CN110373225A

CN110373225A - Usage of the rich aromatic hydrocarbons wax oil in heavy oil up flow type heat from hydrogenation cracking reaction process

Info

Publication number: CN110373225A
Application number: CN201810428995.XA
Authority: CN
Inventors: 何巨堂
Original assignee: Luoyang Rui Hua New Energy Technology Development Co Ltd
Current assignee: Luoyang Rui Hua New Energy Technology Development Co Ltd
Priority date: 2018-04-26
Filing date: 2018-04-26
Publication date: 2019-10-25

Abstract

Usage of the rich aromatic hydrocarbons wax oil in heavy oil up flow type heat from hydrogenation cracking reaction process, by rich aromatic hydrocarbons wax oil KVGO, matter wax oil is different by whole heavy oil R10F up flow type heat from hydrogenation cracking reaction process R10 i.e. introducing front conversion zone R10A such as in rich aromatic hydrocarbons or rich hydrogen supply hydrocarbon from existing usage, by the rear portion conversion zone R10B of KVGO introducing R10 without R10A, KVGO one way hot tearing rate can be significantly reduced, KVGO quantity can be significantly reduced under the identical target of KVGO conversion product wax oil quantity in guaranteeing R10 end product R10P, KVGO can double as the coolant of the R10B hot charge from R10A product to reduce dedicated coolant dosage；R10A, R10B can be significantly reduced, product separation system scale saves significantly on investment；KVGO can be the wax slop of matter wax oil in the isolate of R10P, wax tailings, heavy catalytic cycle oil, clarified oil or heavy crude petroleum.

Description

Usage of the rich aromatic hydrocarbons wax oil in heavy oil up flow type heat from hydrogenation cracking reaction process

Technical field

The present invention relates to rich aromatic hydrocarbons wax oils in the usage of heavy oil up flow type heat from hydrogenation cracking reaction process, will with existing usage Matter wax oil passes through whole heavy oil R10F up flow type heat from hydrogenation cracking reactions in such as rich aromatic hydrocarbons of rich aromatic hydrocarbons wax oil KVGO or rich hydrogen supply hydrocarbon Process R10 introduces front conversion zone R10A difference, can by the rear portion conversion zone R10B of KVGO introducing R10 without R10A KVGO one way hot tearing rate is significantly reduced, the identical target of KVGO conversion product wax oil quantity in guaranteeing R10 end product R10P Under can significantly reduce KVGO quantity, KVGO can reduce dedicated cold as the coolant of the R10B hot charge from R10A product But agent dosage；R10A, R10B can be significantly reduced, product separation system scale saves significantly on investment；KVGO can be point of R10P Wax slop from matter wax oil in object, wax tailings, heavy catalytic cycle oil, clarified oil or heavy crude petroleum；Hydrogen can be reduced Consumption reduces the quantity that KVGO condensation is residual oil, improves the economy of R10；KVGO can lead to together with R10P product residual oil THC-VR It crosses after hydro-upgrading takes off carbon residue reaction process and enters back into rear portion conversion zone R10B；The KVGO logistics of reduction, can be by being hydrocracked The conversion of the processing efficients such as reaction process, catalytic cracking reaction process.

Background technique

Heavy oil R10F of the present invention, 450 DEG C of the usual > of the normal boiling point of hydro carbons, 500 DEG C of general >, particularly > 530 DEG C, more particularly > 570 DEG C.

The up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F of the present invention refers to that heavy oil up flow type expands Bed hydroprocessing heat cracking reaction process, such as floating bed hydrogenation heat cracking reaction process, boiling bed hydrogenation heat cracking reaction process.

At least part occurs for the up flow type expanded bed heat from hydrogenation cracking reaction process R10 of heavy oil R10F of the present invention The heat cracking reaction of heavy oil R10F, the reaction of thermal cracking free radical stabilized hydrogenation generate the lower hydro carbons of at least part boiling point and produce Object；Heavy oil up flow type heat from hydrogenation cracking reaction process R10 usually cannot achieve one way and react whole lightings, and usually it is reasonable High conversion per pass is usually 70~85%, in such heat from hydrogenation cracked reaction product R10P there are certain amount such as 15~ 30% tail oil (heat from hydrogenation crackate residual oil) THC-VR.

If from the point of view of component structure, in heat from hydrogenation crackate residual oil THC-VR inherently heavy oil, macromolecular is not The residue or conversion product of lighting or the concentrate of thermal condensation object macromolecular, with its heat from hydrogenation cracking precursor raw material heavy oil R10F compared with boiling fraction, in general, gum level therein, asphalt content, carbon residue content are significantly increased and are such as increased 30~100%.

In order to improve the processing efficiency of device, preferably increase the conversion per pass of heavy oil R10F；And the one way of heavy oil R10F The raising of conversion ratio necessarily reduces residue oil fraction quantity in reaction product, while increasing thermal condensation object colloid, asphalitine, liquid phase Coke quantity, this " increase of colloid, asphalitine, the quantity of liquid phase coke " with " colloid, asphalitine, liquid phase coke solvent The reduction of oily quantity " develops to over-saturation degree or critical degree of saturation, will lead to colloid, asphalitine, liquid phase coke from stabilization Colloidal solution system in be precipitated become over-saturation pitch mutually be second liquid phase, lead to quick coking in the containers such as reactor, compel Device is set to stop work.

" conversion per pass for improving heavy oil R10F necessarily increases thermal condensation object colloid, asphalitine, liquid phase coke quantity " The fact that under the premise of, avoid " colloid, asphalitine, liquid phase coke be precipitated " method, necessarily reduce heavy oil R10F one way Conversion ratio introduces external solvent naphtha, is passively method due to reducing heavy oil R10F conversion per pass, can reduce device and add Therefore work efficiency rate " introduces external suitable colloid, asphalitine, the solvent naphtha of liquid phase coke and its application method ", just at One important technical problem, it is related to the economy of the up flow type expanded bed heat from hydrogenation cracking reaction process R10 of heavy oil R10F Property, and core of the invention target is, recognize " introduce external suitable colloid, asphalitine, liquid phase coke solvent naphtha " Under the premise of, existing solvent naphtha application method is proposed to improve to reduce solvent naphtha dosage, to rationally reduce R10 and product Separation system scale is to save significantly on investment, reduce hydrogen consumption, reduce the quantity that KVGO condensation is residual oil, improves the economy of R10.

Richness aromatic hydrocarbons wax oil KVGO of the present invention, the conventional boiling range of main hydro carbons is usually 370~570 DEG C, general It is 400~570 DEG C, in particular 450~550 DEG C.

Matter wax oil KVGO in richness aromatic hydrocarbons of the present invention, the conventional boiling range of main hydro carbons is usually 400~520 DEG C, Generally 425~510 DEG C, in particular 450~510 DEG C.

In heavy oil up flow type expanded bed heat from hydrogenation cracking reaction process, the application method of conventional wax oil solvent naphtha such as China Patent ZL200980118107.3, Chinese patent ZL200980145006.5, Chinese Patent Application No. 200980145007.X, in State patent ZL201080035430.7, be by selection rich aromatic hydrocarbons wax oil KVGO and initial feed heavy oil R10F mix into Row Unionfining thermal cracking.

Chinese patent ZL200980118107.3 is used for the choosing of heavy oil conversion and pressure reduction gas oil processing optimized and combined The recycling of selecting property heavy gas oil discloses a kind of for heavy oil conversion and the improved method of upgrading and a kind of for mink cell focus The combined method of conversion and pressure reduction gas oil processing.This process employs from vacuum distillation kettle generate individual product and by its Circulation, is then recycled back to heavy oil conversion reactor, the result is that producing quality higher than entire pressure reduction gas oil product Medium gas oil product (its in typical pressure reduction gas Method for treatment of oil using be acceptable)；In addition, having here Higher diesel yield selectivity from the heavy oil conversion unit, it can significantly improve diesel yield.Chinese patent ZL200980118107.3's is mainly characterized by comprising: that the boiling point of the component greater than 90wt% of weight vacuum gas oil (VGO) logistics is in 840- 1050(449~566 DEG C) range, a part therein is then recycled back to heavy oil conversion upgrading unit 21.? In this method, separation heavy oil conversion upgrading reaction product obtain wax slop HHVGO i.e. logistics 32, separation heavy oil conversion mention The initial feed decompression residuum 20 of the part residual oil that qualitative response product obtains i.e. logistics 30 and heavy oil conversion upgrading unit 21 is mixed It is combined and carries out Unionfining conversion upgrading reaction, have the advantages that process is simple, still, there are following main scarce Point:

1. wax slop HHVGO has passed through whole units 21, wax slop HHVGO residence time and initial feed heavy oil i.e. weight The residence time of vacuum gas oil (VGO) is identical, and therefore, the heat from hydrogenation cracking rate of wax slop HHVGO realizes under joint processing conditions It maximizes, the ratio of the wax oil fraction from wax slop HHVGO in the product 22 of unit 21 is minimum and generally produces one Quantitative thermal condensation object such as colloid, asphalitine, liquid phase coke, that is to say, that come from initial feed decompression residuum in product 22 The quantity of the adventitious solvent oil HHVGO-KL of 20 thermal condensation conversion product " colloid, asphalitine, liquid phase coke " be it is least, protecting Under the premise of the quantity of adventitious solvent oil HHVGO-KL in card product 22 is certain, the quantity of external wax slop HHVGO must be most Bigization, it is evident that the increased amplitude of specific gravity of the processing wax slop HHVGO of unit 21 is maximum, and the processing initial feed of unit 21 The amplitude that the ratio of decompression residuum 20 reduces is maximum, that is to say, that the reaction selectivity of unit 21 is greatly reduced；

Due to wax slop HHVGO, pass through the processing of fixed bed wax oil hydrogenation cracking reaction process, catalytic cracking reaction process Efficiency is much higher than heavy oil up flow type expanded bed heat from hydrogenation cracking reaction process (such as floating bed hydrogenation heat cracking reaction process, boiling Bed hydroprocessing heat cracking reaction process), therefore, the overall lighting processing efficiency of Chinese patent ZL200980118107.3 is lower ?；

2. wax slop HHVGO has passed through whole units 21, (including the front reaction of 21 total overall reaction processes is significantly increased Section and rear portion conversion zone), the scale of product separation system, significantly improve construction investment, increase and carried out the heat of wax slop HHVGO The quantity of condensation product residual oil increases gaseous product quantity；

3. wax slop HHVGO passes through the conversion product that unit 21 obtains, quality index is typically not capable of commodity requirement, thereafter Phase processing also needs to use through corresponding hydro-upgrading process, therefore causes overall plus hydrogen process longer, and overall hydrogen consumption is bigger, overall Economy reduces；

4. in wax slop HHVGO, the hydrocarbon component that normal boiling point is 520~566 DEG C is 450~520 DEG C than normal boiling point The hydrocarbon component is easier to thermal cracking, therefore is unfavorable for improving reduction hot tearing rate, its retention rate；

5. the boiling point of the component in wax slop HHVGO greater than 90wt% is within the scope of 449~566 DEG C, routine therein The hydrocarbon component that boiling point is 520~566 DEG C is difficult to vacuum fractionation with residue fraction (normal boiling point is 566~600 DEG C) and divides in other words It is high from energy consumption, while the hydrocarbon component that normal boiling point is 520~566 DEG C is in heat from hydrogenation cracking reaction process, high temperature fractional distillation process In be easy to generate thermal condensation object (colloid, asphalitine, liquid phase coke even solid coke).

Chinese patent ZL200980145006.5 is comprehensive to be hydrocracked and coking method in slurry, is disclosed and a kind of is prepared silt Slurry is hydrocracked the synthesis slurry hydrocracking (SHC) and coking method of (SHC) distillate.Typical method includes making comprising following again Ring SHC gas oil, coker gas oil, vacuum column Residual oil and solid particle slurry pass through in presence of hydrogen SHC reaction zone with Obtain SHC distillate.Another possibility comprehensive with coking plant is provided by the fractionation recycling SHC pitch of SHC reaction zone effluent Property, especially by coking plant promoted SHC pitch to provide coke and compared with lighter hydrocarbons, such as SHC vacuum gas oil (VGO)。

The slurry hydrocracking reaction process 20 described in Chinese patent ZL200980145006.5 can combine processing weight Decompression residuum, that is, logistics 4 of oil 12, decompressed wax oil, that is, logistics 5a of heavy oil 12,20 product of slurry hydrocracking reaction process point The fractionation fraction wax oil i.e. logistics 2 of the coking product of fraction wax oil i.e. logistics 3, coking 30, above-mentioned a few road material mixing It carries out combining slurry hydrocracking reaction together, has passed through whole slurry hydrocracking reaction process 20, therefore, China is specially Sharp ZL200980145006.5 equally has some or all of Chinese patent ZL200980118107.3 presence aforesaid drawbacks.

The comprehensive solvent deasphalting of Chinese Patent Application No. 200980145007.X and slurry hydrocracking method, disclose Prepare the synthesis slurry hydrocracking (SHC) and coking method of slurry hydrocracking (SHC) distillate.Typical method includes making Produced in solvent deasphalting (SDA) method comprising deasphalted oil (DAO), optionally with recycling SHC gas oil and recycle SHC The slurry of pitch and solid particle passes through SHC reaction zone in presence of hydrogen to obtain SHC distillate.SHC gas oil and pitch From the recycling in SHC effluent and improvement is recycled to the total conversion of naphtha and distillate product and reduces catalyst need It asks.

The slurry hydrocracking reaction process 20 described in Chinese Patent Application No. 200980145007.X can combine and add The deasphalted oil 2 of work heavy oil 10,20 product 13 of slurry hydrocracking reaction process the hot high score oil 3 in part, slurry hydrocracking Fractionation fraction wax oil, that is, logistics 17 (including the heat from hydrogenation cracking light VGO, heat from hydrogenation cracking heavy of 20 product of reaction process VGO), portion of product residual oil, that is, logistics 9 of slurry hydrocracking reaction process 20, above-mentioned a few road materials, which mix, to be joined Heat from hydrogenation cracking is closed, whole slurry hydrocracking reaction process 20, therefore, Chinese Patent Application No. have been passed through 200980145007.X equally having some or all of Chinese patent ZL200980118107.3 presence aforesaid drawbacks.

Chinese patent ZL201080035430.7 from slurry hydrocracking vacuum gas oil (VGO) and composition for separating The method and apparatus of pitch, discloses a kind of for heavy hydrocarbon charge to be converted to the method and apparatus compared with lighter hydrocarbons product, will weigh Matter hydrocarbon charging particulate solid material pulp is to form heavy hydrocarbon slurry and be hydrocracked in slurry hydrocracking unit to produce Raw vacuum gas oil (VGO) (VGO) and pitch.First vacuum column is by VGO and separated from bitumen, and the second vacuum column is further by more heavy VGO and separated from bitumen.The VGO of similar 15 weight % can be recovered and recycled to slurry hydrocracking portion by the second vacuum column Divide 20.It obtains can be made into particle and is not bonded to bituminous composition together when transporting.

