CN109722307A

CN109722307A - The method and system of processing of heavy oil

Info

Publication number: CN109722307A
Application number: CN201711048275.2A
Authority: CN
Inventors: 牛传峰; 张执刚; 戴立顺; 崔琰; 杨清河; 刘涛; 邵志才; 邓中活; 施瑢; 聂鑫鹏
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2017-10-31
Filing date: 2017-10-31
Publication date: 2019-05-07
Anticipated expiration: 2037-10-31
Also published as: CN109722307B

Abstract

The present invention relates to processing of heavy oil fields, disclose the method and system of processing of heavy oil, this method comprises: catalytically cracked stock, which is introduced to the first riser reaction zone of catalytic cracking, carries out catalytic cracking reaction, and separate reaction product；Catalytic cracked oil pulp is introduced in boiling bed hydrogenation unit and carries out hydrogenation reaction；And at least partly heavy catalytic cycle oil it will be introduced in boiling bed hydrogenation unit and/or fixed bed hydrogenation unit and react；Hydrogen recycle oil will be added to be introduced in the second riser of catalytic cracking lower reaction zone and carry out catalytic cracking reaction；By gasoline fraction and hydrogen recycle oil is added to be introduced to catalytic cracking the second riser top reaction zone progress catalytic cracking reaction；Separate the product of catalytic cracking reaction.The method of processing of heavy oil provided by the invention enables to heavy oil Efficient Conversion and is able to produce low olefin catalytic gasoline, compared with high cetane number catalytic diesel oil, and diesel oil and gasoline ratio can be adjusted flexibly and have high light oil yield.

Description

The method and system of processing of heavy oil

Technical field

The present invention relates to hydrocarbon ils manufacture fields, and in particular to the method for processing of heavy oil a kind of and a kind of processing of heavy oil are System.

Background technique

The world is faced with the trend that crude oil change deteriorates again at present, and demand of the people to heavy oil gradually subtracts Few, the demand to light oil is then significantly increased.Therefore, the maximum conversion of residual oil is pursued one after another by oil refining enterprise.

In the various methods of residual oil weight-lightening, good paraffinic base heavy oil can directly carry out catalytic cracking production light oil Product.The high carbon residue residual oil of high-sulfur inferior first carries out hydrotreating, hydrogenation tail oil and carries out catalyzed cracking processing technique again.Residual oil is through adding After the impurity such as hydrogen processing removing metal, sulphur, nitrogen, hydrogen content is improved, can be used as good Rfcc Feedstock, by residual oil It is converted completely.Therefore, the technique nowadays by residual hydrogenation tail oil directly as Rfcc Feedstock obtains increasingly Universal application.

But in process above, catalytic cracking heavy oil is to be recycled in catalytic cracking unit to be further processed.Due to heavy oil Containing polycyclic aromatic hydrocarbon, thus light oil yield is low, and green coke amount is big, increases regenerator load, reduces heavy oil catalytically cracking equipment Treating capacity and economic benefit.If heavy oil is mixed into, slurry oil is directly outer to be got rid of, and is increased the slurry oil yield of low value, is reduced high price It is worth product yield.

At the same time, with the enhancing that human environment protection is realized, dirt of the harmful substance to atmospheric environment in vehicle exhaust Dye increasingly attracts people's attention, and countries in the world propose increasingly stringent limitation to the composition of motor petrol, especially Sulfur content.

European Union came into effect Euro V emissions in 2009, it is desirable that content of sulfur in gasoline, and will be 2014 less than 10 μ g/g Or so year carries out more stringent Europe VI standard.Sulfur in gasoline is respectively provided in second and third stage gasoline standard of California, USA to contain Amount is not higher than 30 μ g/g, 15 μ g/g.China also has been carried out state's V gasoline standard, it is desirable that content of sulfur in gasoline is not more than 10 μ g/g, alkene Hydrocarbon volume fraction is not more than 24%.Future is more stringent to olefin(e) centent limitation in gasoline, and capital VI normal benzine requires alkene body Fraction is not more than 15%.

Alkene in gasoline product therefore, reduces the alkene of FCC gasoline mainly from catalytically cracked gasoline (FCC gasoline) Content is to reduce the key point of gasoline product olefin(e) centent.Hydrogen is added to can reduce the olefin(e) centent in gasoline, but can be along with The sharp fall of octane number.

Currently, catalytic cracking reduces content of olefin in gasoline mainly by using Olefin decrease technique in catalytic cracking unit To reduce the alkene in gasoline.

CN1388219A is reacted by hydrogen supply agent component using boiling range less than 400 DEG C and gasoline one reduces gasoline olefin Content, but then cannot be considered in terms of when needing to drop gasoline olefin and hydrogen supply agent being carried out lighting simultaneously.If in order to which cracking simultaneously is made For the heavy constituent of hydrogen supply agent, need to will cause the cracking loss of gasoline at this time using high reaction temperature；If avoiding catalytic cracking Gasoline loss and use low temperature, then can not cracking as the heavy constituent of hydrogen supply agent.It therefore can not be by catalytic cracking using the method Light cycle oil, catalytic cracking heavy oil or add hydrogen after catalytic cracking light cycle oil, catalytic cracking heavy oil be converted into lighter oil Product can not improve light oil yield；And the catalyst that catalytically cracked gasoline is contacted in this method does not first pass through carbon deposit, will lead to pair Gasoline cracking activity is very high, and the gasoline loss for being originally used for Olefin decrease is larger.

CN102373085A and CN102199447A converts heavy oil using double lifting leg, can produce low alkene vapour Oil.But due to the second riser top gasoline be not with the hydrogenation component with hydrogen supply performance it is admixed together after react again, need It wants gasoline itself to be condensed dehydrogenation to be supplied to itself as hydrogen source, not only therefore leads to valuable gasoline component loss, reduce The amount of high-value product；Moreover, drop gasoline olefin effect can be made bad because gasoline hydrogen supply capacity itself is poor.This method simultaneously Be it is a kind of can high-yield diesel oil scheme, it is right since the catalytic cracking diesel oil market price is far below the catalytically cracked gasoline market price The gasoline of voluminous high value is unfavorable.

Common double lift pipe catalytic cracking technology one of them can be mentioned as a kind of well-known technique in catalytic cracking unit Heavy oil is converted in riser, reduces gasoline olefin in another riser.But since gasoline is to individually enter one of promotion Pipe carries out Olefin decrease, and contacting cracking strong regeneration catalyzing Cracking catalyst there are gasoline causes gasoline cracking more, and does not have Having external hydrogen supply agent to provide hydrogen source, gasoline for gasoline need to take hydrogen that part of gasoline is caused to be condensed the more problem of coking, band from itself Carry out the biggish loss of yield of gasoline, and due to not having hydrogen supply agent and gasoline to feed together, Olefin decrease effect is bad.

Summary of the invention

The purpose of the present invention is provide a kind of work for combining hydrotreating and catalytic cracking on the basis of existing technology Process, so that heavy oil Efficient Conversion and being able to produce low olefin catalytic gasoline, compared with high cetane number catalytic diesel oil, and can Diesel oil and gasoline ratio and the system and method with high light oil yield are adjusted flexibly.

To achieve the goals above, the first aspect of the present invention provides a kind of method of processing of heavy oil, this method comprises:

(1) under the conditions of catalytic cracking reaction, catalytically cracked stock is introduced to catalytic cracking first and promotes tube reaction Area carries out the first catalytic cracking reaction, and separate the product of the first catalytic cracking reaction to obtain dry gas, liquefied gas, catalysis are split Change gasoline, catalytic cracking light cycle oil, heavy catalytic cycle oil and catalytic cracked oil pulp；

(2) it will be introduced in boiling bed hydrogenation unit and carry out from at least partly described catalytic cracked oil pulp of step (1) First hydrogenation reaction；Optionally and boiling will be introduced to from at least partly described catalytic cracking light cycle oil of step (1) It carries out the first hydrogenation reaction in bed hydroprocessing unit and/or is introduced in fixed bed hydrogenation unit to carry out the second hydrogenation reaction；Optionally It ground and at least partly described heavy catalytic cycle oil from step (1) will be introduced in boiling bed hydrogenation unit carries out the It one hydrogenation reaction and/or is introduced in fixed bed hydrogenation unit and carries out the second hydrogenation reaction；Separate first hydrogenation reaction and The product of second hydrogenation reaction is to obtain adding hydrogen recycle oil；

(3) will a part from step (2) is described plus hydrogen recycle oil to be introduced to the second riser of catalytic cracking lower part anti- It answers and carries out the second catalytic cracking reaction in area；By gasoline fraction and from step (2) another part described in plus hydrogen recycle oil draw Enter to the second riser of catalytic cracking top reaction zone and with catalyst and oil gas one from the second riser lower reaction zone It rises and carries out third catalytic cracking reaction；Separate the production after second catalytic cracking reaction and the third catalytic cracking reaction Object is to obtain dry gas, liquefied gas, low Olefinic catalytic cracking gasoline, catalytic cracking light cycle oil, heavy catalytic cycle oil and urge Change cracking slurry oil, the gasoline fraction at least partially comes from the catalytically cracked gasoline of step (1).

