direct liquefaction oil, ICL for Indirect Coal Liquefaction oil, synthetic slag
At least one of oil and shale oil.
4. hydroprocessing technique described in accordance with the claim 1, which is characterized in that step a, protection described in step b and step c
In agent, hydrotreating catalyst, one or more of hydrogenation active component Co, Mo, W, Ni, hydrogenation active component is to aoxidize
The weight content of object meter is 5%~70%；Catalyst carrier contain aluminium oxide, amorphous silicon aluminium, silica, in titanium oxide at least
It is a kind of.
5. hydroprocessing technique according to claim 4, which is characterized in that the protective agent, hydrotreating catalyst
In contain auxiliary agent, the auxiliary agent is selected from least one of P, Si, B, Ti, Zr.
6. hydroprocessing technique described in accordance with the claim 1, which is characterized in that hydroprocessing condition described in step a are as follows: anti-
Answer pressure 5.0MPa~19.0MPa, reaction temperature is 300 DEG C~450 DEG C, volume space velocity 0.05h when liquid-1~5.0h-1, hydrogen oil
Volume ratio is 100:1~2000:1.
7. hydroprocessing technique described in accordance with the claim 1, which is characterized in that the first hydrotreating object extracted out in step a
The weight percent that stream accounts for residual oil raw material oil in terms of liquid phase is 5~90wt%, preferably 10~50wt%.
8. hydroprocessing technique described in accordance with the claim 1, which is characterized in that the first hydrotreating of extraction section in step a
Any position of the corresponding catalyst position between Hydrodemetalation catalyst and removal of ccr by hydrotreating catalyst bed when logistics.
9. hydroprocessing technique described in accordance with the claim 1, which is characterized in that hydroprocessing condition described in step b are as follows: anti-
Answer pressure 5.0MPa~19.0MPa, reaction temperature is 300 DEG C~450 DEG C, volume space velocity 0.05h when liquid-1~5.0h-1, hydrogen oil
Volume ratio is 100:1~2000:1.
10. hydroprocessing technique described in accordance with the claim 1, which is characterized in that the initial boiling point of the LCO is 100~200
DEG C, the end point of distillation is 320~400 DEG C.
11. hydroprocessing technique described in accordance with the claim 1, which is characterized in that also blended in the LCO coker gas oil,
At least one of ethylene cracking tar and coal tar.
12. hydroprocessing technique described in accordance with the claim 1, which is characterized in that logistics is extracted in the first hydrotreating out in step c
It with the weight ratio of LCO raw material is 5:95 ~ 40:60 in terms of liquid phase, preferably 10:90 ~ 30:70.
13. hydroprocessing technique according to claim 7, which is characterized in that hydroprocessing condition described in step c are as follows:
Reaction pressure 5.0MPa~19.0MPa, reaction temperature are 300 DEG C~450 DEG C, and preferably 320 DEG C~410 DEG C, volume is empty when liquid
Fast 0.2h-1~6.0h-1, hydrogen to oil volume ratio is 100:1~2000:1.
14. hydroprocessing technique described in accordance with the claim 1, which is characterized in that in second hydrotreating reaction area
Hydrogenation process includes two stages of reaction successively carried out, and first stage of reaction is in the catalyst bed containing hydrotreating catalyst
It is carried out in layer A, second stage of reaction carries out in the catalyst bed B containing hydrotreating catalyst.
15. hydroprocessing technique according to claim 14, which is characterized in that further include being cut into LCO feedstock oil gently
The process of fraction and heavy distillat, the temperature of the cutting are 245 ~ 300 DEG C.
16. hydroprocessing technique according to claim 15, which is characterized in that the heavy distillat and step a was extracted out
By catalyst bed A after first weighted BMO spaces logistics mixing, catalyst bed A gained hydrotreating logistics is gently evaporated with described
Pass through catalyst bed B after dividing mixing.
17. hydroprocessing technique according to claim 14, which is characterized in that the catalyst bed A and catalyst
Bed B is arranged in a hydrotreating reactor, or is separately positioned in more than two hydrotreating reactors.
18. hydroprocessing technique described in accordance with the claim 1, which is characterized in that separation described in step b and step c and
Fractionation shares a set of separation and fractionating system.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101412928A (en) * | 2007-10-18 | 2009-04-22 | 中国石油化工股份有限公司 | Hydro-desulphurizing combined method |
| CN102041071A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Hydrogenation technology for diesel |
| CN103059928A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Hydrotreating device and application thereof as well as residual oil hydrotreating method |
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2017
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101412928A (en) * | 2007-10-18 | 2009-04-22 | 中国石油化工股份有限公司 | Hydro-desulphurizing combined method |
| CN102041071A (en) * | 2009-10-21 | 2011-05-04 | 中国石油化工股份有限公司 | Hydrogenation technology for diesel |
| CN103059928A (en) * | 2011-10-24 | 2013-04-24 | 中国石油化工股份有限公司 | Hydrotreating device and application thereof as well as residual oil hydrotreating method |
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Effective date of registration: 20230925 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. |