The slurry hydrocracking part 20 described in Chinese patent ZL201080035430.7, can combine processing heavy hydrocarbon Raw material 12,20 product wax oil of slurry hydrocracking reaction process, that is, logistics 8 (including matter VGO, that is, logistics 97 in heat from hydrogenation cracking plus Hydrogen thermal cracking heavy VGO, that is, logistics 116), above-mentioned a few road materials, which mix, carries out Unionfining thermal cracking, has passed through whole Slurry hydrocracking reaction process 20, therefore, Chinese patent ZL201080035430.7 equally has Chinese patent Some or all of ZL200980118107.3 presence aforesaid drawbacks.

The shortcomings that in order to overcome above-mentioned prior art, improves the economy of wax oil solvent naphtha use process, base of the invention This imagination is: rich aromatic hydrocarbons wax oil heavy oil up flow type heat from hydrogenation cracking reaction process usage, with existing usage by rich aromatic hydrocarbons wax Matter wax oil is by whole heavy oil R10F up flow type heat from hydrogenation cracking reaction process R10 in such as rich aromatic hydrocarbons of oily KVGO or rich hydrogen supply hydrocarbon Front conversion zone R10A difference is introduced, KVGO is introduced into the rear portion conversion zone R10B of R10 without R10A, can be significantly reduced KVGO one way hot tearing rate, can be significant under the identical target of KVGO conversion product wax oil quantity in guaranteeing R10 end product R10P KVGO quantity is reduced, KVGO can reduce dedicated coolant as the coolant of the R10B hot charge from R10A product and use Amount；R10A, R10B can be significantly reduced, product separation system scale saves significantly on investment；KVGO can be in the isolate of R10P Matter wax oil, wax tailings, heavy catalytic cycle oil, clarified oil or heavy crude petroleum wax slop；Hydrogen consumption, drop can be reduced Low KVGO condensation is the quantity of residual oil, improves the economy of R10；KVGO can be with R10P product residual oil THC-VR together by adding hydrogen Rear portion conversion zone R10B is entered back into after modifying de- carbon residue reaction process；The KVGO logistics of reduction can pass through hydrocracking reaction mistake The conversion of the processing efficients such as journey, catalytic cracking reaction process.

By and large, heavy oil floating bed hydrogenation heat cracking reaction process R10 can be divided into before inhibiting coking as far as possible The rear portion of sufficient " colloid, the asphalitine, liquid phase coke " dispersion solvent of portion either shallow heat cracking reaction process R10A and as far as possible offer Depth heat cracking reaction process R10B improves the outer solubilization of reaction result in addition to using high degree of dispersion, high-activity hydrogenation catalyst Agent oil logistics and usage thereof principle should be:

1. in front either shallow heat cracking reaction process, the sufficient normal boiling point of usage quantity is between 250~450 DEG C) range Hydrogen supply hydrocarbon, using its carry hydrogen load is high, heat movement speed is fast, lose hydrogen body plus hydrogen bring back to life fireballing feature, realize a large amount of Hydrogen, quick hydrogen supply are carried, the colloid, asphalitine in raising heavy oil feedstock add hydrogen lighting, reduce the initial stage hot tearing of heavy oil feedstock The thermal condensation of change process prepares raw material for rear portion depth heat cracking reaction process；

2. in rear portion depth heat cracking reaction process, it is preferred to use the sufficient normal boiling point of quantity is between 450~510 DEG C) Matter wax oil solvent in the rich aromatic hydrocarbons of range is difficult to thermal cracking, to " colloid, asphalitine, liquid phase coke " dispersing and dissolving energy using it The strong feature of power is in " colloid, the asphalitine, liquid phase coke " component in the depth heat cracking reaction product of rear portion far from dissolution Dilute colloidal solution state of saturated mode, in the case where improving heavy-oil hydrogenation thermal cracking conversion ratio and extending the operation target in operation cycle, Colloid in liquid solution, asphaltene concentration is effectively reduced, prevent gum asphalt be precipitated become second liquid phase, it is ensured that solution it is steady It is qualitative；In high performance richness aromatic hydrocarbons in such as rich hydrogen supply hydrocarbon of matter wax oil solvent matter wax oil have it is strong to gum asphalt solvability, The overall merit of rich hydrogen supply capacity, anti-coking；

Meanwhile rear portion depth heat cracking reaction process needs to be discharged lightweight saturated hydrocarbons in time and prevents its from reducing solution fragrance Degree；The liquid circulation reactor assembly with gas function can be used thus；

3., can be by front either shallow heat cracking reaction in order to improve the conversion per pass of rear portion depth heat cracking reaction process Hydrogen supply dissolvent in product isolates a part, reduces its inhibiting effect to heat cracking reaction；

Why use normal boiling point between 450~510 DEG C of the hydrocarbon component as rich aromatic hydrocarbons heavy solvent, be simultaneously based on Under some factors and determination:

First, boiling point is high, is not easy to vaporize, during high pressure-temperature reaction process and air-distillation, largely be rendered as Liquid phase is efficient liquid phase solvent；

Second, relative to residual oil macromolecular, matter wax oil solvent composition is more difficult to thermal cracking in such richness aromatic hydrocarbons, therefore can To improve its retention rate；

Third, there are certain boiling-point differences with residue fraction (normal boiling point is higher than 570 DEG C of the hydrocarbon component), convenient for decompression point From convenient for being recycled；

4. such material is easily obtained in oil plant there are many source, heavy-cycle oil, clarification such as heavy oil catalytic cracking Oil, such as the wax slop of coking heavy oil, such as the middle matter wax oil of heavy-oil hydrogenation thermal cracking process, the wax slop of viscous crude, the wax of coal tar Oil distillate, ethylene cracking tar etc.；

5. matter wax oil in the product of heavy-oil hydrogenation thermal cracking process, and rich aromatic hydrocarbons heavy solvent, outer for rich aromatic hydrocarbons weight in this way The pollution level that the hydro-conversion object of solvent is saturated the hydrocarbon component is lower.

In general, it is outer molten as rich aromatic hydrocarbons weight for rich aromatic hydrocarbons light wax oil between 350~430 DEG C that normal boiling point also can be used Agent, although it must be noted that the product lightweight wax oil of heavy-oil hydrogenation thermal cracking process, be arene content it is very low (usually 15~ 30%) hydrocarbon ils, in this way with the outer hydro-conversion object for rich aromatic hydrocarbons light wax oil solvent of boiling range by the light wax of heavy-oil hydrogenation thermal cracking The pollution level of oily saturated hydrocarbon component is higher, to be not easy to recycle.

In fact, within the scope of a set threshold thermal cracking conversion ratio, the liquid of heavy oil up flow type heat from hydrogenation cracking reaction process Phase is able to maintain that the stability of colloidal solution not will form second liquid phase, that is to say, that in the heavy oil up flow type of high conversion The front conversion zone of heat from hydrogenation cracking reaction process, the solvent composition of " colloid, asphalitine, liquid phase coke " are adequately, excessively Additional addition wax oil solvent naphtha is unnecessary.The present invention exactly utilizes this feature and formulates.

And in order to reduce outlet tail oil quantity, it is often necessary to the heat from hydrogenation cracking reaction process of tail oil is set, and for letter Change overall procedure, reduce investment and energy consumption, usually by the up flow type of the heat from hydrogenation cracking reaction process of the tail oil and heavy oil R10F Heat from hydrogenation cracking reaction process R10 forms group technology.

In general, the quantity of the tail oil THC-VR of heavy oil up flow type heat from hydrogenation cracking reaction process is seldom compared with heavy oil feedstock It for example is usually the 0.15~0.30 of heavy oil weight, therefore hydrogen supply dissolvent is easy to use for example to reach 0.5~2.0 in high solvent-oil ratio High solvent-oil ratio under the conditions of, carry out floating bed hydrogenation saturated reaction and obtain plus hydrogen saturated products CRP, then can enter and react Journey R10 realizes that the secondary of hydrogen supply dissolvent is used in series.The secondary of hydrogen supply dissolvent in CR reaction process is used in series mode, can be with It is that the separation process R10AP-THPS that CRP enters reaction process R10A, R10B, or can be into R10AP isolates hydrogen supply Enter bis- series connection of reaction process R10B processing after solvent and carry out appropriate heat from hydrogenation cracking, heat from hydrogenation cracked vacuum slag is recycled Be enriched in oily THC-VR have hydrogenation catalyst act on particle can strengthen hydrogen activation and hydrogen supply reaction, enrichment it is other Solid particle have may green coke carrying capacity, the synergistic effect between above-mentioned element is advantageous, objective reality.

It, can be as hydrogen supply dissolvent in heavy-oil hydrogenation thermal cracking when rich aromatic hydrocarbons wax oil hydrogen supply capacity with higher The up flow type expanded bed hydrogenation modification reaction process CR of tail oil THC-VR is used first, in the presence of a large amount of hydrogen-abstracting agents, Fu Fang Chloroflo oil is main to occur dehydrogenation and aromatization rather than hydrogenation reaction, and the retention rate of aromatic hydrocarbons wax oil rich in this way is higher, still may be used It is used with serving as rich aromatic hydrocarbons wax oil KVGO, at this point, the product of reaction process CR is introduced the heat from hydrogenation cracking of heavy oil R10F up flow type The rear portion conversion zone R10B of reaction process R10, may be implemented the conversion product of rich aromatic hydrocarbons wax oil KVGO, hydrogen, catalyst it is secondary It uses, the hydrogenation modification reaction product and heavy oil R10F up flow type heat from hydrogenation cracking reaction process of tail oil THC-VR may be implemented The Unionfining thermal cracking of the front conversion zone R10B product of R10, to improve the service efficiency of rich aromatic hydrocarbons wax oil KVGO.

Richness aromatic hydrocarbons wax oil KVGO of the present invention, can be the hydrocarbon ils all the way in 1 source, can be the 2 road hydrocarbon in 2 sources The miscella of the multichannel hydrocarbon ils in oily or multiple sources；Since the present invention can carry out rich virtue using up flow type expanded bed reactive mode The hydro-upgrading of chloroflo oil KVGO reacts, therefore, allow richness aromatic hydrocarbons wax oil KVGO contain a certain number of solids, carry secretly it is a certain amount of Colloid, asphalitine, that is to say, that rich aromatic hydrocarbons wax oil KVGO can contain a small amount of residue fraction, therefore, the present invention richness aromatic hydrocarbons Wax oil KVGO can be rich aromatic hydrocarbons wax oil KVGO inferior, in this way, being conducive to obtaining the separation or fractionation of rich aromatic hydrocarbons wax oil KVGO In step, rich aromatic hydrocarbons wax oil KVGO yield is improved, the yield of residual oil is reduced.

The present invention, can be by the Process flow of variation hydrogenation processes at different levels, can be other suitable by joint processing In the hydrocarbon material of joint processing, a variety of groups can be formed by the downstream processing methods of hydrocarbon ils in a variety of hot high score gas of joint Close technique.

For specific application, as needed, the present invention is to existing heavy-oil hydrogenation hydrogen addition technology (including Chinese patent ZL201210022921.9, Chinese patent ZL201610525311.9) it can reasonably select use or be used cooperatively.

The present invention, when rich aromatic hydrocarbons wax oil KVGO is Rfcc Products wax oil (heavy-cycle oil, clarified oil), actually The group technology of heavy oil catalytic cracking process Yu heavy-oil hydrogenation thermal cracking process is constituted, Rfcc Products wax is realized The hydrogenation modification of oily (heavy-cycle oil, clarified oil) and heat from hydrogenation cracking, on the one hand reduce the processing of catalytic cracking reaction process Load reduces coke yield, increases liquid receipts, on the other hand increases the middle matter wax oil solvent of heavy-oil hydrogenation thermal cracking process Quantity, reduce heavy-oil hydrogenation heat cracking reaction process thermal condensation object (colloid, asphalitine, coke) yield, increase liquid It receives, increases the quantity of the dispersant solvent oil of gum asphalt in heavy-oil hydrogenation hot cracked product, be conducive to improve heavy-oil hydrogenation Thermal cracking conversion ratio reduces coke output, significantly improves the economy of overall process in short, being conducive to improve fraction oil yield.

Heavy-oil hydrogenation hot cracked product light wax oil can go catalytic cracking reaction process or catalytic cracking reaction process, with Voluminous catalytically cracked gasoline and/or catalytic cracking diesel oil, and the precursor that catalytic cracking diesel oil may be used as lightweight hydrogen supply dissolvent makes With.

The present invention actually constitutes coking heavy oil process and heavy oil when rich aromatic hydrocarbons wax oil KVGO is coking product wax oil The group technology of heat from hydrogenation cracking process realizes hydrogenation modification and the heat from hydrogenation cracking of wax tailings, on the one hand reduces coke Change the machining load of reaction process, reduce coke yield, increase liquid receipts, on the other hand increases heavy-oil hydrogenation thermal cracking The middle matter wax oil amount of solvents of journey, the thermal condensation object (colloid, asphalitine, coke) for reducing heavy-oil hydrogenation heat cracking reaction process Yield, increase liquid receipts, increase the quantity of the dispersant solvent oil of gum asphalt in heavy-oil hydrogenation hot cracked product, it is sharp In improving heavy-oil hydrogenation thermal cracking conversion ratio, in general, it is conducive to improve fraction oil yield, reduces coke output, significantly improve The economy of process.

Particularly, compared with without using the conventional heavy-oil hydrogenation heat cracking reaction process of hydrogen supply dissolvent, hydrogen supply dissolvent is used Heavy-oil hydrogenation heat cracking reaction process, under the conditions of identical heat from hydrogenation cracking conversion rate, heat from hydrogenation crackate residual oil Hydrogen content can dramatically increase, carbon residue can significantly reduce, the heat from hydrogenation cracked residue as circulation heat from hydrogenation cracked stock slag Oily then be easier to heat from hydrogenation cracking, then coke produces when which is used as coking raw material as outer oil extraction Rate is lower, to be conducive to improve coking distillate yield, if also mixed in the feedstock oil of coking such as delayed coking The molten wax oil of a certain proportion of hydrogen supply is refined, then forms hydrogen supply pyrogenetic reaction process, which allows heavy-oil hydrogenation hot tearing Change reaction process and processes (carbon residue content is higher) more inferior, the lower residual oil of price.The heavy-oil hydrogenation thermal cracking process and heavy oil The group technology of coking, particularly suitable for creating the combination of heavy-oil hydrogenation thermal cracking process and existing coking heavy oil process.