The second aspect of the present invention provides a kind of system of processing of heavy oil, which includes:

First riser reaction zone contains the first reaction member and the first separative unit in first riser reaction zone, Catalytically cracked stock, which is introduced in first reaction member, carries out the first catalytic cracking reaction, and the first Catalytic Cracking Unit of Measure The product answered is separated in first separative unit and is gently recycled with obtaining dry gas, liquefied gas, catalytically cracked gasoline, catalytic cracking Oil, heavy catalytic cycle oil and catalytic cracked oil pulp；

Hydrogenation unit, in the hydrogenation unit containing boiling bed hydrogenation reactor or and fixed bed hydrogenation reactor, with And also containing the second separative unit, the catalytic cracked oil pulp from first riser reaction zone enters the ebullated bed The first hydrogenation reaction is carried out in hydrogenator；Optionally from at least partly described catalytic cracking light cycle oil of step (1) Into carried out in the boiling bed hydrogenation reactor the first hydrogenation reaction and/or enter the fixed bed hydrogenation reactor in carry out Second hydrogenation reaction；Add optionally from at least partly described heavy catalytic cycle oil of step (1) into the ebullated bed It carries out the first hydrogenation reaction in hydrogen reactor and/or enters in the fixed bed hydrogenation reactor to carry out the second hydrogenation reaction；Institute The product line of the product and/or second hydrogenation reaction of stating the first hydrogenation reaction be introduced in second separative unit into Row separation is to obtain adding hydrogen recycle oil；And

Second riser reaction zone contains top reaction zone, lower reaction zone and third in second riser reaction zone Separative unit, a part from the hydrogenation unit is described plus hydrogen recycle oil carries out the second catalysis in the lower reaction zone Cracking reaction；Described in gasoline fraction and another part from the hydrogenation unit plus hydrogen recycle oil is in the top reaction zone Third catalytic cracking reaction is carried out together with catalyst and oil gas from the lower reaction zone；Through second catalytic cracking Product after reaction and the third catalytic cracking reaction is separated in the third separative unit to obtain dry gas, liquefaction Gas, low Olefinic catalytic cracking gasoline, catalytic cracking light cycle oil, heavy catalytic cycle oil and catalytic cracked oil pulp.

The method of processing of heavy oil provided by the invention enables to heavy oil Efficient Conversion and is able to produce low olefin catalytic vapour Oil, compared with high cetane number catalytic diesel oil, and can be adjusted flexibly diesel oil and gasoline ratio and have high light oil yield.

Detailed description of the invention

Fig. 1 is the process flow chart of the method for processing of heavy oil shown in a kind of preferred embodiment of the invention.

Description of symbols

1、2、5、6、8、9、10、11、15、16、17、27、25、26、27、35、36、38、41、43、46、47、48、49、50、 51,52,53,54,55 be pipeline

3, catalytic cracking the first riser 4, the first stripper

7, regenerator 12, the second riser of catalytic cracking

13, the second riser top reaction zone 14, the second stripper

18, catalytic cracking the first fractionating system 19, the first dry gas

20, the first liquefied gas

21, the first riser catalytic cracking gasoline

22, the first riser catalytic cracking light cycle oil

23, the first riser catalytic cracking heavy-cycle oil

24, the first riser catalytic cracking slurry oil

28, catalytic cracking after-fractionating system

29, the second dry gas 30, the second liquefied gas

31, the second riser catalytic cracking gasoline

32, the second riser catalytic cracking light cycle oil

33, the second riser catalytic cracking heavy-cycle oil

34, the second riser catalytic cracking slurry oil

37, boiling bed hydrogenation reactor 39, the first fractionating system

40, first adds hydrogen recycle oil 42, fixed bed hydrogenation reactor

44, after-fractionating system 45, second plus hydrogen recycle oil

Specific embodiment

The endpoint of disclosed range and any value are not limited to the accurate range or value herein, these ranges or Value should be understood as comprising the value close to these ranges or value.For numberical range, between the endpoint value of each range, respectively It can be combined with each other between the endpoint value of a range and individual point value, and individually between point value and obtain one or more New numberical range, these numberical ranges should be considered as specific open herein.

As previously mentioned, the first aspect of the present invention provides a kind of method of processing of heavy oil, this method comprises:

Aforementioned " a part is described to add hydrogen recycle oil " and " described in another part plus hydrogen recycle oil " are constituted and are obtained by step (2) Whole add at least part of hydrogen recycle oil.

Catalytic cracking light cycle oil of the present invention is conventional catalytic cracking diesel oil in the art.

Under preferable case, in the present invention, in step (3), participate in second catalytic cracking reaction adds hydrogen circulation Oil is 1:(0.01~10 with the third catalytic cracking reaction plus hydrogen recycle oil weight ratio is participated in).

In case of no particular description, there is no special for content of the present invention to " part " in aforementioned " at least partly " Other requirement, those skilled in the art can be adjusted flexibly according to actual needs, this is but also side provided by the invention Method has the advantages that flexible operating.

Under preferable case, at least partly catalytic cracking light cycle oil obtained in step (3) is introduced to boiling by the present invention It carries out the first hydrogenation reaction in bed hydroprocessing unit and/or is introduced in fixed bed hydrogenation unit to carry out the second hydrogenation reaction；Optionally Ground and at least partly catalytic cracked oil pulp obtained in step (3) is introduced in boiling bed hydrogenation unit and carries out described first Hydrogenation reaction；Optionally and by least partly heavy catalytic cycle oil obtained in step (3) it is introduced to boiling bed hydrogenation It carries out the first hydrogenation reaction in unit and/or is introduced in fixed bed hydrogenation unit to carry out the second hydrogenation reaction.

Two kinds of preferred embodiments of method of the invention presented below.

Preferred embodiment 1: by at least partly described catalytic cracked oil pulp from step (1) or and come Obtained in step (3) at least partly catalytic cracked oil pulp be introduced in boiling bed hydrogenation unit carry out described first plus hydrogen it is anti- It answers；Optionally and fixed bed hydrogenation unit will be introduced to from at least partly described catalytic cracking light cycle oil of step (1) The second hydrogenation reaction of middle progress；Optionally and it will draw at least partly catalytic cracking light cycle oil obtained in step (3) Enter and carries out the second hydrogenation reaction into fixed bed hydrogenation unit；It will urge optionally and from at least partly described of step (1) Change cracking heavy-cycle oil and be introduced in boiling bed hydrogenation unit and carries out the first hydrogenation reaction and/or be introduced to fixed bed hydrogenation unit The second hydrogenation reaction of middle progress；Optionally and it will draw at least partly heavy catalytic cycle oil obtained in step (3) Enter to carry out the first hydrogenation reaction into boiling bed hydrogenation unit and/or be introduced to progress second in fixed bed hydrogenation unit to add hydrogen anti- It answers.

Preferred embodiment 2: by whole catalytic cracked oil pulps from step (1) and from institute in step (3) The whole catalytic cracked oil pulps obtained, which are introduced in boiling bed hydrogenation unit, carries out first hydrogenation reaction；And step will be come from (1) whole catalytic cracking light cycle oils and the whole catalytic cracking light cycle oil obtained in step (3) are introduced to boiling It carries out the first hydrogenation reaction in bed hydroprocessing unit and/or is introduced in fixed bed hydrogenation unit to carry out the second hydrogenation reaction；And By whole heavy catalytic cycle oils from step (1) and come from whole heavy catalytic cycle oil obtained in step (3) It is introduced in boiling bed hydrogenation unit and carries out the first hydrogenation reaction and/or be introduced in fixed bed hydrogenation unit to carry out second plus hydrogen Reaction.