Matter wax oil or its hydrogenation modification oil, Rfcc Products wax oil are (heavy-cycle oil, clear in heavy-oil hydrogenation thermal cracking Edible vegetable oil) hydrogenation modification oil, coking heavy oil product wax oil or its hydrogenation modification oil, such as delayed coking of coking reaction process can be gone Reaction process or fluid coking reaction process or flexicoking reaction process serve as the hydrogen supply dissolvent oil with certain hydrogen supply capacity It uses, the pyrogenetic reaction process that carries out is combined with heavy-oil hydrogenation thermal cracking residue, the pyrogenetic reaction process usually also joint processing is straight Decompression residuum is evaporated to control content of ashes, the tenor in the carbon residue content and/or product char of overall coking raw material oil, and Heavy-oil hydrogenation thermal cracking process is carried using that can reduce heavy-oil hydrogenation hot cracking catalyst solid and coke after hydrogen supply dissolvent The dosage of agent solid, to be conducive to the operating effect of the pyrogenetic reaction process of optimization heavy-oil hydrogenation thermal cracking residue；At this point, coking Reaction process can increase substantially the efficiency of processing decompression residuum using ultralow recycle ratio even zero recycle ratio operation scheme.

The method of the invention has not been reported.

Therefore, the first object of the present invention is to propose rich aromatic hydrocarbons wax oil in heavy oil up flow type heat from hydrogenation cracking reaction process Usage.

The second object of the present invention is to propose a kind of total heavy-oil hydrogenation method for thermal cracking for refining rich aromatic hydrocarbons wax oil, heavy oil feedstock It may include heavy-oil hydrogenation hot cracked product residual oil, to constitute circulation thermocracking process.

The third object of the present invention is to propose the combination of heavy oil catalytic cracking process, heavy oil up flow type heat from hydrogenation cracking process Method, the hydrocarbon ils rich in 2~4 ring structure aromatic hydrocarbons that heavy oil catalytic cracking process (or heavy-oil catalytic thermal cracking process) is generated (wax slop of catalytic cracking diesel oil and/or catalytic cracking wax oil and/or hydrocarbon material up flow type heat from hydrogenation cracking process) is as rich virtue Chloroflo oil uses, and heavy-oil hydrogenation hot cracked product light wax oil can go catalytic cracking reaction process with voluminous catalytically cracked gasoline And/or catalytic cracking diesel oil, to constitute a kind of heavy-oil catalytic thermal cracking process, hydrogenation of residual oil suspended bed warmly changes the group of process It closes.

The fourth object of the present invention is to propose the heavy oil up flow type heat from hydrogenation cracking process using rich aromatic hydrocarbons wax oil, get rid of contain outside Gu residuum coking process combined method, get rid of outside oil containing solid slag as coking raw material can go coking such as delayed coking or Refining processing is individually processed or mixed to fluid coking process or Flexicoking process, and the gas that coking generates can be used as hydrogen manufacturing Waste hydrogen, it is molten that the hydrocarbon ils rich in double ring arene and/or polycyclic aromatic hydrocarbon that coking generates can be used as good hydrogen supply Agent precursor, which enters, combines processing in group technology of the invention, to constitute the big of a kind of coking and processing of heavy oil process Combination.

The fifth object of the present invention is to propose the heavy oil up flow type heat from hydrogenation cracking process using rich aromatic hydrocarbons wax oil, get rid of contain outside Solid slag oil mixes the processing combined method of coal coking process, gets rid of oil containing solid slag outside and coal coking process is gone to be used as blending Raw material processing, And the gas that process of coking generates can be used as hydrogen feedstock hydrogen making, process of coking generate rich in double ring arene and/or more The hydrocarbon ils of cycloaromatics can be used as good hydrogen supply dissolvent precursor and enter joint processing in group technology of the invention, thus structure At the big combination of a kind of coal coking process and processing of heavy oil process.Outside get rid of oil containing solid slag as coal coking process ingredient in use, The oil containing solid slag as room temperature solid is used as coking raw material with coking coal blending after individually crushing or room temperature is solid containing solid Residual oil crushes together after blending with coking coal is used as coking raw material, since oil containing solid slag is rich in colloid, asphalitine, in high-temperature coking Process is equivalent to the use of the coal rich in gel, compared with the gel inside coal particle, the ratio of the gel from residual oil More greatly, mobility is more preferable, and energy filled solid particulate interspaces have good cementation；With the gel phase inside coal particle Than, first, the molecular weight of the gel from residual oil is smaller, thus its to be heated the critical transition temperature with mobility lower It can enter flow regime in advance in heating process, the hydrogen content of the second gel from residual oil is higher, so its dehydrogenation is solid The time of change, longer i.e. colloidal state was longer there are the time, therefore had better bond effect；Containing solid coking of residues product, First part's product, that is, coked solid becomes the component part of coke, the second part product, that is, high temperature thermal cracking reaction of process of coking Raw gas is generated, raw gas is the gas comprising components such as hydrogen, conventional gas hydrocarbon, tar, the available tar of coal gas is separated, Tar or tarry distillate enter heavy hydrocarbon up flow type hydro-upgrading process inferior and/or hydrocarbon material up flow type heat from hydrogenation cracking process connection Close processing.

Summary of the invention

Usage of the richness aromatic hydrocarbons wax oil of the invention in heavy oil up flow type heat from hydrogenation cracking reaction process, it is characterised in that comprising with Lower step:

(1) cracking reaction of up flow type heat from hydrogenation is carried out in heavy oil up flow type heat from hydrogenation cracking reaction process R10, heavy oil R10F It is converted into final product R10P；

Heavy oil up flow type heat from hydrogenation cracking reaction process R10 includes front conversion zone R10A and rear portion conversion zone R10B；

In front conversion zone R10A, there are hydrogen, conventional liq hydrocarbon simultaneously there may be hydrogen supply hydrocarbon, there may be solids Under the conditions of the mixed phase material of particle, at least part heavy oil R10F carries out hydrogenation reaction R10A-R and at least part heat from hydrogenation occurs Cracking reaction is converted into hydrogenation reaction product R10AP；Front conversion zone R10A, possible simultaneous processing is other to contain residual oil streams；

The hydrocarbonaceous liquid for being higher than 530 DEG C of the hydrocarbon components containing at least part normal boiling point based on hydrogenation reaction product R10AP Material R10AP-LX enters rear portion conversion zone R10B；

In rear portion hydrogenation reaction section R10B, there are hydrogen, conventional liq hydrocarbon simultaneously there may be hydrogen supply hydrocarbon, there may be Under the conditions of the mixed phase material of solid particle, the hydrocarbonaceous liquid material R10AP-LX of at least part carry out hydrogenation reaction R10B-R occur to Few a part of heat from hydrogenation cracking reaction is converted into hydrogenation reaction product R10BP；Rear portion hydrogenation reaction section R10B, possible simultaneous processing It is other to contain residual oil streams；

The rich aromatic hydrocarbons wax for mainly containing solid particle between the possibility that 370~550 DEG C of the hydrocarbon component forms by normal boiling point Oily KVGO, into rear portion conversion zone R10B and without front conversion zone R10A, with hydrocarbonaceous liquid material R10AP-LX or its add hydrogen Conversion product contact carries out hydrogenation reaction, and the heat from hydrogenation cracking conversion product of rich aromatic hydrocarbons wax oil KVGO enters heat from hydrogenation cracked reaction product In R10BP；

Final product R10P includes heat from hydrogenation cracked reaction product R10BP；

(2) it is separated into thermal high separate section S100, R10BP comprising conventional hydrogen, conventional gas hydrocarbon, conventional liq hydrocarbon Gas S100V and the liquid material S100L that liquid phase component is mainly made of conventional liq hydrocarbon of solid may be contained；

(3) in liquid material recovery section S100L-GU, separation mainly may form liquid phase by conventional liq hydrocarbon containing solid The liquid material S100L of component is obtained that the hydrocarbon mainly by normal boiling point higher than 520 DEG C forms and is higher than 570 DEG C containing normal boiling point The heat from hydrogenation cracked vacuum residue THC-VR for containing solid particle rich in colloid, the possibility of asphalitine.

The present invention, in general, (4) separate gas S100V and obtain hydrogen-rich gas HPV in gas recovery section S100V-GU, until Few a part of hydrogen rich gas gas HPV enters hydrogenation process use；The hydrogen volume concentration of hydrogen rich gas gas HPV is in general, big In 75%, generally higher than 85%.

The present invention, in general, heavy oil R10F, mainly the hydrocarbon component by normal boiling point higher than 530 DEG C is formed.

The present invention, there are powder, existing powders can be selected from following by heavy oil up flow type heat from hydrogenation cracking reaction process R10 In a kind or several:

1. catalyst solid particle；

2. sulphur powder；

3. hydrocarbon ils coking material carrier semicoke particle；

4. heavy oil up flow type heat from hydrogenation cracking reaction process R10 needs the other solid powders inputted.

The present invention, heavy oil up flow type heat from hydrogenation cracking reaction process R10, the work side of the hydrogenator R10UE used Formula can a kind or several in following:

1. suspended-bed reactor, that is, paste state bed reactor；

2. fluidized bed reactor；

3. suspension bed and ebullated bed combination type reactor.

Option 1, liquid material and gas material use the counter-current reactor of pure adverse current working method；

Option 2, reactor R10UE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of reactor R10UE material inlet；

Option 3, reactor R10UE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of reactor R10UE material inlet；

Option 4, reactor R10UE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of reactor R10UE material inlet, while circulating pump conveys circulation fluid, downstream transport liquid material product；

Option 5, reactor R10UE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of reactor R10UE material inlet, while circulating pump conveys circulation fluid, downstream transport liquid material product；

Option 6, reactor R10UE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of reactor R10UE material inlet is collected simultaneously other collection liquids of cup discharge by other dedicated feedings Pump downstream transport liquid material product；

Option 7, reactor R10UE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of reactor R10UE material inlet is collected simultaneously other collection liquids of cup discharge by other dedicated feedings Pump downstream transport liquid material product；

Option 8, reactor R10UE, top are arranged liquid collecting cup and liquid material product are discharged by dedicated feeding engine downstream transport Liquid material product is not provided with the fluidized bed reactor system of liquid material product forced circulation；

Option 9, reactor R10UE, top are arranged liquid collecting cup and liquid material product are discharged by dedicated feeding engine downstream transport Liquid material product is not provided with the suspended-bed reactor system of liquid material product forced circulation；

Option 10, reactor R10UE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor R10UE material inlet and the combination type reactor of ebullated bed；

Option 11, reactor R10UE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor R10UE material inlet and the combination type reactor of ebullated bed, while circulating pump conveys circulation fluid, downwards Trip conveying liquid material product；

Option 12, reactor R10UE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor R10UE material inlet and the combination type reactor of ebullated bed are collected simultaneously other collection liquids of cup discharge By other dedicated feeding engine downstream transport liquid material products；

The suspended-bed reactor system of flow pattern under the center upstream surrounding of internal guide cylinder is arranged in option 13；

The suspended-bed reactor system of flow pattern in the dirty surrounding in center of internal guide cylinder is arranged in option 14；

Option 15, empty cylinder bubbling bed suspended-bed reactor system；

Option 16 is formed reactor top reaction zone liquid phase and is flowed down under Returning reactor using the external circulation pipe of reactor The device outside circulation of portion's reaction zone；

Option 17, in reactor R10UE, setting enters stripping step and the top of the end gas-liquid product of top liquid collecting cup Liquid collecting cup gas-liquid separation step, the average molecular weight for the balance liquid phase that hydrogen rich gas gas stripping gas is formed after mixing with end gas-liquid product Greater than the average molecular weight of the balance liquid phase of end gas-liquid product, what hydrogen rich gas gas stripping gas was formed after mixing with end gas-liquid product The concentration for the hydrocarbon component that the normal boiling point for balancing liquid phase is higher than 350 DEG C is greater than the normal boiling point of the balance liquid phase of end gas-liquid product The concentration of the hydrocarbon component higher than 350 DEG C；The slurries that liquid collecting cup in the final reactor of autoreaction section is discharged through diversion pipe, as Conversion zone product slurry or circular response liquid phase.

The present invention, in heavy oil up flow type heat from hydrogenation cracking reaction process R10, conversion zone obtains the mode of product liquid, can With a kind or several in following manner:

1. the slurries that the gas-liquid separation process of autoreaction section reaction product is discharged, as final reaction section product slurry；

2. the final reactor of conversion zone uses pure counter-current reactor, the bottom liquid phase region of the final reactor of autoreaction section The slurries of discharge, as conversion zone product slurry；

3. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup warp in the final reactor of autoreaction section The slurries of diversion pipe discharge, as conversion zone product slurry；

4. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup warp in the final reactor of autoreaction section The slurries of diversion pipe discharge, as slurry to be de-gassed；

Possibility to be de-gassed contains the liquid of solid, by cyclonic separation step be separated into all the way rich in bubble liquid stream, The liquid stream of lean gas bubble all the way；The liquid stream of lean gas bubble, the possibility as conversion zone contain the product liquid of solid；

5. setting enters stripping step and the top of the end gas-liquid product of top liquid collecting cup in the final reactor of conversion zone Portion's liquid collecting cup gas-liquid separation step, the mean molecule for the balance liquid phase that hydrogen rich gas gas stripping gas is formed after mixing with end gas-liquid product Amount is greater than the average molecular weight of the balance liquid phase of end gas-liquid product, and hydrogen rich gas gas stripping gas is formed after mixing with end gas-liquid product Normal boiling point the conventional of balance liquid phase that is greater than end gas-liquid product higher than the concentration of 350 DEG C of the hydrocarbon component of balance liquid phase boil The concentration of the hydrocarbon component of the point higher than 350 DEG C；The slurries that liquid collecting cup in the final reactor of autoreaction section is discharged through diversion pipe are made For conversion zone product slurry or circular response liquid phase.

The present invention, the mode of operation of (1) heavy oil up flow type heat from hydrogenation cracking reaction process R10 can in following 1 Kind is several:

1. heavy oil up flow type heat from hydrogenation cracking reaction process R10, operating condition are as follows: reaction temperature is 400~485 DEG C, instead Answering device pressure is 6~30MPa, and vapor phase hydrogen volumetric concentration 50~95%, gas-liquid volume ratio is 300~1500Nm³/m³, hydrogen is added to urge Agent additive amount is 0.1~3 mass % of dry pulverized coal weight, and co-catalyst additive amount is sulphur/catalyst activity in co-catalyst The molar ratio of metal is 1.0~2.0, and coal slurry solid concentration is 40~60 mass %, and reaction time TRU is 0.5~4 small When；

2. heavy oil up flow type heat from hydrogenation cracking reaction process R10, the heat from hydrogenation Cracking catalyst used are a kind of compound Hydrogenation catalyst includes high-activity component and low activity component；The weight of the high-activity component metal and low activity component metals Amount is than being 1: 10 to 10: 1；The high-activity component contain molybdenum oil-soluble salt compounds water soluble salt compound or its Mixture；The low activity group is divided into ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, adds Hydrogen hot cracking catalyst water content is lower than 2wt%；The powdered granule that heat from hydrogenation cracking catalyst particles diameter is 1~100 μm；

3. heavy oil up flow type heat from hydrogenation cracking reaction process R10, the heat from hydrogenation Cracking catalyst used includes that nanometer is ultra-fine Particle aqua oxidation iron catalyst and/or iron oxide and/or pyrite and/or bloodstone and/or molybdenum oxide and/or molybdenum sulfide and/or molybdenum Sour ammonium and/or nickel sulfide.

The present invention, in general, heavy oil up flow type heat from hydrogenation cracking reaction process R10, uses at least part hydrogen supply dissolvent R10-DS；

Hydrogen supply dissolvent R10-DS, it may be possible to the intermediate production based on heavy oil separation up flow type heat from hydrogenation cracking reaction process R10 The hydrocarbon component or its stabilized hydrogenation the hydrocarbon component contained in gas phase obtained by object；

Hydrogen supply dissolvent R10-DS, it may be possible to be based on heavy oil separation up flow type heat from hydrogenation cracking reaction process R10 end reaction The hydrocarbon component obtained by product R10P or its stabilized hydrogenation the hydrocarbon component；

Hydrogen supply dissolvent R10-DS, it may be possible to the hydrogen supply hydrocarbon generated based on heavy oil up flow type heat from hydrogenation cracking reaction process R10 Component BRA-DSC；

Hydrogen supply dissolvent R10-DS, it may be possible to external hydrogen supply hydrocarbon OUT-TO-R10-DS.

The present invention, in general, (1) heavy oil up flow type heat from hydrogenation cracking reaction process R10, uses at least part hydrogen supply dissolvent R10-DS；

Hydrogen supply dissolvent R10-DS is mainly 250~530 DEG C of hydro carbons by normal boiling point or is that 250~430 DEG C of hydro carbons form, It is 0.35~0.70 that the weight content of middle fractional saturation aromatic hydrocarbons, which is greater than 15%, aromatic carbon rate,.

The present invention, generally, (1) heavy oil up flow type heat from hydrogenation cracking reaction process R10 uses at least part hydrogen supply dissolvent R10-DS；

Hydrogen supply dissolvent R10-DS is mainly 250~530 DEG C of hydro carbons by normal boiling point or is that 250~430 DEG C of hydro carbons form, It is 0.45~0.60 that the weight content of middle fractional saturation aromatic hydrocarbons, which is greater than 25%, aromatic carbon rate,.

The present invention, in general, the raw material R10F of (1) heavy oil up flow type heat from hydrogenation cracking reaction process R10 is mainly by heavy The heavy oil R10F of hydrocarbon HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；

In heavy oil up flow type heat from hydrogenation cracking reaction process R10, the hydrocarbon for being mainly 230~400 DEG C by normal boiling point is used The hydrogen supply hydrocarbon R10-DS of class composition；

The ratio of the weight flow rate heavy oil R10F-W of the weight flow rate R10-DS-W and heavy oil R10F of hydrogen supply hydrocarbon R10-DS is Oil ratio KP80, KP80=(R10-DS-W)/(R10F-W), KP80 are 0.05~2.0.

The present invention, generally, the raw material R10F of (1) heavy oil up flow type heat from hydrogenation cracking reaction process R10 are mainly by heavy The heavy oil R10F of hydrocarbon HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；

The ratio of the weight flow rate heavy oil R10F-W of the weight flow rate R10-DS-W and heavy oil R10F of hydrogen supply hydrocarbon R10-DS is Oil ratio KP80, KP80=(R10-DS-W)/(R10F-W), KP80 are 0.2~0.6.

The present invention, the raw material heavy oil R10F of (1) heavy oil up flow type heat from hydrogenation cracking reaction process R10 are mainly by heavy hydrocarbon The heavy oil R10F of HNBPC composition；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；

It is split in the heavy hydrocarbon HNBPC heat from hydrogenation of heavy oil up flow type heat from hydrogenation cracking reaction process R10, front conversion zone R10A Change reaction conversion ratio, one of the following or several can be selected from:

1. heat from hydrogenation cracking reaction conversion ratio is 5~25%；

2. heat from hydrogenation cracking reaction conversion ratio reaches 25~45% stage of reaction；

3. heat from hydrogenation cracking reaction conversion ratio reaches 45~55% stage of reaction.

In heavy oil up flow type heat from hydrogenation cracking reaction process R10, heavy hydrocarbon HNBPC heat from hydrogenation cracking reaction conversion ratio can Selected from one of the following or several:

1. the 80~98% of overall conversion per pass；

2. raw material heavy oil R10F heavy oil up flow type heat from hydrogenation cracking reaction process R10 overall conversion per pass 60~ 80%；

3. raw material heavy oil R10F heavy oil up flow type heat from hydrogenation cracking reaction process R10 overall conversion per pass 35~ 60%.

It is split in the heavy hydrocarbon HNBPC heat from hydrogenation of heavy oil up flow type heat from hydrogenation cracking reaction process R10, rear portion conversion zone R10B Change reaction conversion ratio, one of the following or several can be selected from:

1. raw material heavy oil R10F heavy oil up flow type heat from hydrogenation cracking reaction process R10 overall conversion per pass 35~ 50%；

2. raw material heavy oil R10F heavy oil up flow type heat from hydrogenation cracking reaction process R10 overall conversion per pass 20~ 35%；

3. raw material heavy oil R10F heavy oil up flow type heat from hydrogenation cracking reaction process R10 overall conversion per pass 5~ 20%.

The present invention, in general, (3), in liquid material recovery section S100L-GU, separation may be containing solid mainly by conventional liquid The liquid material S100L of body hydrocarbon composition obtains mainly being in heat from hydrogenation crackate that 250~450 DEG C of hydrocarbon forms by normal boiling point Distillate THC-MD obtains mainly containing solid by the possibility rich in aromatic hydrocarbons that the hydrocarbon that normal boiling point is 450~570 DEG C forms The heat from hydrogenation cracking wax slop THC-HVGO of grain is obtained that the hydrocarbon mainly by normal boiling point higher than 520 DEG C forms and is contained conventional The heat from hydrogenation cracked vacuum residue THC-VR that rich in colloid, the possibility of asphalitine contains solid particle of the boiling point higher than 570 DEG C；

It is cracked that at least part heat from hydrogenation crackate intermediate distillates THC-MD may be recycled into hydrocarbon material heat from hydrogenation Journey R10 participates in reaction, produces the lower hydro carbons of boiling point；

At least part heat from hydrogenation cracking wax slop THC-HVGO may be used as high aromatic hydrocarbons wax oil KVGO；

A part of heat from hydrogenation cracked vacuum residue THC-VR possibly serves for recycle stock THC-VR-TO-R10 into hydrocarbon material Heat from hydrogenation cracking process R10 participates in reaction；

A part of heat from hydrogenation cracked vacuum residue THC-VR, as discharge colloid, asphalitine and solid that may be present With material THC-VR-TO-OUT；In general, the weight of the hydrocarbon component from hydrocarbon material R10F in material THC-VR-TO-OUT The 2~10% of the weight of the hydrocarbon component lower than hydrocarbon material R10F.

The present invention, a part of heat from hydrogenation cracked vacuum residue THC-VR possibly serve for recycle stock THC-VR-TO-R10 into Enter hydrocarbon material heat from hydrogenation cracking process R10 and participate in reaction, working method can be selected from one of the following or several:

Selection 1, passes through front conversion zone R10A；

Selection 2, by rear portion conversion zone R10B without passing through front conversion zone R10A.

The present invention may include following materials in heavy oil up flow type heat from hydrogenation cracking reaction process R10, raw material heavy oil R10F One or more of:

Logistics containing oil product obtained by selection 1, middle coalite tar or its distillate or its hot procedure；Hot procedure choosing From coking or catalytic cracking process or catalytic pyrolysis process or hydrogenation process；

Logistics containing oil product obtained by selection 2, high temperature coal-tar or its distillate or its hot procedure；

Selection 3, the logistics containing oil product of direct hydrogenation liquefaction of coal liquefaction process gained, the coal hydrogenation including using hydrogen supply dissolvent oil Direct liquefaction liquefaction process, coal refines process to oil altogether, coal faces hydrogen thermosol liquefaction process；

Logistics containing oil product obtained by selection 4, shale oil or its distillate or its hot procedure；

Logistics containing oil product obtained by selection 5, ethylene cracking tar or its distillate or its hot procedure；

Logistics containing oil product obtained by selection 6, petroleum based heavy fuel oils or its hot procedure；

Selection 7, the logistics containing oil product of tar sand base weight oil or its hot procedure gained.

The present invention, in general, (3), in liquid material recovery section S100L-GU, separation may be containing solid mainly by conventional liquid Body hydrocarbon forms the liquid material S100L of liquid phase component, obtains mainly being split by the heat from hydrogenation that the hydrocarbon that normal boiling point is 350~470 DEG C forms Change light wax oil THC-LVGO；

At least part heat from hydrogenation cracking light wax oil THC-LVGO can go catalytic cracking reaction process UNIT600 to participate in Reaction is converted into conventional gas hydrocarbon, conventional liq hydrocarbon and the coke that may be generated.

The present invention, in general, (3), in liquid material recovery section S100L-GU, separation may be containing solid mainly by conventional liquid Body hydrocarbon forms the liquid material S100L of liquid phase component, obtain mainly by normal boiling point be 450~570 DEG C of hydrocarbon form rich in polycyclic The possibility of aromatic hydrocarbons contains the heat from hydrogenation cracking wax slop THC-HVGO of solid particle, obtains mainly being higher than 520 DEG C by normal boiling point Hydrocarbon composition and contain the heat from hydrogenation of solid particle rich in colloid, the possibility of asphalitine higher than 570 DEG C containing normal boiling point Cracked vacuum residue THC-VR；

At least part heat from hydrogenation cracked vacuum residue THC-VR and/or at least part heat from hydrogenation cracking wax slop THC- HVGO can go coking reaction process UNIT800 to participate in reaction and be converted into conventional gas hydrocarbon, conventional liq hydrocarbon, coke；

Pyrogenetic reaction process UNIT800, the possible other feedstock oils of simultaneous processing.

The present invention, the technique that pyrogenetic reaction process UNIT800 is used, can be selected from one of the following or several:

1. delay coking process；

2. fluidized coking process；

3. flexicoking technique.

The present invention, preferably, KVGO is the rich aromatic hydrocarbons wax oil rich in hydrogen supply hydrocarbon.

The present invention, in general, KVGO, it can be selected from one or more of following logistics:

1. logistics containing oil product obtained by middle coalite tar or its distillate or its hot procedure；Hot procedure is selected from coke Change process or catalytic cracking process or catalytic pyrolysis process or hydrogenation process；

2. logistics containing oil product obtained by high temperature coal-tar distillate or its hot procedure；

3. logistics containing oil product obtained by direct hydrogenation liquefaction of coal liquefaction process, including using the coal hydrogenation of hydrogen supply dissolvent oil direct Liquefaction liquefaction process, coal refines process to oil altogether, coal faces hydrogen thermosol liquefaction process；

4. logistics containing oil product obtained by shale oil or its distillate or its hot procedure；

5. logistics containing oil product obtained by ethylene cracking tar or its distillate or its hot procedure；

6. logistics containing oil product obtained by petroleum based heavy fuel oils or its hot procedure；

7. logistics containing oil product obtained by tar sand base weight oil or its hot procedure；

8. other aromatic hydrocarbons weight contents are higher than 40% hydrocarbon ils.

The present invention, in general, rich aromatic hydrocarbons wax oil KVGO, it can be selected from one or more of following materials:

1. the middle matter wax oil of petroleum base viscous crude；

2. the heavy-oil catalytic heavy-cycle oil that heavy oil catalytic cracking reaction product fractionation process obtains；

3. the heavy-oil catalytic clarified oil that heavy oil catalytic cracking reaction product fractionation process obtains；

4. the wax tailings that coking heavy oil reaction product fractional distillation process obtains；

5. the middle matter wax oil that heavy-oil hydrogenation heat cracking reaction product fractionation process obtains；

6. the middle matter wax oil that direct hydrogenation liquefaction of coal reaction product fractional distillation process obtains；

7. kerosene refines the middle matter wax oil that hydrogenation reaction product fractional distillation process obtains altogether.

The present invention, preferably, rich aromatic hydrocarbons wax oil KVGO, mainly by normal boiling point be 450~510 DEG C of the hydrocarbon component form and Solid particle can be contained.

The present invention, in general, (3), in liquid material recovery section S100L-GU, separation may be containing solid mainly by conventional liquid Body hydrocarbon forms the liquid material S100L of liquid phase component, obtains mainly being rich in aromatic hydrocarbons by what the hydrocarbon that normal boiling point is 450~510 DEG C formed Possibility contain matter wax oil THC-MVGO in the heat from hydrogenation cracking of solid particle；

Matter wax oil THC-MVGO is used as rich aromatic hydrocarbons wax oil KVGO in part or all of heat from hydrogenation cracking.

The present invention, in the rear portion conversion zone R10B of heavy oil up flow type heat from hydrogenation cracking reaction process R10, rich aromatic hydrocarbons wax oil The heat from hydrogenation cracking rate of KVGO is usually less than 40%, generally below 20%.

The present invention, mode of operation CASE-A feature are as follows:

Heavy oil up flow type heat from hydrogenation cracking reaction process R10 includes front conversion zone R10A, gas-liquid separation step R10AP- THPS and rear portion conversion zone R10B；

Being separated into separation process R10AP-THPS, front conversion zone product R10AP containing normal boiling point is 220~430 The gas R10AP-THPS-V of DEG C the hydrocarbon component and liquid R10AP- for being higher than 530 DEG C of the hydrocarbon components containing at least part normal boiling point THPS-L, at least part gas R10AP-THPS-V are used as logistics R10AP-THPS-VK and do not enter rear portion conversion zone R10B；? Separation process R10AP-THPS may use hydrogen rich gas gas stripping gas to contact with liquid existing for separation process R10AP-THPS with gas Mention low boiling hydrocarbon；

The hydrocarbonaceous liquid object for being higher than 530 DEG C of the hydrocarbon components containing at least part normal boiling point based on liquid R10AP-THPS-L Material R10AP-THPS-LX enters rear portion conversion zone R10B；

In rear portion hydrogenation reaction section R10B, there are hydrogen, conventional liq hydrocarbon simultaneously there may be hydrogen supply hydrocarbon, there may be Under the conditions of the mixed phase material of solid particle, the hydrocarbonaceous liquid material R10AP-THPS-LX of at least part carries out hydrogenation reaction R10B-R The cracking reaction of at least part heat from hydrogenation occurs and is converted into hydrogenation reaction product R10BP；Rear portion hydrogenation reaction section R10B, Ke Nengtong Shi Jiagong is other to contain residual oil streams；

The rich aromatic hydrocarbons wax for mainly containing solid particle between the possibility that 370~550 DEG C of the hydrocarbon component forms by normal boiling point Oily KVGO, into separation process R10AP-THPS and/or rear portion conversion zone R10B without front conversion zone R10A, rich aromatic hydrocarbons The heat from hydrogenation cracking conversion product of wax oil KVGO enters in heat from hydrogenation cracked reaction product R10BP.