In aforementioned preferred embodiment 1, preferably will from step (1) the catalytic cracking light cycle oil with And the low Olefinic catalytic cracking gasoline from step (3) goes out device respectively as diesel product and gasoline products.

In aforementioned preferred embodiment 2, the low Olefinic catalytic cracking gasoline of step (3) will be preferably come from Go out device as gasoline products.

Preferably, it is 450~540 DEG C that the reaction condition of first riser reaction zone, which includes: average reaction temperature, agent Oily weight ratio is (2~15): 1, the residence time is 0.4~10 second；It is highly preferred that the reaction item of first riser reaction zone Part includes: that average reaction temperature is 470~500 DEG C, and agent oil weight ratio is (5~8): 1, the residence time is 0.8~3 second.

Preferably, the reaction condition of second riser of catalytic cracking lower reaction zone includes: that average reaction temperature is 500~600 DEG C, agent oil weight ratio is (2~30): 1, the residence time is 0.4~10 second；It is highly preferred that the catalytic cracking The reaction condition of two riser lower reaction zones include: average reaction temperature be 530~570 DEG C, agent oil weight ratio be (8~ 20): 1, the residence time is 0.8~3 second.Described dose of oily weight ratio indicates urging into catalytic cracking the second riser lower reaction zone The weight ratio of agent and the feedstock oil into the second riser of catalytic cracking lower reaction zone；The residence time indicates be catalyzed Cracking the second riser lower reaction zone residence time.

In the present invention, it is preferred to the average reaction temperature of second riser of catalytic cracking top reaction zone be 350~ 520 DEG C, more preferably 350~449.99 DEG C, further preferably 400~449.99 DEG C, particularly preferably 350~400 DEG C.This Invention inventors have found that controlling the reaction temperature of second riser of catalytic cracking top reaction zone of the invention aforementioned When in range, when can be improved the yield of high-value product, also, being reacted at such as 400~449.99 DEG C, the present invention Method i.e. have good hydrogen transfer activity to reduce gasoline olefin；Even in the range of lower 350~400 DEG C, this The method of invention also has hydrogen transfer activity to reduce gasoline olefin.Method of the invention under relatively low reaction temperature into When row Above-mentioned catalytic cracking reaction, gasoline cracking degree is very low, helps to obtain high light oil yield.

According to a kind of preferred embodiment, the reaction condition of second riser of catalytic cracking top reaction zone Include: average reaction temperature be 350~520 DEG C, reaction weight (hourly) space velocity (WHSV) be 0.5~30h^-1；It is highly preferred that the catalytic cracking The reaction condition of two riser top reaction zones includes: that average reaction temperature is 350~449.99 DEG C, and reaction weight (hourly) space velocity (WHSV) is 0.5~30h^-1；It is further preferred that the reaction condition of second riser of catalytic cracking top reaction zone includes: average Reaction temperature is 350~449.99 DEG C, and reaction weight (hourly) space velocity (WHSV) is 2~8h^-1.The reaction temperature refers to the second riser of catalytic cracking The average reaction temperature of top reaction zone；The weight (hourly) space velocity (WHSV) refers to the charging of catalytic cracking the second riser lower reaction zone and urges Change the sum of weight flows of the second riser of cracking top reaction zone feeds in the reaction zone of the second riser of catalytic cracking top The weight ratio of catalyst.

Preferably, the average reaction temperature of second riser of catalytic cracking top reaction zone is than the catalytic cracking The average reaction temperature of two riser lower reaction zones is 30~150 DEG C low, and further preferably low 40~120 DEG C；More preferably low 50 ~100 DEG C.

Under preferable case, in the second riser of catalytic cracking top reaction zone of step (3), the gasoline fraction and institute It states plus the weight ratio of hydrogen recycle oil is (0.2~100): 1；Further preferably (0.5~10): 1；More preferably (1~6): 1.

Preferably, it is 3.0 that the condition of the second hydrogenation reaction in the fixed bed hydrogenation unit of step (2), which includes: hydrogen partial pressure, ~22.0MPa, reaction temperature are 280~450 DEG C, and volume space velocity is 0.1~5.0h^-1, hydrogen to oil volume ratio be 200~2000Nm³/ m³。

Preferably, it is 3.0 that the condition of the first hydrogenation reaction in the boiling bed hydrogenation unit of step (2), which includes: hydrogen partial pressure, ~22.0MPa, reaction temperature are 280~450 DEG C, and volume space velocity is 0.1~5.0h^-1, hydrogen to oil volume ratio be 200~2000Nm³/ m³。

Under preferable case, participates in first catalytic cracking reaction, second catalytic cracking reaction and the third and urge Change zeolite of the catalytic cracking catalyst each independently containing 5~50 weight % of cracking reaction, the inorganic oxygen of 5~95 weight % The clay of compound and 0~70 weight %.The content of clay is 0~70 weight %, indicates to participate in first Catalytic Cracking Unit of Measure It answers, contain each independently in the catalytic cracking catalyst of second catalytic cracking reaction and the third catalytic cracking reaction Or clay is not contained.

Under preferable case, in the catalytic cracking catalyst, the zeolite be the catalytic cracking catalyst in extremely A kind of few active component, the preferably described zeolite are selected from large pore zeolite or and mesopore zeolite；It is highly preferred that the large pore zeolite Account for 25~100 weight %, more preferable 50~100 weight % of whole active components in the catalytic cracking catalyst；And The mesopore zeolite accounts for 0~75 weight % of whole active components in the catalytic cracking catalyst, more preferable 0~50 weight Measure %.

Under preferable case, the large pore zeolite is selected from y-type zeolite, rare earth Y type zeolite (REY), rare earth hydrogen y-type zeolite (REHY), the mixture of one or more of ultrastable (USY), extremely steady y-type zeolite of rare earth (REUSY).

Preferably, the mesopore zeolite is selected from ZSM series zeolite and/or ZRP zeolite；It is highly preferred that the mesopore zeolite The modified mesoporous zeolite obtained after being modified for transition metal elements such as nonmetalloids and/or iron, cobalt, nickel such as use phosphorus.

The ZSM series zeolite of the invention be selected from ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, The zeolite of ZSM-48 and other similar structures any one of or appoint several mixture.

Inorganic oxide in Above-mentioned catalytic Cracking catalyst of the invention is as binder, preferably silica (SiO₂) and/or aluminum oxide (Al₂O₃)。

Clay in Above-mentioned catalytic Cracking catalyst of the invention is preferably selected from kaolin as the carrier being optionally present And/or halloysite.

Preferably, it participates in first hydrogenation reaction of step (2) and the hydrogenation catalyst of second hydrogenation reaction Active metal component containing carrier and load on the carrier each independently, optionally and contains molecular sieve, described Active metal component be selected from vib metals element and/or group VIII non-noble metal j element, the carrier be selected from aluminium oxide, At least one of silica and amorphous silica-alumina.

Preferably, it participates in first hydrogenation reaction of step (2) and the hydrogenation catalyst of second hydrogenation reaction The active metal component be selected from nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum, the combination of nickel-molybdenum-at least one of tungsten and cobalt-molybdenum.

Preferably, method of the invention further comprises that will participate in first catalytic cracking reaction, second catalysis The catalyst of at least one of cracking reaction and the third catalytic cracking reaction reaction is regenerated, and will be obtained after regeneration Regenerated catalyst be back to continue to participate in react accordingly.

Preferably, the catalytically cracked stock of the invention is residual oil and/or wax oil；It is highly preferred that the catalysis is split Change and further contains diesel oil and/or naphtha in feedstock oil.

The catalytic cracking light cycle oil of the invention is also conventional catalytic cracking diesel oil in the art.

Dry gas and liquefied gas can also be obtained by separating fractionation in preceding method of the invention.

The boiling bed hydrogenation unit of the invention and the fixed bed hydrogenation unit are various independently including at least one Reactor, the boiling bed hydrogenation unit and the fixed bed hydrogenation unit can include respectively a fractionating system, can also share one A fractionating system；The fractionating system includes fractionating column and/or stripper.