The present invention obtains the ADSC of hydrocarbon containing solvent generally, based on gas R10AP-THPS-VK when mode of operation is CASE-A Material R10AP-THPS-RLK, participate in reacting into hydrogenation process, working method is selected from one of following manner Or it is several:

1. the front conversion zone R10A for entering hydrocarbon material R10F up flow type heat from hydrogenation cracking reaction process R10 participates in reaction；

2. the rear portion conversion zone R10B for entering hydrocarbon material R10F up flow type heat from hydrogenation cracking reaction process R10 participates in reaction.

The present invention obtains the ADSC of hydrocarbon containing solvent generally, based on gas R10AP-THPS-VK when mode of operation is CASE-A Material R10AP-THPS-RLK stabilized hydrogenation process R10AP-THPS-MR product R10AP-THPS-MRP obtain containing supply Hydrogen hydrocarbon stream R10AP-THPS-RLKH, into hydrogenation process participate in react, working method in following manner one Kind is several:

2. the rear portion conversion zone R10B for entering hydrocarbon material R10F up flow type heat from hydrogenation cracking reaction process R10 participates in reaction；

Aromatic moiety, which occurs, in stabilized hydrogenation process R10AP-THPS-MR, material R10AP-THPS-RLK adds hydrogen saturation anti- The higher hydrocarbon stream of hydrogen supply hydrocarbon concentration should be converted into；Stabilized hydrogenation process R10AP-THPS-MR, may receive simultaneously it is other containing The material of hydrogen supply hydrocarbon or the solvent hydrocarbon ADSC of hydrogen supply hydrocarbon precursor.

The present invention, when joint processes poor quality hydrocarbon CRF, in general, poor quality hydrocarbon CRF is mainly to be higher than 570 DEG C by normal boiling point The possibility of the hydrocarbon component composition contains the high carbon residue hydrocarbon of solid particle, and hydrocarbon CRF carbon residue content inferior is higher than in hydrocarbon material R10F with boiling The carbon residue content of journey fraction；

In hydrocarbon CRF up flow type expanded bed hydrogenation modification reaction process CR inferior, simultaneously can there are hydrogen, conventional liq hydrocarbon There can be hydrogen supply hydrocarbon, there may be under the conditions of the mixed phase material of solid particle, at least part poor quality hydrocarbon CRF occurs at least one The removal of ccr by hydrotreating reaction of point colloid, asphalitine is converted into the hydrogenation modification reaction CR-R conversion of low aromatic carbon rate heavy hydrocarbon component KVRC For hydrogenation modification reaction product CRP；

The logistics of conversion product wax oil component comprising inferior hydrocarbon CRF and residue fraction of at least part based on product CRP CRP-X is contacted into heavy oil up flow type heat from hydrogenation cracking reaction process R10 with hydrocarbonaceous liquid material R10F or its hydro-conversion object Hydrogenation reaction is carried out, the heat from hydrogenation cracking conversion product of at least part flow C RP-X enters heat from hydrogenation cracked reaction product R10BP In；

(3) in liquid material recovery section S100L-GU, separation mainly may form liquid phase by conventional liq hydrocarbon containing solid The liquid material S100L of component obtains mainly being contained by what the hydrocarbon that normal boiling point is higher than 530 DEG C formed rich in colloid, the possibility of asphalitine There is the heat from hydrogenation cracked vacuum residue THC-VR of solid particle；

Partial hydrogenation thermal cracking decompression residuum THC-VR, possibly serving for hydrocarbon CRF inferior, to enter hydrocarbon CRF hydrogenation modification inferior anti- Process CR is answered to participate in reaction；

At least part heat from hydrogenation cracked vacuum residue THC-VR-TO-OUT as discharge colloid, asphalitine and may be deposited Solid outlet residual oil THC-VR-TO-OUT discharge system of processing without enter hydroconversion process.

The present invention, when joint processes poor quality hydrocarbon CRF, the first mode of operation is the packet at least partially based on product CRP The flow C RP-X of conversion product wax oil component and residue fraction containing hydrocarbon CRF inferior, into heavy oil up flow type heat from hydrogenation cracking reaction The front conversion zone R10A of process R10 is contacted with hydrocarbonaceous liquid material R10F or its hydro-conversion object and is carried out hydrogenation reaction, and at least one The heat from hydrogenation cracking conversion product of fraction of stream CRP-X enters in heat from hydrogenation cracked reaction product R10BP.

The present invention, when joint processes poor quality hydrocarbon CRF, second of mode of operation is the packet at least partially based on product CRP The flow C RP-X of conversion product wax oil component and residue fraction containing hydrocarbon CRF inferior, into heavy oil up flow type heat from hydrogenation cracking reaction The rear portion conversion zone R10B of process R10 and without front conversion zone R10A, add hydrogen to turn with hydrocarbonaceous liquid material R10AP-LX or its Compound contact carries out hydrogenation reaction, and the heat from hydrogenation cracking conversion product of flow C RP-X enters heat from hydrogenation cracked reaction product R10BP In.

The present invention, when joint processes poor quality hydrocarbon CRF, hydrocarbon CRF inferior can have a kind or several in lower Column Properties:

Option 1, hydrocarbon CRF inferior are mainly to be rich in colloid, asphalitine by what the hydrocarbon component that normal boiling point is higher than 570 DEG C formed Possibility contain the hydrocarbon stream of solid particle, carbon residue content is 20~65 weight %；

Option 2, hydrocarbon CRF inferior are mainly to be rich in colloid, asphalitine by what the hydrocarbon component that normal boiling point is higher than 560 DEG C formed Possibility contain the hydrocarbon stream of solid particle, carbon residue content is 30~45 weight %；

Option 3, hydrocarbon CRF inferior are mainly to be rich in colloid, asphalitine by what the hydrocarbon component that normal boiling point is higher than 550 DEG C formed The high carbon residue hydrocarbon containing solid particle, the weight concentration of solid particle is 0.010 weight of weight %~40.0 %；

Option 4, hydrocarbon CRF inferior are mainly to be rich in colloid, asphalitine by what the hydrocarbon component that normal boiling point is higher than 540 DEG C formed The high carbon residue hydrocarbon containing solid particle, the weight concentration of solid particle is 0.10 weight of weight %~20.0 %；

Option 5, hydrocarbon CRF inferior are mainly to be rich in colloid, asphalitine by what the hydrocarbon component that normal boiling point is higher than 530 DEG C formed The high carbon residue hydrocarbon containing solid particle, the weight concentration of solid particle is 0.10 weight of weight %~15.0 %.

The present invention, when joint processes poor quality hydrocarbon CRF, in general, (3), in liquid material recovery section S100L-GU, separation may contain By the liquid material S100L for being mainly made of liquid phase component conventional liq hydrocarbon of solid, obtain mainly being higher than 500 DEG C by normal boiling point The the first heat from hydrogenation cracked vacuum residue THC-VR1 for containing solid particle rich in colloid, the possibility of asphalitine of hydrocarbon composition, obtains Mainly second plus the hydrogen for containing solid particle rich in colloid, the possibility of asphalitine that the hydrocarbon by normal boiling point higher than 550 DEG C forms Thermal cracking decompression residuum THC-VR2；Hydrocarbon of the normal boiling point lower than 550 DEG C in second heat from hydrogenation cracked vacuum residue THC-VR2 The weight concentration of hydrocarbon of the weight concentration lower than normal boiling point in the first heat from hydrogenation cracked vacuum residue THC-VR1 lower than 550 DEG C；

Part or all of first heat from hydrogenation cracked vacuum residue THC-VR1 enters hydrocarbon CRF inferior as hydrocarbon CRF inferior and adds Hydrogen modified-reaction process CR participates in reaction；

Part the second heat from hydrogenation cracked vacuum residue THC-VR2, possibly serves for hydrocarbon CRF inferior and enters hydrocarbon CRF inferior adding hydrogen Modified-reaction process CR participates in reaction；

Second heat from hydrogenation cracked vacuum residue THC-VR2 at least partially, as discharge colloid, asphalitine, solid it is outer System of processing is discharged without entering hydroconversion process in deslagging oil THC-VR2-TO-OUT.

The present invention, when joint processes poor quality hydrocarbon CRF, in general, (3) are in liquid material recovery section S100L-GU, material THC-VR- The weight of the hydrocarbon component from hydrocarbon material R10F in TO-OUT is the 2~10% of the weight of the hydrocarbon component of hydrocarbon material R10F.

The present invention, when joint processes poor quality hydrocarbon CRF, in general, in hydrocarbon CRF hydrogenation modification reaction process CR inferior, it is existing Solid particle may include a kind or several in following:

1. catalyst solid particle；

2. the particle being mainly made of carbon；

3. sulphur powder；

4. poor quality hydrocarbon CRF hydrogenation modification reaction process CR needs the other solid powders inputted.

The present invention, when joint processes poor quality hydrocarbon CRF, in general, being used in hydrocarbon CRF hydrogenation modification reaction process CR inferior The working method of hydrogenation modification reactor CRUE can a kind or several in following:

1. suspended-bed reactor, that is, paste state bed reactor；

2. fluidized bed reactor；

3. suspension bed and ebullated bed combination type reactor.

Option 2, reactor CRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump Answer the fluidized bed reactor of device CRUE material inlet；

Option 3, reactor CRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump Answer the suspended-bed reactor of device CRUE material inlet；

Option 4, reactor CRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of device CRUE material inlet is answered, while circulating pump conveys circulation fluid, downstream transport liquid material product；

Option 5, reactor CRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of device CRUE material inlet is answered, while circulating pump conveys circulation fluid, downstream transport liquid material product；

Option 6, reactor CRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor for answering device CRUE material inlet, be collected simultaneously cup discharge other collection liquids by other dedicated feeding engines to Downstream conveys liquid material product；

Option 7, reactor CRUE, forced circulation returns anti-after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor for answering device CRUE material inlet, be collected simultaneously cup discharge other collection liquids by other dedicated feeding engines to Downstream conveys liquid material product；

Option 8, reactor CRUE, top are arranged liquid collecting cup and liquid material product are discharged by dedicated feeding engine downstream transport liquid Expect product, is not provided with the fluidized bed reactor system of liquid material product forced circulation；

Option 9, reactor CRUE, top are arranged liquid collecting cup and liquid material product are discharged by dedicated feeding engine downstream transport liquid Expect product, is not provided with the suspended-bed reactor system of liquid material product forced circulation；

Option 10, reactor CRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor CRUE material inlet and the combination type reactor of ebullated bed；

Option 11, reactor CRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor CRUE material inlet and the combination type reactor of ebullated bed, while circulating pump conveys circulation fluid, downwards Trip conveying liquid material product；

Option 12, reactor CRUE, forced circulation returns after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of reactor CRUE material inlet and the combination type reactor of ebullated bed are collected simultaneously other collection liquids warp of cup discharge Cross other dedicated feeding engine downstream transport liquid material products；

Option 15, empty cylinder bubbling bed suspended-bed reactor system；

Option 17, in reactor CRUE, setting enters stripping step and the top of the end gas-liquid product of top liquid collecting cup Liquid collecting cup gas-liquid separation step, the average molecular weight for the balance liquid phase that hydrogen rich gas gas stripping gas is formed after mixing with end gas-liquid product Greater than the average molecular weight of the balance liquid phase of end gas-liquid product, what hydrogen rich gas gas stripping gas was formed after mixing with end gas-liquid product The concentration for the hydrocarbon component that the normal boiling point for balancing liquid phase is higher than 350 DEG C is greater than the normal boiling point of the balance liquid phase of end gas-liquid product The concentration of the hydrocarbon component higher than 350 DEG C；The slurries that liquid collecting cup in the final reactor of autoreaction section is discharged through diversion pipe, as Conversion zone product slurry or circular response liquid phase.

The present invention, when joint processes poor quality hydrocarbon CRF, in general, in hydrocarbon CRF hydrogenation modification reaction process CR inferior, conversion zone Obtaining may be containing the mode of the product liquid of solid, can a kind or several in following manner:

1. the possibility that the gas-liquid separation process of autoreaction section reaction product is discharged contains the liquid of solid, as final reaction The possibility of section contains the product liquid of solid；

2. the final reactor of conversion zone uses pure counter-current reactor, the bottom liquid phase region of the final reactor of autoreaction section The possibility of discharge contains the liquid of solid, and the possibility as conversion zone contains the product liquid of solid；

3. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup warp in the final reactor of autoreaction section The possibility of diversion pipe discharge contains the liquid of solid, and the possibility as conversion zone contains the product liquid of solid；

4. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup warp in the final reactor of autoreaction section The possibility of diversion pipe discharge contains the liquid of solid, and the liquid of solid is contained as possibility to be de-gassed；

The present invention, when joint processes poor quality hydrocarbon CRF, in general, being reacted in hydrocarbon CRF up flow type expanded bed hydrogenation modification inferior The heat from hydrogenation cracking rate of journey CR, hydrocarbon CRF inferior, can a kind or several in following:

1. the heat from hydrogenation cracking rate of hydrocarbon CRF inferior is 3~10%；

2. the heat from hydrogenation cracking rate of hydrocarbon CRF inferior is 10~20%；

3. the heat from hydrogenation cracking rate of hydrocarbon CRF inferior is 20~30%；

In hydrocarbon CRF hydrogenation modification reaction process CR inferior, the heat from hydrogenation cracking rate of hydrocarbon CRF inferior is 30~60%.

The present invention, when joint processes poor quality hydrocarbon CRF, in general, being reacted in hydrocarbon CRF up flow type expanded bed hydrogenation modification inferior The removal of ccr by hydrotreating rate of journey CR, hydrocarbon CRF inferior operates target, can a kind or several in following:

1. the removal of ccr by hydrotreating rate of hydrocarbon CRF inferior is 5~20%；

2. the removal of ccr by hydrotreating rate of hydrocarbon CRF inferior is 20~35%；

3. the removal of ccr by hydrotreating rate of hydrocarbon CRF inferior is 35~60%.

The present invention, when joint processes poor quality hydrocarbon CRF, in general, the operation of up flow type expanded bed hydrogenation modification reaction process CR Mode can a kind or several in following:

1. the operating condition of up flow type expanded bed hydrogenation modification reaction process CR are as follows: reaction temperature is 390~445 DEG C, instead Answering device pressure is 6~30MPa, and vapor phase hydrogen volumetric concentration 50~95%, gas-liquid volume ratio is 100~2000Nm³/m³, hydrogen is added to change Property catalyst CR-CAT additive amount be hydrocarbon CRF inferior weight the 0.001 mass % of mass %~5, co-catalyst additive amount is Sulphur/catalyst activity metal molar ratio is 1.0~2.0 in co-catalyst, and reaction time TRU is 5 minutes~120 points Clock；

Add 2. the hydrogenation catalyst CR-CAT that up flow type expanded bed hydrogenation modification reaction process CR is used is that one kind is compound Hydrogen catalyst includes high-activity component and low activity component；The weight of the high-activity component metal and low activity component metals Than being 1: 10 to 1000: 1；The high-activity component contain molybdenum oil-soluble salt compounds water soluble salt compound or its Mixture；The low activity component contains ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, Catalyst water content is lower than 2wt%；The powdered granule that hydrogenation catalyst particle diameter is 1~100 μm；

3. the hydrogenation catalyst CR-CAT that up flow type expanded bed hydrogenation modification reaction process CR is used includes nanometer ultra-fine Grain aqua oxidation iron catalyst and/or iron oxide and/or pyrite and/or bloodstone and/or molybdenum oxide and/or molybdenum sulfide and/or molybdic acid Ammonium and/or nickel sulfide.

The present invention, when joint processes poor quality hydrocarbon CRF, in general, in hydrocarbon CRF hydrogenation modification reaction process CR inferior, using extremely Few a part of hydrogen supply dissolvent CR-DS；

Hydrogen supply dissolvent CR-DS, it may be possible to based on gas phase obtained by the intermediate product for separating hydrocarbon material heat from hydrogenation cracking process R10 Contained in the hydrocarbon component or its stabilized hydrogenation the hydrocarbon component；

Hydrogen supply dissolvent CR-DS, it may be possible to based on the heat from hydrogenation cracking reaction final product R10P institute for separating hydrocarbon material R10F Obtain the hydrocarbon component or its stabilized hydrogenation the hydrocarbon component；

Hydrogen supply dissolvent CR-DS, it may be possible to based on obtained by the intermediate product for separating hydrocarbon CRF hydrogenation modification reaction process CR inferior The hydrocarbon component contained in gas phase or its stabilized hydrogenation the hydrocarbon component；

Hydrogen supply dissolvent CR-DS, it may be possible to based on the final product CRP for separating hydrocarbon CRF hydrogenation modification reaction process CR inferior Gained the hydrocarbon component or its stabilized hydrogenation the hydrocarbon component；

Hydrogen supply dissolvent CR-DS, it may be possible to the hydrogen supply the hydrocarbon component generated based on hydrocarbon CRF hydrogenation modification reaction process CR inferior CR-DSC；

Hydrogen supply dissolvent BR-DS, it may be possible to external hydrogen supply hydrocarbon OUT-TO-CR-DS.

The ratio of the weight flow rate CRF-W of the weight flow rate CR-DS-W of hydrogen supply dissolvent flow C R-DS and hydrocarbon stream CRF inferior Value is oil ratio BK100=(CR-DS-W)/(CRF-W), and CK100 is usually 0.05~5.0, generally 0.5~1.5.

Hydrogen supply dissolvent flow C R-DS is mainly that 250~530 DEG C of hydro carbons form by normal boiling point, part saturation aromatic hydrocarbons Weight content be greater than 15%, aromatic carbon rate be 0.35~0.70.

The present invention, when joint processes poor quality hydrocarbon CRF, generally, in hydrocarbon CRF hydrogenation modification reaction process CR inferior, using extremely Few a part of hydrogen supply dissolvent CR-DS；

Hydrogen supply dissolvent flow C R-DS is mainly that 250~530 DEG C of hydro carbons form by normal boiling point, part saturation aromatic hydrocarbons Weight content be greater than 25%, aromatic carbon rate be 0.45~0.60.

The present invention, when joint processes poor quality hydrocarbon CRF, in general, CRF is up flow type expanded bed hydrogenation modification reaction process CR's Operate target are as follows: hydrogen consumption is 0.1 mass of mass %~1.5 %, CRF heat from hydrogenation cracking reaction of high aromatic hydrocarbons wax oil BRF weight Conversion ratio is 5~20 mass %；

Operation target of the CRF in the rear portion conversion zone R10B of up flow type expanded bed heat from hydrogenation cracking reaction process R10 are as follows: add Hydrogen heat cracking reaction conversion ratio is 20~50 mass %；

CRF is in up flow type expanded bed hydrogenation modification reaction process CR, up flow type expanded bed heat from hydrogenation cracking reaction process R10 Rear portion conversion zone R10B overall cascade process operation target are as follows: heat from hydrogenation cracking reaction conversion ratio be 25~65 matter Measure %.

The present invention, when joint processes poor quality hydrocarbon CRF, generally, CRF is up flow type expanded bed hydrogenation modification reaction process CR's Operate target are as follows: hydrogen consumption is 0.1 mass of mass %~1.5 %, CRF heat from hydrogenation cracking reaction of high aromatic hydrocarbons wax oil BRF weight Conversion ratio is 5~15 mass %；

Operation target of the CRF in the rear portion conversion zone R10B of up flow type expanded bed heat from hydrogenation cracking reaction process R10 are as follows: add Hydrogen heat cracking reaction conversion ratio is 25~35 mass %；

CRF is in up flow type expanded bed hydrogenation modification reaction process CR, up flow type expanded bed heat from hydrogenation cracking reaction process R10 Rear portion conversion zone R10B overall cascade process operation target are as follows: heat from hydrogenation cracking reaction conversion ratio be 25~50 matter Measure %.

The present invention, when joint processes poor quality hydrocarbon CRF, at least part richness aromatic hydrocarbons wax oil KVGO can be used as rich aromatic hydrocarbons wax oil CR-KVGO enters back into heavy oil up flow type heat from hydrogenation cracking reaction after first passing through up flow type expanded bed hydrogenation modification reaction process CR The rear portion conversion zone R10B of process R10 and without front conversion zone R10A；

In up flow type expanded bed hydrogenation modification reaction process CR, at least part richness aromatic hydrocarbons wax oil KVGO and hydrocarbon CRF inferior Or at least part hydrogenation reaction occurs for the contact of its hydro-conversion object, the hydro-conversion object of rich aromatic hydrocarbons wax oil KVGO enters reaction and produces In object CRP；

Conversion product wax oil component comprising rich aromatic hydrocarbons wax oil CR-KVGO of at least part based on product CRP includes poor quality The conversion product wax oil component of hydrocarbon CRF and the flow C RP-X of residue fraction, into heavy oil up flow type heat from hydrogenation cracking reaction process The rear portion conversion zone R10B of R10 and without front conversion zone R10A, with hydrocarbonaceous liquid material R10AP-LX or its hydro-conversion object Contact carries out hydrogenation reaction, and the heat from hydrogenation cracking conversion product of flow C RP-X enters in heat from hydrogenation cracked reaction product R10BP.

The present invention, when joint processes poor quality hydrocarbon CRF, the rich aromatic hydrocarbons wax oil KVGO of at least part first passes through up flow type expansion The rear portion conversion zone R10B of heavy oil up flow type heat from hydrogenation cracking reaction process R10 is entered back into after bed hydroprocessing modified-reaction process CR and Without front conversion zone R10A, it is usual to operate target are as follows:

Operation target of the rich aromatic hydrocarbons wax oil KVGO in up flow type expanded bed hydrogenation modification reaction process CR are as follows: KVGO heat from hydrogenation Cracking reaction conversion ratio is 5~20 mass %；

Behaviour of the rich aromatic hydrocarbons wax oil KVGO in the rear portion conversion zone R10B of up flow type expanded bed heat from hydrogenation cracking reaction process R10 Make target are as follows: KVGO heat from hydrogenation cracking reaction conversion ratio is 20~50 mass %；

Rich aromatic hydrocarbons wax oil KVGO is in up flow type expanded bed hydrogenation modification reaction process CR, up flow type expanded bed heat from hydrogenation cracking The operation target of the overall cascade process of the rear portion conversion zone R10B of reaction process R10 are as follows: KVGO heat from hydrogenation cracking reaction conversion Rate is 15~50 mass %.

The present invention, when joint processes poor quality hydrocarbon CRF, the rich aromatic hydrocarbons wax oil KVGO of at least part first passes through up flow type expansion The rear portion conversion zone R10B of heavy oil up flow type heat from hydrogenation cracking reaction process R10 is entered back into after bed hydroprocessing modified-reaction process CR and Without front conversion zone R10A, it is general to operate target are as follows:

Operation target of the rich aromatic hydrocarbons wax oil KVGO in up flow type expanded bed hydrogenation modification reaction process CR are as follows: KVGO heat from hydrogenation Cracking reaction conversion ratio is 5~15 mass %；

Behaviour of the rich aromatic hydrocarbons wax oil KVGO in the rear portion conversion zone R10B of up flow type expanded bed heat from hydrogenation cracking reaction process R10 Make target are as follows: KVGO heat from hydrogenation cracking reaction conversion ratio is 15~30 mass %；

Rich aromatic hydrocarbons wax oil KVGO is in up flow type expanded bed hydrogenation modification reaction process CR, up flow type expanded bed heat from hydrogenation cracking The operation target of the overall cascade process of the rear portion conversion zone R10B of reaction process R10 are as follows: KVGO heat from hydrogenation cracking reaction conversion Rate is 20~40 mass %.

The present invention, when joint processes poor quality hydrocarbon CRF, mode of operation when separation process CRP-THPS is set are as follows:

Hydrocarbon CRF inferior is the height that the possibility that the hydrocarbon component mainly by normal boiling point higher than 570 DEG C forms contains solid particle Carbon residue hydrocarbon, hydrocarbon CRF carbon residue content inferior are higher than the carbon residue content in hydrocarbon material R10F with boiling fraction；

Being separated into separation process CRP-THPS, hydrogenation modification reaction product CRP containing normal boiling point is 220~430 DEG C The gas CRP-THPS-V of the hydrocarbon component and liquid CRP-THPS- for being higher than 530 DEG C of the hydrocarbon components containing at least part normal boiling point L, at least part gas CRP-THPS-V are used as flow C RP-THPS-VK and do not enter rear portion conversion zone R10B；In separation process CRP-THPS may use hydrogen rich gas gas stripping gas to contact with liquid existing for separation process CRP-THPS with air lift low boiling hydrocarbon；

The hydrocarbonaceous liquid material for being higher than 350 DEG C of the hydrocarbon components containing at least part normal boiling point based on liquid CRP-THPS-L CRP-THPS-LX enters rear portion conversion zone R10B.

The present invention, can be with when setting separation process CRP-THPS when mode of operation when joint processing poor quality hydrocarbon CRF:

The material CRP-THPS-RLK of the ADSC of hydrocarbon containing solvent is obtained based on gas CRP-THPS-VK, into hydrogenation reaction mistake Journey participates in reaction, and working method is selected from one or more of following manner:

1. entering up flow type expanded bed hydrogenation modification reaction process CR participates in reaction；

2. the front conversion zone R10A into up flow type heat from hydrogenation cracking reaction process R10 participates in reaction；

3. the rear portion conversion zone R10B into up flow type heat from hydrogenation cracking reaction process R10 participates in reaction.

The stabilized hydrogenation process of the material CRP-THPS-RLK of the ADSC of hydrocarbon containing solvent is obtained based on gas CRP-THPS-VK CRP-THPS-RLKH containing hydrogen-containing hydrocarbon stream obtained from the product CRP-THPS-MRP of CRP-THPS-MR, into hydrogenation reaction mistake Journey participates in reaction, and working method is selected from one or more of following manner:

3. the rear portion conversion zone R10B into up flow type heat from hydrogenation cracking reaction process R10 participates in reaction；

In CRP-THPS-MR, it is dense that material CRP-THPS-RLK generation aromatic moiety adds hydrogen saturated reaction to be converted into hydrogen supply hydrocarbon Spend higher hydrocarbon stream；Stabilized hydrogenation process CRP-THPS-MR may be received other containing hydrogen supply hydrocarbon or hydrogen supply hydrocarbon predecessor simultaneously The material of the solvent hydrocarbon ADSC of object.

The present invention when joint processes poor quality hydrocarbon CRF, grasps when the separation process R10AP-THPS that R10AP, CRP are shared is arranged It is as mode:

The logistics of conversion product wax oil component comprising inferior hydrocarbon CRF and residue fraction of at least part based on product CRP CRP-X, into separation process R10AP-THPS, isolate contain normal boiling point based on flow C RP-X at least partially Enter in gas R10AP-THPS-V for the gas of 220~430 DEG C of the hydrocarbon components, is separated at least partially based on flow C RP-X Liquid out enters in liquid R10AP-THPS-L；

The working method of rich aromatic hydrocarbons wax oil KVGO, a kind or several in following:

It is used 1. entering in up flow type expanded bed hydrogenation modification reaction process CR as flow C R-KVGO, with hydrocarbon CRF inferior Or the reaction of at least part heat from hydrogenation occurs for the contact of its hydro-conversion object, the hydro-conversion object of flow C R-KVGO enters plus hydrogen changes In property reaction product CRP；

2. enter separation process R10AP-THPS in, it is understood that there may be at least part be based on richness aromatic hydrocarbons wax oil KVGO and divide What is separated out enters in gas R10AP-THPS-V containing the gas that normal boiling point is 220~430 DEG C of the hydrocarbon components, at least part base Enter in liquid R10AP-THPS-L in the waxy oil liquid that rich aromatic hydrocarbons wax oil KVGO is isolated；

3. into rear portion conversion zone R10B without front conversion zone R10A, also without separation process R10AP- THPS is contacted with hydrocarbonaceous liquid material R10AP-THPS-LX or its hydro-conversion object and is carried out hydrogenation reaction, rich aromatic hydrocarbons wax oil KVGO's Heat from hydrogenation cracking conversion product enters in heat from hydrogenation cracked reaction product R10BP.

The present invention, particularly, (1) heavy oil up flow type heat from hydrogenation cracking reaction process R10, comprising front conversion zone R10A and Rear portion conversion zone R10B；

Heavy oil up flow type heat from hydrogenation cracking reaction process R10, using the reactor of at least 2 serial operations, rich aromatic hydrocarbons wax Oily KVGO enters in last reactor.

The present invention, more particularly, (1) heavy oil up flow type heat from hydrogenation cracking reaction process R10 includes front conversion zone R10A With rear portion conversion zone R10B；

Heavy oil up flow type heat from hydrogenation cracking reaction process R10, using the reactor of at least 2 serial operations, rich aromatic hydrocarbons wax Oily KVGO enters in the second half reaction compartment of last reactor.

Specific embodiment

The present invention described in detail below.

Pressure of the present invention, refers to absolute pressure.