As previously mentioned, the second aspect of the present invention provides a kind of system of processing of heavy oil, which includes:

According to a kind of preferred embodiment, in second riser reaction zone, the top reaction zone Internal diameter is more than or equal to the internal diameter of the lower reaction zone.For example, the catalytic cracking second in second riser reaction zone mentions The lower part of riser is Conventional riser, top is bed reactor that internal diameter is significantly greater than lower lift pipe.In the present invention, right There is the riser of expanding type in top, then wide diameter portion can be allocated as top reaction zone；It is mentioning for bed type for top Riser, then can be using bed reactor area as top reaction zone.

Preferably, the ratio between the internal diameter of the top reaction zone and the internal diameter of the lower reaction zone are (1.0~10): 1.

Under preferable case, second riser reaction zone is connect so that from described by pipeline with the hydrogenation unit The catalytic cracked oil pulp of second riser reaction zone, which is able to enter in the boiling bed hydrogenation reactor, carries out described first plus hydrogen Reaction；Optionally and at least partly catalytic cracking light cycle oil from second riser reaction zone is able to enter First hydrogenation reaction is carried out in the boiling bed hydrogenation reactor and/or is able to enter in the fixed bed hydrogenation reactor Carry out second hydrogenation reaction；Optionally and make at least partly catalytic cracking from second riser reaction zone Heavy-cycle oil, which is able to enter in the boiling bed hydrogenation reactor, to carry out first hydrogenation reaction and/or is able to enter described solid Second hydrogenation reaction is carried out in fixed bed hydrogenator.

In the system of the invention, the top reaction zone of preferably described second riser reaction zone and lower reaction zone Join domain in be provided with feed inlet.

Particularly, in the process system stated before this invention, it is not limited to contain only pair there are two riser reactor Riser catalytic cracking facility, can be to contain the more of more than two riser reactors in the process system of the invention Riser catalytic cracking facility.In double lift pipe catalytic cracking facility or multiple riser catalytic cracking facility of the invention at least One riser reactor is used to cracked fuel oil and at least another riser reactor is used to cracking and hydrogenation recycle oil and goes forward side by side The reaction of row decreasing by gasoline olefin.

Under preferable case, regeneration unit, and first riser reaction zone and described are further contained in the system Two riser reaction zones share the regeneration unit to participation first catalytic cracking reaction, second Catalytic Cracking Unit of Measure It should be regenerated with the catalyst of at least one of third catalytic cracking reaction reaction, the regeneration catalyzing obtained after regeneration Agent is back to continue to participate in react accordingly by pipeline.

It is described in detail below in conjunction with method and system of the Fig. 1 to processing of heavy oil of the invention:

It is catalyzed after catalytically cracked stock and the vapor from pipeline 2 and the regeneration from pipeline 8 from pipeline 1 Cracking catalyst enters the lower part of the first riser of catalytic cracking 3 together, urges in the first riser of catalytic cracking 3 lower The first catalytic cracking reaction is carried out at a temperature of change cracking reaction, the logistics after reaction carries out gas solid separation and in the first stripper 4 Interior carry out catalyst stripping is entered in regenerator 7 after the catalyst stripping isolated by pipeline 5 and pipeline 6 and is regenerated.It urges Change in the first riser of cracking 3 oil gas that generates and the first fractionating system of catalytic cracking 18 is entered by pipeline 9, isolates the herein One dry gas 19, the first liquefied gas 20, the first riser catalytic cracking gasoline 21, the first riser catalytic cracking light cycle oil 22, First riser catalytic cracking heavy-cycle oil 23 and the first riser catalytic cracking slurry oil 24.First riser catalytic cracking slurry oil 24 pass through pipeline 27 into boiling bed hydrogenation reactor 37.First riser catalytic cracking light cycle oil 22 can all pass through pipeline 25 Device partially can also go out device as diesel product, partially by pipeline 26 and pipeline by pipeline 25 as diesel product out 49 into fixed bed hydrogenation reactor 42.First riser catalytic cracking heavy-cycle oil 23 both can be by pipeline 49 into fixed bed hydrogenation Reactor 42, can also be by pipeline 50 and pipeline 27 into boiling bed hydrogenation reactor 37.Into going back for boiling bed hydrogenation reactor 37 There is the second riser catalytic cracking slurry oil, there can also be the second riser catalytic cracking gently to follow into fixed bed hydrogenation reactor 42 Ring oil, the second riser catalytic cracking heavy-cycle oil 33 can optionally be converged by pipeline 51 and the second riser catalytic cracking slurry oil 34 By pipe after converging after conjunction through pipeline 35 into boiling bed hydrogenation reactor 37 or with the second riser catalytic cracking light cycle oil 32 Line 36 is into fixed bed hydrogenation reactor 42.Hydrogen by pipeline 54 into boiling bed hydrogenation reactor 37 and hydrogen by pipeline 55 into Fixed bed hydrogenation reactor 42.Into the first fractionating system 39, sour gas and light is being stripped off through pipeline 38 in boiling bed hydrogenation product It is drawn after hydrocarbon through pipeline 41, tower bottom draws first plus hydrogen recycle oil 40；Fixed bed hydrogenation product is through pipeline 43 into after-fractionating system System 44, after sour gas and lighter hydrocarbons is stripped off, tower bottom draws second plus hydrogen recycle oil 45, adds hydrogen recycle oil through pipeline 52 and first 40 converge at pipeline 53, are then divided into two parts, and a portion is by pipeline 46 under the second riser of catalytic cracking 12 Portion's reaction zone, and the water vapour from pipeline 11 and the regenerated catalyst from pipeline 10 contact and under higher reaction temperatures The second catalytic cracking reaction is carried out in the lower reaction zone of the second riser of catalytic cracking 12；Another part adds hydrogen recycle oil logical Cross pipeline 47 and by pipeline 48 come the first riser catalytic cracking gasoline into the second riser top reaction zone 13, herein With on the lower part for carrying out the second riser of catalytic cracking 12 oil gas and catalyst contact, in lower reaction temperature and longer Olefin decrease reaction (as third catalytic cracking reaction) is carried out under residence time, logistics after reaction carries out gas solid separation and the Catalyst stripping is carried out in two strippers 14, separation rear catalyst is delivered to regenerator 7 by pipeline 15 and pipeline 16 and carries out again Raw, the oil gas of generation isolates the second dry gas 29, the second liquefied gas into catalytic cracking after-fractionating system 28 by pipeline 17 30, the second riser catalytic cracking gasoline 31, the second riser catalytic cracking light cycle oil 32, the second riser catalytic cracking weight Recycle oil 33 and the second riser catalytic cracking slurry oil 34.Second riser catalytic cracking slurry oil 34 passes through pipeline 35 into ebullated bed Hydrogenator 37, the second riser catalytic cracking light cycle oil 32 by pipeline 36 into fixed bed hydrogenation reactor 42, second Riser catalytic cracking heavy-cycle oil 33 can be optionally by pipeline 36 into fixed bed hydrogenation reactor 42 or by pipeline 51 and pipe Line 35 is into boiling bed hydrogenation reactor 37.

The method and system of aforementioned processing of heavy oil provided by the invention also has following specific excellent compared with the existing technology Point:

(1) present invention has found under study for action, and a part in hydrogen recycle oil will be added into the second riser of catalytic cracking lower part Reaction zone, another part mix laggard the second riser of catalytic cracking top reaction zone with high olefin gasolines, can be by making to urge Fluidized cracking catalysts carry out part carbon deposit first before contacting gasoline and reduce cracking activity, to make catalytic cracking catalyst Hydrogen transfer activity and cracking reaction activity are than rising when to the second riser top reaction zone, therefore can reduce catalytic cracking vapour The cracking loss of oil itself, also can reduce catalytically cracked gasoline itself while dropping catalytic cracking gasoline olefine content and disappear Consumption；On the other hand, due to high olefin gasolines and plus hydrogen recycle oil reacted together, drop gasoline olefin needed for hydrogen from confession Hydrogen performance is very strong plus hydrogen recycle oil, does not need gasoline itself and carrys out hydrogen supply, thus reduce catalytically cracked gasoline condensation coking and Caused by gasoline loss.These two aspects combination more effectively realizes the reduction gasoline itself while reducing gasoline olefin and damages It loses, higher yield gasoline can be obtained.