Normal boiling point of the present invention refers to vapour of the substance under an atmospheric pressure, liquid equilibrium temperature.

Routine boiling range of the present invention refers to the normal boiling point range of fraction.

Specific gravity of the present invention, unless stated otherwise, refer to normal pressure, fluid density and normal pressure under the conditions of 15.6 DEG C, The ratio of water density under the conditions of 15.6 DEG C.

The composition or concentration or content or yield value of component of the present invention are unless stated otherwise weight basis Value.

Conventional gas hydrocarbon of the present invention refers under normal condition in gaseous hydro carbons, including methane, ethane, third Alkane, butane.

Conventional liq hydrocarbon of the present invention refers to the hydro carbons being in a liquid state under normal condition, including pentane and its boiling point Higher hydro carbons.

Impurity element of the present invention, refer to non-hydrogen in feedstock oil, non-carbon, nonmetallic ingredient for example oxygen, sulphur, nitrogen, Chlorine etc..

Impurity composition of the present invention refers to hydro-conversion object such as water, ammonia, the vulcanization of non-hydrocarbon component in feedstock oil Hydrogen, hydrogen chloride etc..

Light hydrocarbon of the present invention is naphtha component, refers to that normal boiling point is lower than 200 DEG C of conventional liq hydrocarbon.

Diesel component of the present invention, the normal boiling point of institute's hydrocarbon-containifirst is usually 155~375 DEG C, generally 200~ 350℃。

Wax oil component of the present invention, the normal boiling point of institute's hydrocarbon-containifirst is usually 350~575 DEG C, generally 370~ 530℃。

Heavy oil component of the present invention, the normal boiling point of institute's hydrocarbon-containifirst be typically larger than 350 DEG C, generally higher than 450 DEG C, Particularly greater than 530 DEG C, more particularly greater than 575 DEG C.

Atmospheric resid component of the present invention, usually atmospheric fractional tower tower bottom oil, the normal boiling point of institute's hydrocarbon-containifirst Typically larger than 330 DEG C, generally higher than 350 DEG C, particularly greater than 370 DEG C.

Vacuum Residue Fractions of the present invention, usually vacuum fractionation tower tower bottom oil, the normal boiling point of institute's hydrocarbon-containifirst Typically larger than 450 DEG C, generally higher than 530 DEG C, particularly greater than 575 DEG C.

Middle matter hydrocarbon of the present invention refers to that normal boiling point is 230~400 DEG C of hydro carbons.

Heavy hydrocarbon of the present invention refers to that normal boiling point is higher than 350 DEG C of hydro carbons.

Solvent hydrocarbon ADSC described herein refers to hydrogen supply hydrocarbon or hydrogen supply hydrocarbon precursor, in the up flow type hydrogenation process of heavy oil (hydrogenation modification reaction process, heat from hydrogenation cracking reaction process) serves as hydrogen supply hydrocarbon or hydrogen transmitting hydrocarbon.

Hydrogen supply hydrocarbon described herein refers to that direct hydrogenation liquefaction of coal reaction process, heavy-oil hydrogenation reaction process, kerosene refine altogether In hydrogenation process with hydrogen supply function the hydrocarbon component, hydrogen supply hydrocarbon include the double ring arene of fractional saturation, fractional saturation it is more Cycloaromatics.Hydrogen supply hydrocarbon reduces reaction compartment thermal cracking certainly while discharging reactive hydrogen makes thermal cracking free radical stabilized hydrogenation By the concentration of base, to have the function of inhibiting thermal cracking, the hot tearing rate of heavy hydrocarbon can be reduced, for example, in heavy-oil hydrogenation hot tearing Change the front conversion zone R10A of a large amount of heat cracking reactions of generation of reaction process R10, the sufficient hydrogen supply hydrocarbon of usage quantity has suppression The function of heating condensation coking, has positive influences to production process；And at the rear portion that heat cracking reaction quantity is greatly reduced There is the superfluous hydrogen supply hydrocarbon in part in the hydrogen supply hydrocarbon of equivalent in conversion zone R10B, superfluous hydrogen supply hydrocarbon, which has, to be inhibited heavy hydrocarbon thermal cracking, reduces The negative effect of heavy hydrocarbon hot tearing rate.

Hydrogen supply hydrocarbon precursor described herein refers to that the hydrocarbon component of hydrogen supply agent can be changed into after adding hydrogen or hydrogen supply hydrocarbon loses Conversion product after the hydrogen of part.

Hydrogen described herein transmits hydrocarbon, refers to that direct hydrogenation liquefaction of coal reaction process, heavy-oil hydrogenation reaction process, kerosene are total Refine the hydrocarbon component in hydrogenation process with transmitting hydrogen function, such as polycyclic aromatic hydrocarbon.

The gas-liquid volume ratio or hydrogen to oil volume ratio of hydrogenation process of the present invention, refer to the standard state of hydrogen The ratio of volume flow and the normal pressure of specified oily logistics, 20 DEG C of volume flow.

Hydrogenation reaction space refers to the process fluid flowing space that the hydrogenation reaction occurs, can be empty in reaction Between such as empty barrel reactor area, air lift hydrogen mixed zone, liquid collection cups upper space region, can be the reactor external space such as Space in pipeline, space in valve, space in mixer, space etc. in pump.

Polycyclic aromatic hydrocarbon mentioned herein, aromatic ring number >=3.

Up flow type hydrogenator of the present invention, reaction compartment or the processing medium in hydrogenation catalyst bed Macroscopic view flowing dominant direction is from top to bottom.

Up flow type expanded bed reactor of the present invention is vertical up-flow reactor, expansion is belonged to when using catalyst Bed reactor；The vertical central axis upright for referring to working condition reactor after installing is in ground；Up flow type refers to reacting Process materials main body flow direction travels through reaction compartment or catalyst bed or the catalyst co-flow with uplink from bottom to top； Expanded bed refers to that working condition catalyst bed is in swelling state, and catalyst bed expansion ratio, which is defined as catalyst bed, to be had The height CUH of the empty bed static condition of the maximum height CWH and catalyst bed of working condition when reaction raw materials pass through it Ratio K BED, in general, referred to as slight expanded-bed when KBED is lower than 1.10, referred to as ebullated bed when KBED is between 1.25~1.55, and hang Floating bed is considered as the expanded bed of most extreme form.

Back-mixing stream expanded bed reactor of the present invention refers to reaction zone or main reaction region using expanded bed reactor Mode of operation there are liquid stream back-mixings there is circulation fluid in other words；Back-mixing stream or circulation fluid refer to the intermediate production at flow points K Upstream reaction of at least part liquid phase XK-L as circulating fluid XK-LR Returning process point K in object XK or final product XK Area, the reaction product of circulating fluid XK-LR flow through K point and are present among XK.The mode for forming back-mixing stream can be any conjunction Built-in inner ring flow cartridge, built-in outer ring flow cartridge, built-in liquid collecting cup+diversion pipe+circulating pump, external is such as arranged in suitable mode Formula circulation pipe etc..

Liquid product recycle up flow type expanded bed hydrogenator system of the present invention, refers to reacting using expanded bed The reaction zone of device or the mode of operation of main reaction region return to the processing of upstream reaction space cycle there are product liquid and exist in other words Liquid product recycle；Liquid product recycle in hydrogenator refers to intermediate product XK or final product at flow points K At least part liquid phase XK-L in XK as the upstream reaction zone circulating fluid XK-LR return logistics XK, circulating fluid XK-LR's Reaction product flows through K point and is present among XK.The mode for forming Liquid product recycle can be any appropriate mode, still Gas-liquid separation zone must be set in the headspace in reactor, obtain circulation fluid and other products, that is, built-in liquid collecting is set Cup+diversion pipe+circularly-supercharged device, circularly-supercharged device are generally circulated pump, can be arranged in inside reactor or outside.

The liquid collecting cup or liquid trap being arranged in reactor of the present invention, refer to being arranged in reactor for collecting The container of liquid, usual top or upper side opening, bottom or lower side installation diversion pipe are for conveying or being discharged collection Liquid；The top liquid trap of expanded bed reactor is typically mounted on the de- liquid zone of gas-liquid material, obtains the liquid containing a small amount of bubble With gas-liquid mixed phase logistics or obtain liquids and gases, at least partly liquid product returns to reaction compartment after circulating pump pressurizes and follows Ring processing.Typical example is that heavy oil boiling bed hydrogenation reactor, the HTI direct hydrogenation liquefaction of coal that H-OIL technique uses react Device.

Hot high score device of the present invention, refers to the gas-liquid separation for separating hydrogenation reaction intermediate product or final product Equipment.

Second level of the present invention or multistage method of hydrotreating refer to comprising two order of reactions or multiple order of reactions plus hydrogen side Method.

A hydrogenation reaction grade of the present invention refers to adding entering a hydrogenation process since hydrocarbon raw material to it Hydrogen product gas-liquid separation obtains at least one process section until generating the liquid product that oil forms by least part, comprising being somebody's turn to do The gas-liquid separation process of at least part hydrogenation reaction product of the hydrogenation process and this grade of hydrogenation reaction grade.Therefore, one Grade method of hydrotreating refers to that the process of initial hydrocarbon feedstock only includes that a hydrogenation reaction step and the hydrogenation reaction step produce The flow model of object gas-liquid separation process, a hydrogenation reaction step can be used 1 or 2 or more as needed The hydrogenator of platform serial operation, therefore number of reactors and form are not the foundation for determining order of reaction, one or some strings Connection reactor group at reaction step and its product separator common combination could form one complete meaning on hydrogenation reaction Grade.

Secondary hydrogenation method of the present invention refers to that the process of initial hydrocarbon feedstock includes liquid material processing flow For " by the gas-liquid separation process of two different hydrogenation reaction steps and corresponding hydrogenation reaction step products " group of serial operation At flow model, the logistics of wherein at least a part of level-one hydrogenated oil composition enters secondary hydrogenation reaction process.

Three-level method of hydrotreating of the present invention refers to that the process of initial hydrocarbon feedstock includes liquid material processing flow For " by the gas-liquid separation process of three different hydrogenation reaction steps and corresponding hydrogenation reaction step products " group of serial operation At flow model, the logistics of wherein at least a part of level-one hydrogenated oil composition enters secondary hydrogenation reaction process, at least The logistics that a part of secondary hydrogenation generates oil composition enters three-level hydrogenation process.The process knot of the method for hydrotreating of more series Structure is analogized according to mentioned above principle.Multistage method of hydrotreating refers to that the process of initial hydrocarbon feedstock includes liquid material processing flow For the process of serial operation formed " by three or more different hydrogenation processes and hydrogenation products gas-liquid separation process " Mode.

Three-level method of hydrotreating, it is serial operation that the process for referring to initial hydrocarbon feedstock, which includes liquid material processing flow, The process formed " by the gas-liquid separation process by three different hydrogenation reaction steps and corresponding hydrogenation reaction step products " Mode, according to this definition, it is evident that the gas-liquid separation process of the hydrogenation products not at the same level can be carried out independently, can also portion Divide or all joint carries out.

It is of the present invention like secondary hydrogenation method, the method for referring to being similar to secondary hydrogenation method, when rear class upper feeding When liquid phase flow ratio tends to infinity in the back-mixing liquid phase flow and upper feeding of back-mixing stream expanded bed reactor, it is considered as second level and adds Hydrogen methods.

Up flow type heat from hydrogenation cracking reaction process R10, the reaction product BASE-R10P of heavy oil R10F of the present invention, At least gas-liquid two-phase logistics, most cases belong to gas, liquid, solid three-phase logistics.Hydrogenation reaction effluent R10P of the present invention For hydrogenation reaction product BASE-R10P to be discharged, occur in the form of 1 tunnel or 2 tunnels or multichannel material, is gas phase or liquid phase or gas Liquid mixed phase or gas-liquid-solid three-phase logistics.

Each section of the invention described in detail below.

Hydrogen supply hydrocarbon (or hydrogen supply the hydrocarbon component) DS is described below, hydrogen supply hydrocarbon precursor DS-BF, hydrogen supply dissolvent SHS, loses hydrogen hydrogen supply Solvent (or hydrogen supply hydrocarbon precursor or hydrogen supply hydrocarbon to be brought back to life) MFS and the stabilized hydrogenation for lose hydrogen hydrogen supply dissolvent MFS resurrection process Reaction process MR.

Hydrogen supply the hydrocarbon component DS described herein refers to facing (including the heavy-oil hydrogenation hot tearing of hydrogen hot-working reaction process in heavy oil Change reaction process), direct hydrogenation liquefaction of coal reaction process, kerosene refine hydrocarbon group in hydrogenation process with hydrogen supply function altogether Point, hydrogen supply hydrocarbon include the double ring arene of fractional saturation, fractional saturation polycyclic aromatic hydrocarbon (usually with tricyclic structure hydrocarbon, tetracyclic structure Hydrocarbon is advisable).In hydrogen supply hydrocarbon, the hydrogen supply speed of dihydro body is all larger than tetrahydro body, and the two of the dihydro body of thrcylic aromatic hydrocarbon and double ring arene Hydrogen body is compared, and it is low that hydrogen supply speed has height to have；Although test is it has been proved that polycyclic aromatic hydrocarbon has transmitting hydrogen without hydrogen supply capacity Ability.At 400 DEG C, the opposite hydrogen supply speed of following component is as follows:

For the hydrogen supply dissolvent SHS industrially used, usually contain hydrogen supply the hydrocarbon component DS and/or hydrogen supply hydrocarbon predecessor The hydrocarbon mixture of object the hydrocarbon component DS-BF, the common source hydrogen supply dissolvent SHS have:

1. the hydrocarbon-fraction that the normal boiling point of coalite tar is 220~480 DEG C；

2. the hydrocarbon-fraction that the normal boiling point of medium temperature coal tar is 220~480 DEG C；

3. the hydrocarbon-fraction that the normal boiling point of high temperature coal-tar is 220~480 DEG C；

4. the hydrocarbon-fraction that the normal boiling point of pulverized coal pyrolysis tar is 220~480 DEG C；

5. 220~480 DEG C of hydrocarbon-fraction of ethylene bottom oil；

6. 220~480 DEG C of hydrocarbon-fraction obtained by petroleum based heavy fuel oils hot procedure, hot procedure is heavy oil catalytic cracking Process or heavy oil catalytic pyrolysis process；

7. 220~480 DEG C of hydrocarbon-fraction obtained by direct hydrogenation liquefaction of coal reaction process；

8. the hydrocarbon-fraction that normal boiling point is 450~570 DEG C；

9. other hydrocarbon mixtures rich in hydrogen supply the hydrocarbon component DS and/or hydrogen supply hydrocarbon precursor the hydrocarbon component DS-BF.