(2) catalytically cracked gasoline is injected in catalytic cracking the second riser top reaction zone and add hydrogen recycle oil, it is anti-at this It answers area using more Conventional catalytic cracking low 30 DEG C or more even 50 DEG C or more of low reaction temperatures, is split using far below Conventional catalytic Change reaction temperature and even uses the temperature for being in hydrogenation reaction temperature region, it can be with hydrogenation reaction temperature on catalytic cracking unit Degree realizes decreasing by gasoline olefin.Cracking and reaction temperature due to gasoline itself have close association, using low reaction temperature energy Enough effectively reduce the generation of the cracking side reaction of catalytically cracked gasoline.

(3) plus hydrogen recycle oil wax oil or hydrogenated residue cracking difficulty for example than traditional catalytically cracked material is big.Hydrogen is added to recycle Oil is fed in catalytic cracking the second riser lower part, and the high temperature for making full use of riser lower part can be given to carry out more effective cracking, Light oil with high yield product, and a degree of coking can be generated on catalytic cracking catalyst, it is catalyst cracking after coking Performance significantly reduces, to improve the ratio between hydrogen migration/cracking reaction activity, the hydrogen migration for being more advantageous to middle and upper part progress gasoline is anti- It answers and reduces gasoline cracking.

(4) the second riser of catalytic cracking top reaction zone average reaction temperature is significantly lower than the promotion of catalytic cracking second Pipe lower reaction zone average reaction temperature, can guarantee difficult cracking adds hydrogen recycle oil to carry out cracking under high severity, and urges Change cracking gasoline also can use hydrogen supply agent under low reaction temperatures and carry out Olefin decrease to gasoline hydrogen supply to reduce gasoline cracking band The cracking for adding hydrogen recycle oil and decreasing by gasoline olefin two are realized in the loss come by the reaction temperature of two reaction zones significant difference Reaction reaches optimization.

(5) catalytic cracking recycle oil is catalytic cracking byproduct, because to be difficult to cracking easy for a large amount of polycyclic aromatic hydrocarbon contained by it In green coke, if hydrogen is not added in catalytic cracking unit freshening, will increase coking yield and itself bring light oil is received Rate is not but high.Catalytic cracking recycle oil can only be as the fuel oil of low value if getting rid of outside.After catalytic cracking recycle oil adds hydrogen, Aromatic hydrocarbons is saturated, and hydrogen content can be improved, then light oil yield can be improved into catalyzed cracking processing.

(6) high olefin gasolines enter in catalytic cracking the second riser top reaction zone with hydrogen recycle oil is added, available Hydrogen recycle oil is added to have the characteristics that high hydrogen transfer reaction reduces the alkene in catalytically cracked gasoline using the hydrogen added in hydrogen recycle oil, Low-alkene gasoline is converted by high olefin gasolines.And the catalytic cracking catalyst of catalytically cracked gasoline contact has been that band is burnt Catalyst rather than raw catelyst, can reduce the cracking possibility occurrence of catalytically cracked gasoline.

(7) heavy oil can reduce catalysis and split to carry out catalytic cracking compared with low reaction temperatures in the first riser of catalytic cracking Change coke and dry gas yied, improves liquid product yield；And the other byproduct heavy catalytic cycle oil of gained can be gone plus hydrogen Cracking is carried out into the second riser of catalytic cracking again afterwards, produces more light-end products, therefore the present invention has than the prior art The higher light-end products yield of catalytic cracking unit.

(8) catalytic cracking light cycle oil boiling range range is urged in diesel oil distillate section generally as diesel product in the present invention Changing cracking light cycle oil can partly or entirely carry out returning the progress cracking of the second riser of catalytic cracking again after adding hydrogen, can produce catalysis less Diesel oil fecund gasoline, and the ratio of catalytic diesel oil and gasoline can flexible modulation.It is even logical when not needing catalytic cracking diesel oil The heavy-cycle oil that kicks the beam all returns catalytic cracking unit cracking after all adding hydrogen again and maximizes production gasoline and do not produce catalytic cracking bavin Oil.

(9) catalytic cracked oil pulp contains acidic catalyst cracking catalyst particles object.If using fixed bed hydrogenation method into Row hydrogenation reaction, then these solid particulate matters understand blocking catalyst bed, and acidic catalyst will induce contained in slurry oil Asphalitine is easy to shorten the hydrogenation catalyst cycle of operation in hydrogenation catalyst coking.And use boiling bed hydrogenation reactor can be Line displacement catalyst, so that catalyst activity keeps stablizing.Fixed bed hydrogenation reactor has due to logistics is piston flow not back-mixing There are better refining effect, catalytic cracking light cycle oil and heavy-cycle oil to have using fixed bed hydrogenation and more preferably adds hydrogen effect.

To sum up, multiple effect can be reached using method of the present invention, significantly improves device economic benefit.

The present invention will be described in detail by way of examples below.

Hydrogenation protecting agent and Hydrobon catalyst used in fixed bed reactors hydropyrolysis experiment in embodiment and comparative example Trade names be respectively RG-30A, RN-32V, produced by Sinopec catalyst Chang Ling branch company, the two successively load and Admission space ratio is 10:90.The trade names of catalyst used in fluidized bed reactor hydropyrolysis experiment are RN-32V, by Chinese stone Change the production of catalyst Chang Ling branch company.FCC tests trial assembly in the medium-sized reactor of double lifting leg in embodiment and comparative example Progress is set, used catalytic cracking catalyst trade names are MLC-500, raw by Sinopec catalyst asphalt in Shenli Refinery It produces.

Embodiment 1

Using residual hydrogenation tail oil A as raw material, property is shown in Table 1.It is carried out using process flow shown in FIG. 1.

First riser and vapor and again of the residual hydrogenation tail oil A into the medium-sized catalytic cracking test device of double lifting leg The catalyst contact of raw device carries out the first catalytic cracking reaction, the condition of the first catalytic cracking reaction are as follows: reaction temperature 480 DEG C, agent oil weight ratio is 6, and the residence time in the first riser is 1.5 seconds.Oil gas after reaction is separated, and is isolated Dry gas, liquefied gas, the first riser catalytic cracking gasoline, the first riser catalytic cracking light cycle oil, the catalysis of the first riser Cracking heavy-cycle oil and the first riser catalytic cracking slurry oil.First riser catalytic cracking light cycle oil is all used as diesel oil to produce Product.All the first riser catalytic cracking heavy-cycle oil and all second being promoted from the second riser of catalytic cracking unit Pipe catalytic cracking light cycle oil and all the second riser catalytic cracking heavy-cycle oil are into fixed bed hydrogenation reactor, reaction condition Are as follows: 380 DEG C of reaction temperature, hydrogen partial pressure 10.0Mpa, volume space velocity 1.0h^-1, hydrogenated oil obtains after sour gas is stripped off Add hydrogen recycle oil A；All the first riser catalytic cracking slurry oil and whole second riser catalytic cracking slurry oils add into ebullated bed Hydrogen reactor, reaction condition are as follows: 380 DEG C of reaction temperature, hydrogen partial pressure 15.0Mpa, volume space velocity 0.5h^-1；Hydrogenated oil is through vapour It obtains adding hydrogen recycle oil B after proposing sour gas；Add hydrogen recycle oil A and hydrogen recycle oil B is added to mix to add hydrogen recycle oil.It is resulting Hydrogen recycle oil is added to be divided into two parts, 70 weight %'s therein adds hydrogen recycle oil to enter from the lower part of the second riser of catalytic cracking The second riser of catalytic cracking lower reaction zone contacts the second catalytic cracking of progress with vapor and from the catalyst that regenerator comes Reaction, the condition of the second catalytic cracking reaction are as follows: reaction temperature is 540 DEG C, and agent oil weight ratio is 20, is mentioned in catalytic cracking second The residence time of riser lower reaction zone is 1.5 seconds；Add the 30 weight % of residue of hydrogen recycle oil and all the first riser is catalyzed The top reaction zone for entering the second riser of catalytic cracking after cracking gasoline mixing, with the lower part uplink from the second riser Oil gas and catalyst contact carry out Olefin decrease reaction (as third catalytic cracking reaction, similarly hereinafter), third catalytic cracking reaction Condition are as follows: reaction temperature is 449 DEG C, on the second riser top in terms of the whole chargings for entering the second riser of catalytic cracking Reaction zone weight (hourly) space velocity (WHSV) is 4h^-1.Oil gas after reaction is separated, and dry gas, liquefied gas, the second riser catalytic cracking are isolated Gasoline, the second riser catalytic cracking light cycle oil, the second riser catalytic cracking heavy-cycle oil and the catalysis of the second riser are split Carburetion slurry.All the second riser catalytic cracking light cycle oils and all the second riser catalytic cracking heavy-cycle oil and all the One riser catalytic cracking heavy-cycle oil is into fixed bed hydrogenation reactor, whole the second riser catalytic cracking slurry oils and all the One riser catalytic cracking slurry oil is mixed into boiling bed hydrogenation reactor.

Whole product distribution is shown in Table 2, and olefin(e) centent is shown in Table 2 in the second riser catalytic cracking gasoline, and the first riser is urged Change cracking light cycle oil density and Cetane number is shown in Table 2.

Comparative example 1

Raw material and device are the same as embodiment 1.The charging of first riser and hydrogenation reaction system and reaction condition are also the same as real Apply example 1.

Second riser is with embodiment 1, but feeding manner is different, specifically:

All plus hydrogen recycle oil and all the first riser catalytic cracking gasoline, the first riser catalytic cracking slurry oil and Water vapour enters the second riser of catalytic cracking from the lower part of the second riser and is reacted at being 495 DEG C in reaction temperature, Residence time in the second riser lower reaction zone is 1.5 seconds, is mentioned in terms of the whole chargings for entering the second riser second Riser tube upper portion reaction zone weight (hourly) space velocity (WHSV) is 4h^-1.Second promotion tube reaction after oil gas separated, isolate dry gas, liquefied gas, Second riser catalytic cracking gasoline, the second riser catalytic cracking light cycle oil, the second riser catalytic cracking heavy-cycle oil With the second riser catalytic cracking slurry oil.All the second riser catalytic cracking light cycle oil and whole second riser catalysis are split Change heavy-cycle oil and all the first riser catalytic cracking heavy-cycle oil is into fixed bed hydrogenation reactor, all the second riser is urged Change cracking slurry oil and whole first riser catalytic cracking slurry oils into boiling bed hydrogenation reactor.

Comparative example 2

Full income plus hydrogen recycle oil and all the first riser catalytic cracking slurry oils from the lower part of the second riser into The lower reaction zone for entering the second riser of catalytic cracking contacts the second catalysis of progress with vapor and from the catalyst that regenerator comes Cracking reaction, the reaction temperature of the second riser lower reactor zone are 540 DEG C, and agent oil weight ratio is 20, in the second riser The residence time of lower reaction zone is 1.5 seconds；All the first riser catalytic cracking gasoline enters the second riser of catalytic cracking Top reaction zone, with the lower part uplink from the second riser and come oil gas and catalyst contact progress Olefin decrease reaction, on The reaction temperature of portion's reaction zone is 449 DEG C, in the second riser top reaction zone in terms of the whole chargings for entering the second riser Weight (hourly) space velocity (WHSV) is 4h^-1.Oil gas after reaction is separated, isolate dry gas, liquefied gas, the second riser catalytic cracking gasoline, Second riser catalytic cracking light cycle oil, the second riser catalytic cracking heavy-cycle oil and the second riser catalytic cracking oil Slurry.All the second riser catalytic cracking light cycle oil and whole second riser catalytic cracking heavy-cycle oil are mentioned with whole first Riser heavy catalytic cycle oil is into fixed bed hydrogenation reactor, and all the second riser catalytic cracking slurry oil is mentioned with whole first Riser catalytic cracked oil pulp is into boiling bed hydrogenation reactor.

Embodiment 2

Using paraffinic base residual oil B as raw material, property is shown in Table 1.It is carried out using process flow shown in FIG. 1.

Paraffinic base residual oil B is into the first riser and vapor of the medium-sized catalytic cracking test device of double lifting leg and regeneration The catalyst contact that device comes carries out the first catalytic cracking reaction, the condition of the first catalytic cracking reaction are as follows: reaction temperature 470 DEG C, agent oil weight ratio is 7, and the residence time in the first riser is 1.8 seconds.Oil gas after reaction is separated, and is isolated Dry gas, liquefied gas, the first riser catalytic cracking gasoline, the first riser catalytic cracking light cycle oil, the catalysis of the first riser Cracking heavy-cycle oil and the first riser catalytic cracking slurry oil.All the first riser catalytic cracking light cycle oils and come from second All the second riser catalytic cracking light cycle oils of riser are into fixed bed hydrogenation reactor, reaction condition are as follows: reaction temperature 370 DEG C, hydrogen partial pressure 6.4Mpa, volume space velocity 0.7h^-1, hydrogenated oil obtains after sour gas is stripped off plus hydrogen recycle oil A； All the first riser catalytic cracking heavy-cycle oil, all the first riser catalytic cracking slurry oil and whole second risers are urged Change cracking heavy-cycle oil, all the second riser catalytic cracking slurry oil is into boiling bed hydrogenation reactor, reaction condition are as follows: reaction temperature 370 DEG C, hydrogen partial pressure 13.0Mpa, volume space velocity 0.4h of degree^-1.Hydrogenated oil obtains after sour gas is stripped off plus hydrogen circulation Oily B；Add hydrogen recycle oil A and hydrogen recycle oil B is added to mix to add hydrogen recycle oil.Resulting plus hydrogen recycle oil is divided into two parts, wherein 80 weight %'s plus hydrogen recycle oil and all the first riser catalytic cracking slurry oils from the lower part of the second riser enter catalysis The second riser of cracking lower reaction zone contacts the second Catalytic Cracking Unit of Measure of progress with vapor and from the catalyst that regenerator comes It answers, the reaction temperature of the second riser lower reaction zone is 540 DEG C, and agent oil weight ratio is 20, is reacted in the second riser lower part The residence time in area is 1.3 seconds；The 20 weight % of residue in hydrogen recycle oil and whole first riser catalytic cracking gasoline is added to mix The top reaction zone for entering the second riser of catalytic cracking after conjunction, with the oil gas next from the second riser lower part uplink and catalysis Agent contact carries out Olefin decrease reaction, and top reaction zone reaction temperature is 430 DEG C, in terms of the whole chargings for entering the second riser Second riser top reaction zone weight (hourly) space velocity (WHSV) is 3h^-1.Oil gas after reaction is separated, and dry gas, liquefied gas, second are isolated Riser catalytic cracking gasoline, the second riser catalytic cracking light cycle oil, the second riser catalytic cracking heavy-cycle oil and Two riser catalytic cracking slurry oils.All the second riser catalytic cracking light cycle oil and whole first riser catalytic crackings are light Recycle oil is into fixed bed hydrogenation reactor, and all the second riser catalytic cracking heavy-cycle oil, whole second riser catalysis are split Carburetion slurry is with all the first riser catalytic cracking heavy-cycle oil, all the first riser catalytic cracking slurry oil is into boiling bed hydrogenation Reactor.

Whole product distribution is shown in Table 2, and olefin(e) centent is shown in Table 2 in the second riser catalytic cracking gasoline.

Embodiment 3

Paraffinic base residual oil B is into the first riser and vapor of the medium-sized catalytic cracking test device of double lifting leg and regeneration The catalyst contact that device comes carries out the first catalytic cracking reaction, the condition of the first catalytic cracking reaction are as follows: reaction temperature 490 DEG C, agent oil weight ratio is 6, and the residence time in the first riser is 1.5 seconds.Oil gas after reaction is separated, and is isolated Dry gas, liquefied gas, the first riser catalytic cracking gasoline, the first riser catalytic cracking light cycle oil, the catalysis of the first riser Cracking heavy-cycle oil and the first riser catalytic cracking slurry oil.It is the first riser catalytic cracking light cycle oil of 50 weight %, complete Portion's the second riser catalytic cracking light cycle oil is into fixed bed hydrogenation reactor, reaction condition are as follows: and 370 DEG C of reaction temperature, hydrogen point Press 8.0Mpa, volume space velocity 0.8h^-1, hydrogenated oil obtains after sour gas is stripped off plus hydrogen recycle oil A；All first mention Riser heavy catalytic cycle oil, all the first riser catalytic cracking slurry oil and all the second riser catalytic cracking follow again Ring oil, all the second riser catalytic cracking slurry oils are into boiling bed hydrogenation reactor, reaction condition are as follows: and 370 DEG C of reaction temperature, hydrogen Divide 13.0Mpa, volume space velocity 0.4h^-1.Hydrogenated oil obtains after sour gas is stripped off plus hydrogen recycle oil B；Hydrogen is added to follow Ring oil A and plus hydrogen recycle oil B mix plus hydrogen recycle oil.Resulting plus hydrogen recycle oil is divided into two parts, 75 weight % therein Plus hydrogen recycle oil enter catalytic cracking second with the first riser catalytic cracking slurry oils of whole from the lower part of the second riser and mention Riser lower reaction zone contacts the second catalytic cracking reaction of progress with vapor and from the catalyst that regenerator comes, and second is promoted The reaction temperature of pipe lower reaction zone is 540 DEG C, and agent oil weight ratio is 20, and the residence time in riser lower reaction zone is 1.0 the second；Enter catalysis after adding the 25 weight % of residue in hydrogen recycle oil to mix with all the first riser catalytic cracking gasoline to split The top reaction zone for changing the second riser, the oil gas and catalyst next with the lower part uplink from the second riser, which contact, to be dropped Olefine reaction, top reaction zone reaction temperature are 465 DEG C, in terms of the whole chargings for entering the second riser on the second riser Portion's reaction zone weight (hourly) space velocity (WHSV) is 5h^-1.Oil gas after reaction is separated, and is isolated dry gas, liquefied gas, the second riser and is catalyzed and splits Change gasoline, the second riser catalytic cracking light cycle oil, the second riser catalytic cracking heavy-cycle oil and the catalysis of the second riser Cracking slurry oil.All the first riser catalytic cracking light cycle oils of the second riser catalytic cracking light cycle oil and 50 weight % Into fixed bed hydrogenation reactor, whole second riser catalytic cracking heavy-cycle oil, all the second riser catalytic cracking slurry oil With all the first riser catalytic cracking heavy-cycle oil, all the first riser catalytic cracking slurry oil is reacted into boiling bed hydrogenation Device.

Table 1

Project name	Residual hydrogenation tail oil A	Paraffinic base residual oil B
			Density (20 DEG C)/(g/cm³)	0.9482	0.8950
Carbon residue/weight %	6.54	5.35
			Element mass fraction/%
Carbon/%	87.16	86.34
			Hydrogen/%	11.62	13.10
Sulphur/%	0.68	0.32
			Nitrogen/%	0.21	0.24
Ni	6.0	18.3
			V	5.9	0.3

Table 2

It can be seen that method light oil of the method provided by the invention than comparative example 1 from the comparison of embodiment 1 and comparative example 1 Yield is higher, and coke yield is lower, and gasoline olefin can be down to 15% or less volume content.

From the comparison of embodiment 1 and comparative example 2 as can be seen that the light oil yield of method provided by the invention and comparative example 2 It is similar, but the effect for dropping gasoline olefin is much better than comparative example 2, and the yield that highest gasoline is worth in product is higher than comparative example 2.

The embodiment of the present invention 2 describes the method and result of maximum production low-alkene gasoline, it can be seen that the present invention mentions The method of confession can maximum produce low-alkene gasoline, do not produce catalytic cracking diesel oil.

The embodiment of the present invention 3 describes while producing low-alkene gasoline and has on a small quantity compared with high cetane number catalytic cracking The method and result of diesel oil.

For heavy oil feedstock of the carbon residue content more than 5 weight %, using high-value product when conventional heavy oil catalytic cracking (gasoline+diesel oil+liquefied gas) yield is generally 82% or so.And method provided by the invention not only has and is significantly higher than conventional urge Change the high-value product yield of cracking, and low-alkene gasoline can be produced and compared with high cetane number catalytic cracking diesel oil, while can Diesel and gasoline ratio is adjusted flexibly, or even does not produce diesel oil fecund high value gasoline.

The preferred embodiment of the present invention has been described above in detail, and still, the present invention is not limited thereto.In skill of the invention In art conception range, can with various simple variants of the technical solution of the present invention are made, including each technical characteristic with it is any its Its suitable method is combined, and it should also be regarded as the disclosure of the present invention for these simple variants and combination, is belonged to Protection scope of the present invention.

Claims

1. a kind of method of processing of heavy oil, this method comprises:

(1) under the conditions of catalytic cracking reaction, by catalytically cracked stock be introduced to the first riser reaction zone of catalytic cracking into The first catalytic cracking reaction of row, and the product of the first catalytic cracking reaction is separated to obtain dry gas, liquefied gas, catalytic cracking vapour Oil, catalytic cracking light cycle oil, heavy catalytic cycle oil and catalytic cracked oil pulp；

(2) it will be introduced in boiling bed hydrogenation unit from at least partly described catalytic cracked oil pulp of step (1) and carry out first Hydrogenation reaction；Optionally and at least partly described catalytic cracking light cycle oil that come from step (1) ebullated bed will be introduced to add It carries out the first hydrogenation reaction in hydrogen unit and/or is introduced in fixed bed hydrogenation unit to carry out the second hydrogenation reaction；Optionally with And it will be introduced to progress first in boiling bed hydrogenation unit from at least partly described heavy catalytic cycle oil of step (1) and add Hydrogen, which is reacted and/or is introduced in fixed bed hydrogenation unit, carries out the second hydrogenation reaction；Separate first hydrogenation reaction and described The product of second hydrogenation reaction is to obtain adding hydrogen recycle oil；

(3) hydrogen recycle oil will be added to be introduced to the second riser of catalytic cracking lower reaction zone described in a part from step (2) The second catalytic cracking reaction of middle progress；By gasoline fraction and from step (2) another part described in plus hydrogen recycle oil be introduced to The second riser of catalytic cracking top reaction zone and together with catalyst and oil gas from the second riser lower reaction zone into Row third catalytic cracking reaction；Separate product after second catalytic cracking reaction and the third catalytic cracking reaction with Dry gas, liquefied gas, low Olefinic catalytic cracking gasoline, catalytic cracking light cycle oil, heavy catalytic cycle oil and catalysis is obtained to split Carburetion slurry, the gasoline fraction at least partially come from the catalytically cracked gasoline of step (1).

2. according to the method described in claim 1, wherein, in step (3), participate in second catalytic cracking reaction adds hydrogen Recycle oil and the weight ratio for adding hydrogen recycle oil for participating in the third catalytic cracking reaction are 1:(0.01~10).

3. method according to claim 1 or 2, wherein gently recycle at least partly catalytic cracking obtained in step (3) Oil, which is introduced in boiling bed hydrogenation unit, to be carried out the first hydrogenation reaction and/or is introduced to progress second in fixed bed hydrogenation unit to add Hydrogen reaction；Optionally and by least partly catalytic cracked oil pulp obtained in step (3) it is introduced in boiling bed hydrogenation unit Carry out first hydrogenation reaction；Optionally and by least partly heavy catalytic cycle oil introduces obtained in step (3) The first hydrogenation reaction is carried out into boiling bed hydrogenation unit and/or be introduced in fixed bed hydrogenation unit carry out second plus hydrogen it is anti- It answers.

4. method according to claim 1 or 2, wherein at least partly described catalytic cracked oil pulp of step (1) will be come from Or and described at least partly catalytic cracked oil pulp is introduced in boiling bed hydrogenation unit and carries out obtained in step (3) First hydrogenation reaction；Optionally and fixation will be introduced to from at least partly described catalytic cracking light cycle oil of step (1) The second hydrogenation reaction is carried out in bed hydroprocessing unit；Optionally and at least partly catalytic cracking obtained in step (3) Light cycle oil, which is introduced in fixed bed hydrogenation unit, carries out the second hydrogenation reaction；It optionally and will be from step (1) at least The part heavy catalytic cycle oil, which is introduced in boiling bed hydrogenation unit, to carry out the first hydrogenation reaction and/or is introduced to fixation The second hydrogenation reaction is carried out in bed hydroprocessing unit；Optionally and at least partly catalytic cracking obtained in step (3) Heavy-cycle oil, which is introduced in boiling bed hydrogenation unit, to carry out the first hydrogenation reaction and/or is introduced in fixed bed hydrogenation unit to carry out Second hydrogenation reaction.

5. method according to claim 1 or 2, wherein by whole catalytic cracked oil pulps from step (1) and from step Suddenly whole catalytic cracked oil pulp obtained in (3), which is introduced in boiling bed hydrogenation unit, carries out first hydrogenation reaction；And By whole catalytic cracking light cycle oils from step (1) and come from whole catalytic cracking light cycle oil obtained in step (3) It is introduced in boiling bed hydrogenation unit and carries out the first hydrogenation reaction and/or be introduced in fixed bed hydrogenation unit to carry out second plus hydrogen Reaction；And by whole heavy catalytic cycle oils from step (1) and come from whole catalytic cracking obtained in step (3) Heavy-cycle oil, which is introduced in boiling bed hydrogenation unit, to carry out the first hydrogenation reaction and/or is introduced in fixed bed hydrogenation unit to carry out Second hydrogenation reaction.

6. the method according to claim 3 or 4, wherein by from step (1) the catalytic cracking light cycle oil and The low Olefinic catalytic cracking gasoline from step (3) goes out device respectively as diesel product and gasoline products.

7. according to the method described in claim 5, wherein, the low Olefinic catalytic cracking gasoline conduct of step (3) will be come from Gasoline products go out device.

8. method according to any one of claims 1-7, wherein the reaction condition of first riser reaction zone Include: average reaction temperature be 450~540 DEG C, agent oil weight ratio be (2~15): 1, the residence time be 0.4~10 second；It is preferred that Ground,

The reaction condition of first riser reaction zone includes: that average reaction temperature is 470~500 DEG C, and agent oil weight ratio is (5~8): 1, the residence time is 0.8~3 second.

9. method according to any one of claims 1-7, wherein catalytic cracking the second riser lower part reaction The reaction condition in area includes: that average reaction temperature is 500~600 DEG C, and agent oil weight ratio is (2~30): 1, the residence time 0.4 ~10 seconds；Preferably,

The reaction condition of second riser of catalytic cracking lower reaction zone includes: that average reaction temperature is 530~570 DEG C, Agent oil weight ratio is (8~20): 1, the residence time is 0.8~3 second.

10. method according to any one of claims 1-7, wherein second riser of catalytic cracking top is anti- It is 350~520 DEG C that the reaction condition for answering area, which includes: average reaction temperature, and reaction weight (hourly) space velocity (WHSV) is 0.5~30h^-1；Preferably,

The reaction condition of second riser of catalytic cracking top reaction zone includes: that average reaction temperature is 350~449.99 DEG C, reaction weight (hourly) space velocity (WHSV) is 0.5~30h^-1；Preferably,

The reaction condition of second riser of catalytic cracking top reaction zone includes: that average reaction temperature is 350~449.99 DEG C, reaction weight (hourly) space velocity (WHSV) is 2~8h^-1。

11. according to claim 1, method described in any one of 9 and 10, wherein on second riser of catalytic cracking The average reaction temperature of portion's reaction zone is lower than the average reaction temperature of second riser of catalytic cracking lower reaction zone 30~ It is 150 DEG C, 40~120 DEG C preferably low, more preferably low 50~100 DEG C.

12. method described in any one of -11 according to claim 1, wherein promoted in the catalytic cracking second of step (3) In the reaction zone of pipe top, the gasoline fraction and described plus hydrogen recycle oil weight ratio are (0.2~100): 1；Preferably (1~ 6): 1.

13. according to the method described in claim 1, wherein, the second hydrogenation reaction in the fixed bed hydrogenation unit of step (2) Condition includes: that hydrogen partial pressure is 3.0~22.0MPa, and reaction temperature is 280~450 DEG C, and volume space velocity is 0.1~5.0h^-1, hydrogen oil Volume ratio is 200~2000Nm³/m³。

14. according to the method described in claim 1, wherein, the first hydrogenation reaction in the boiling bed hydrogenation unit of step (2) Condition includes: that hydrogen partial pressure is 3.0~22.0MPa, and reaction temperature is 280~450 DEG C, and volume space velocity is 0.1~5.0h^-1, hydrogen oil Volume ratio is 200~2000Nm³/m³。

15. according to the method described in claim 1, wherein, participating in first catalytic cracking reaction, second catalytic cracking Zeolite of the catalytic cracking catalyst each independently containing 5~50 weight % of reaction and the third catalytic cracking reaction, 5~ The clay of the inorganic oxide of 95 weight % and 0~70 weight %.

16. according to the method described in claim 1, wherein, first hydrogenation reaction and described second for participating in step (2) add Each independently containing carrier and load active metal component on the carrier in the hydrogenation catalyst of hydrogen reaction, optionally And contain molecular sieve, the active metal component is selected from vib metals element and/or group VIII non-noble metal j element, The carrier is selected from least one of aluminium oxide, silica and amorphous silica-alumina；Preferably,

The active metal component is selected from nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum, nickel-molybdenum-at least one of tungsten and cobalt-molybdenum combination.

17. a kind of system of processing of heavy oil, the system include:

First riser reaction zone contains the first reaction member and the first separative unit, catalysis in first riser reaction zone Cracked stock oil, which is introduced in first reaction member, carries out the first catalytic cracking reaction, and the first catalytic cracking reaction Product separated in first separative unit with obtain dry gas, liquefied gas, catalytically cracked gasoline, catalytic cracking light cycle oil, Heavy catalytic cycle oil and catalytic cracked oil pulp；

Hydrogenation unit, in the hydrogenation unit containing boiling bed hydrogenation reactor or and fixed bed hydrogenation reactor, and also Containing the second separative unit, the catalytic cracked oil pulp from first riser reaction zone enters the boiling bed hydrogenation The first hydrogenation reaction is carried out in reactor；Enter optionally from at least partly described catalytic cracking light cycle oil of step (1) It carries out the first hydrogenation reaction in the boiling bed hydrogenation reactor and/or enters in the fixed bed hydrogenation reactor to carry out second Hydrogenation reaction；It is anti-into the boiling bed hydrogenation optionally from at least partly described heavy catalytic cycle oil of step (1) It answers and carries out the first hydrogenation reaction in device and/or enter in the fixed bed hydrogenation reactor to carry out the second hydrogenation reaction；Described The product of one hydrogenation reaction and/or the product line of second hydrogenation reaction, which are introduced in second separative unit, to be divided From to obtain adding hydrogen recycle oil；And

Second riser reaction zone contains top reaction zone, lower reaction zone and third separation in second riser reaction zone Unit, a part from the hydrogenation unit is described plus hydrogen recycle oil carries out the second catalytic cracking in the lower reaction zone Reaction；Described in gasoline fraction and another part from the hydrogenation unit plus hydrogen recycle oil in the top reaction zone with come Third catalytic cracking reaction is carried out together from the catalyst and oil gas of the lower reaction zone；Through second catalytic cracking reaction Separated in the third separative unit with the product after the third catalytic cracking reaction with obtain dry gas, liquefied gas, Low Olefinic catalytic cracking gasoline, catalytic cracking light cycle oil, heavy catalytic cycle oil and catalytic cracked oil pulp.

18. system according to claim 17, wherein in second riser reaction zone, the top reaction zone Internal diameter be more than or equal to the lower reaction zone internal diameter；Preferably,

The ratio between internal diameter and the internal diameter of the lower reaction zone of the top reaction zone are (1.0~10): 1.

19. system according to claim 17, wherein second riser reaction zone and the hydrogenation unit pass through pipe Line connects so that the catalytic cracked oil pulp from second riser reaction zone is able to enter the boiling bed hydrogenation reactor It is middle to carry out first hydrogenation reaction；Optionally and at least partly catalysis from second riser reaction zone is split Change light cycle oil, which is able to enter in the boiling bed hydrogenation reactor, to carry out first hydrogenation reaction and/or is able to enter described Second hydrogenation reaction is carried out in fixed bed hydrogenation reactor；Optionally and make from second riser reaction zone At least partly heavy catalytic cycle oil be able to enter in the boiling bed hydrogenation reactor and carry out first hydrogenation reaction And/or it is able to enter in the fixed bed hydrogenation reactor and carries out second hydrogenation reaction.

20. system according to claim 17, wherein the top reaction zone of second riser reaction zone and lower part are anti- It answers and is provided with feed inlet in the join domain in area.