By taking heavy-oil hydrogenation heat cracking reaction process as an example, in hydrocarbon hydrogen heat cracking reaction process, thermal cracking of hydrocarbons from The stabilized hydrogenation process of reactive hydrogen is obtained by base, thermal cracking of hydrocarbons free radical belongs to hydrogen-abstracting agent, while the confession that hydrogen supply capacity is excellent Hydrogen the hydrocarbon component releases active hydrogen atom (referred to as mistake hydrogen) becomes the worse hydro carbons of the higher hydrogen supply capacity of aromatic carbon rate afterwards；Due to supplying Hydrogen hydrocarbon composition is special, and price is higher, outer in order to reduce for needing there are the occasion of a large amount of hydrogen supply hydrocarbon in order to reduce cost For the consumption of hydrogen supply hydrocarbon, it usually needs the hydrogen hydrogen supply hydrocarbon of recycling mistake in a certain way (or hydrogen supply hydrocarbon precursor or hydrogen supply to be brought back to life Hydrocarbon) DS-BF obtains losing hydrogen hydrogen supply dissolvent MFS, and restores the hydrogen supply of mistake hydrogen hydrogen supply dissolvent MFS by stabilized hydrogenation reaction process MR Then ability is recycled；It is obvious that usually lose hydrogen hydrogen supply dissolvent MFS be also hydrocarbon mixture, and would generally by with heavy-oil hydrogenation The same boiling product of process mixes, in this way if the same boiling product of heavy-oil hydrogenation process belongs to hydrogen supply the hydrocarbon component DS and/or hydrogen supply Hydrocarbon precursor the hydrocarbon component DS-BF can then can increase hydrogen supply dissolvent quantity, in this way if the same boiling product of heavy-oil hydrogenation process not The concentration of hydrogen supply hydrocarbon in hydrogen supply dissolvent can then be reduced by belonging to hydrogen supply the hydrocarbon component DS and/or hydrogen supply hydrocarbon precursor the hydrocarbon component DS-BF, right In there are the stable production systems that hydrogen supply dissolvent recycles, the basicly stable recycle stock of the hydrocarbon component will form.

Since hydrogen supply dissolvent can face in heavy oil, hydrogen hot-working aromatic hydrogenation saturated reaction process, that heavy oil faces hydrogen thermal cracking is anti- It answers process quickly to provide reactive hydrogen, quickly transmit reactive hydrogen and (for example pass out the reactive hydrogen of catalyst surface quickly to improve The utilization rate that catalyst generates active hydrogen efficiency, improves reactive hydrogen), therefore, in the cyclic process of a hydrogen supply dissolvent, if energy The enough work for crossing hydrogen supply the hydrocarbon component DS transmitting more with reasonable flow model (for example passing through more hydrocarbons hydrogenation reaction process) Property hydrogen, then can be improved the service efficiency of reactive hydrogen, to form the effective use method of reactive hydrogen, the present invention also utilizes this Kind theory.

Hydrogen supply the hydrocarbon component DS is mainly shown as in the beneficial effect of hydrocarbon hydrogen heat cracking reaction process:

1. under suitable conditions, being converted into the process for losing hydrogen solvent, molecular level is dispersed in entire reaction compartment, Reactive hydrogen is quickly provided to the free radical in liquid phase reactor space, there is hydrogen supply capacity, have the function of hydrogen supply agent, coking inhibitor, This is the distribution consistency degree that the smallest nm-class catalyst of current granularity also cannot achieve；

2. all processes for providing reactive hydrogen to hydro carbons belong to hydrogen migration between hydrocarbon molecule, reaction heat is not generated substantially, is had There is the function of reducing target hydrocarbon ils hydrogenation process reaction heat；

3. thermal cracking of hydrocarbons reaction temperature can be reduced, has the function of dynamics coking inhibitor；

4. the understanding energy of molecular hydrogen can be reduced, accelerate the rate of dissociation of molecular hydrogen；

5. quickly transmitting reactive hydrogen (for example quickly passes out the reactive hydrogen of catalyst surface and generates work to improve catalyst Property hydrogen efficiency, improve reactive hydrogen utilization rate)；

6., can be with multiple conversions " hydrogen supply hydrocarbon, hydrogen supply hydrocarbon precursor " under suitable conditions, under hydrogenation catalyst effect State, repeatedly plays the role of reactive hydrogen delivery agent, and the present invention also utilizes this feature.

1. heat cracking reaction can be induced, heat cracking reaction temperature is reduced, thermal condensation reacting dose is reduced, to improve operation Stability extends the operation cycle；

2. the reaction process time can be shortened, thermal condensation reacting dose is reduced, to improve operational stability, extend operation week Phase；

3. reaction overall temperature rise can be reduced；

4. the retention rate of pyrolysis molecule can be improved while reducing thermal condensation object such as coke yield, i.e. raising light-end products produce Rate is saved to be separated by solid-liquid separation and be consumed energy；

5. operational stability can be improved, extend the operation cycle；, improve catalyst efficiency

6. the overall thermal cracking conversion ratio of heavy oil can be improved.

The hydroconversion reaction zone MR described in detail below that target is prepared as with hydrogen supply hydrocarbon.

According to the present invention, the logistics SHS containing hydrogen supply hydrocarbon SH of recycling is from rich in double ring arene and/or polycyclic The hydrogen supply hydrocarbon precursor logistics SHSBF of aromatic hydrocarbons hydrogenation reaction obtained by the hydroconversion reaction zone MR conversion for being prepared as target with hydrogen supply hydrocarbon The logistics of effluent MRP；It is prepared as the hydroconversion reaction zone MR of target with hydrogen supply hydrocarbon, can work under conditions of any be suitble to.

Stabilized hydrogenation reaction process MR, can using beaded catalyst bed (down-flow fixed bed, it is upflow fixed bed, Up flow type slight expanded-bed) reactive mode, usually temperature is 280~440 DEG C, pressure is 6.0~20.0MPa, hydrogenation catalyst MR-CAT volume space velocity is 0.05~10.0hr^-1, hydrogen/feedstock oil volume ratio be 300: 1~3000: 1 reaction condition under grasp Make.

Stabilized hydrogenation reaction process MR, can be using the moving bed or boiling bed hydrogenation reaction side for using beaded catalyst Formula, usually temperature is 280~440 DEG C, pressure is 6.0~20.0MPa, hydrogenation catalyst MR-CAT volume space velocity be 0.05~ 10.0hr^-1, hydrogen/feedstock oil volume ratio be 100: 1~1200: 1 reaction condition under operate.

Stabilized hydrogenation reaction process MR, it might even be possible to use floating bed hydrogenation reactive mode, usually temperature be 280~ 440 DEG C, pressure be 6.0~20.0MPa, addition hydrogenation catalyst be preferably that the oil-soluble catalyst of high degree of dispersion or water solubility are urged It is operated under the reaction condition that agent, hydrogen/feedstock oil volume ratio are 100: 1~1200: 1.

The aromatic hydrogenation fractional saturation that the hydroconversion reaction zone MR of the present invention for being prepared as target with hydrogen supply hydrocarbon occurs is anti- It answers, refers to existing in hydrogen and suitable hydrogenation catalyst MR-CAT (catalyst with aromatic hydrogenation fractional saturation function) Under the conditions of the reaction process of consumption hydrogen that occurs of the hydrocarbon material SHSBF rich in double ring arene and/or polycyclic aromatic hydrocarbon, minimum reaction Depth should have the industrial significance of bottom line: complete to the hydrocarbon material SHSBF rich in double ring arene and/or polycyclic aromatic hydrocarbon pre- The aromatic hydrogenation fractional saturation of phase, the hydrogenation reaction depth should be according to aromatic component structure in SHSBF and expected aromatic moieties Degree of saturation determines, hydrogen supply hydrocarbon weight in the hydrocarbon-fraction that the normal boiling point in hydrogenation reaction effluent MRP is 350~480 DEG C The higher the better for concentration value SHN expectation, and SHN is the same as often greater than greater than 6 weight %, generally higher than 10 weight %.

The hydroconversion reaction zone MR that target is prepared as with hydrogen supply hydrocarbon, because (tenor, oxygen content contain feedstock property Amount, olefin(e) centent, sulfur content, nitrogen content, arene content, boiling range, specific gravity) difference and hydrogenation reaction (hydrogenation deoxidation plus hydrogen are de- Sulphur, hydrodenitrogeneration, plus hydrogen partial saturation) depth difference, the variation range of operating condition is very wide, should be according to specific process Condition determines.

For beaded catalyst bed (down-flow fixed bed, upflow fixed bed, up flow type slight expanded-bed) reactive mode, The hydroconversion reaction zone MR that target is prepared as with hydrogen supply hydrocarbon, the hydrogenation catalyst MR-CAT used can be it is one or two kinds of or It the tandem compound of a variety of Hydrobon catalysts and loads in mixture, can be the special-purpose catalyst for specific raw material, be also possible to close What the unifining process of suitable petroleum refining heavy diesel fuel type or wax oil type used has hydrodemetallization or hydrogenation deoxidation or adds Hydrogen desulfurization or hydrodenitrogeneration add the Hydrobon catalysts of functions and combinations thereof such as hydrogen saturation.Coal liquefaction crude oil produces coal liquefaction Aromatic hydrogenation fractional saturation reaction process catalyst, the coal tar light fraction deep hydrofinishing catalyst of solvent naphtha be usually It can be used.

The hydroconversion reaction zone MR that target is prepared as with hydrogen supply hydrocarbon, the hydrogenation catalyst MR-CAT used are included at least Hydrocatalyst for saturating arylhydrocarbon, usually also comprising Hydrodemetalation catalyst, (workflow position is likely located at aromatic hydrogenation saturation and urges Before agent bed).

Any supplement sulphur can be added to the hydroconversion reaction zone MR that target is prepared as with hydrogen supply hydrocarbon as needed, to guarantee Reactive moieties necessary minimum concentration of hydrogen sulfide such as 500PPm (v) or 1000PPm (v), to guarantee the necessary vulcanization of catalyst Hydrogen partial pressure is not less than minimum must value.The supplement sulphur can be sulfide hydrogen or can be converted into hydrogen sulfide to adding hydrogen Material of the conversion process without ill-effect, such as hydrogen sulfide containing gas or oil product, or vulcanization is generated after contacting with high-temperature hydrogen The carbon disulfide of hydrogen or dimethyl disulfide etc..

Hydrogen supply dissolvent is used in the up flow type hydrogenation process of heavy oil, free radical can be quickly eliminated, can be improved hot tearing Change product hydrogen content, but also therefore heat cracking reaction can be inhibited to reduce thermal cracking conversion ratio；And the up flow type of heavy oil adds hydrogen The raising of the residual oil quality of reaction process allows its further heat from hydrogenation cracking (such as circulation heat from hydrogenation cracking) total to improve Body heat cracking conversion rate.With regard to the thermal cracking again of thermal cracking tail oil of thermal cracking of heavy oil and heavy oil general effect and Speech, can effectively improve overall heat from hydrogenation cracking conversion rate using hydrogen supply dissolvent, is effectively reduced and gets rid of the yield containing solid tail oil outside, from And improve the economy of process.

Reaction of the richness aromatic hydrocarbons wax oil KVGO described in detail below during heat from hydrogenation cracking reaction tends to.

From the point of view of component characteristic, richness aromatic hydrocarbons wax oil KVGO of the present invention, is that heat from hydrogenation cracking reaction difficulty is inferior to Decompression residuum, the hydrocarbon component for depressurizing heavy wax oil；Residual oil, heavy-oil hydrogenation hot cracked product for heavy-oil hydrogenation hot cracked product Wax slop for, although the middle matter wax oil of heavy-oil hydrogenation hot cracked product is the fraction of arene rich, but its colloid, pitch Matter content is much lower, have lower carbon residue, thermal condensation sensibility, during heat from hydrogenation cracking reaction, hydrogenation reaction with Thermal condensation reaction exists parallel, but is leading with hydrogenation reaction.

From the point of view of component characteristic, the wax slop of heavy-oil hydrogenation hot cracked product, be heat from hydrogenation cracking reaction difficulty only The hydrocarbon-fraction of enrichment polycyclic aromatic hydrocarbon inferior to heat from hydrogenation crackate decompression residuum THC-VR, carbon residue with higher, pyrocondensation More thermal condensation objects can be generated in heavy-oil hydrogenation heat cracking reaction process iterative cycles by closing sensibility；It is anti-in heat from hydrogenation cracking During answering, hydrogenation reaction reacts presence parallel with thermal condensation, i.e., there is parallel to add hydrogen lighting reaction and dehydrogenative condensation Heaviness reaction, both the Direction of Reaction are:

1. plus hydrogen lighting reaction i.e. inhibit coking reaction, direction be " condensed-nuclei aromatics → polycyclic aromatic hydrocarbon → fractional saturation Multiring structure aromatic hydrocarbons → higher hydro carbons of hydrogen content "；

2. dehydrogenation reaction, that is, coking reaction, direction are " coke ← Carbonaceous mesophase ← asphalitine component ← colloid ← condensed ring Aromatic hydrocarbons ← polycyclic aromatic hydrocarbon ".

Hydrocarbon CRF up flow type hydrogenation modification reaction process CR inferior of the invention described in detail below, hydrocarbon CRF inferior can be Heavy-oil hydrogenation hot cracked product decompression residuum THC-VR.

Poor quality hydrocarbon CRF of the present invention, usually heavy hydrocarbon inferior, common to be meant that: not use hydrogen supply dissolvent condition Under, in other operating conditions (reaction pressure, reaction temperature, catalyst composition and additive amount and amount, residence time, hydrogen oil Volume ratio, way of operation) under the same conditions, coking tendency of the hydrocarbon CRF inferior during heat from hydrogenation cracking reaction, Fraction more identical than boiling range in heavy oil R10F during heat from hydrogenation cracking reaction coking tendency it is more serious, i.e., coking yield it is higher and Or heat from hydrogenation cracking conversion rate is lower；In general, the carbon residue that the normal boiling point in hydrocarbon CRF inferior is higher than 530 DEG C of hydro carbons compares heavy oil The carbon residue that normal boiling point in R10F is higher than 530 DEG C of hydro carbons is higher.

The up flow type hydrogenation modification reaction process CR of poor quality hydrocarbon CRF of the present invention, main target are added with conventional Hydrogen heat cracking reaction process is compared, under catalyst and hydrogen supply dissolvent existence condition that may be present, make hydrocarbon CRF inferior occur compared with More plus hydrogen saturated reaction and the reaction of sufficient thermal cracking free radical stabilized hydrogenation, so that the carbon residue of hydrocarbon CRF inferior be effectively reduced Value makes hydro carbons of the normal boiling point therein higher than 530 DEG C become the heat from hydrogenation cracking reaction process of appropriate heat from hydrogenation cracking severity Raw material.

In group technology of the invention, the up flow type hydrogenation modification reaction process CR's of poor quality hydrocarbon CRF of the present invention First reaction task be carry out heavy hydrocarbon inferior removal of ccr by hydrotreating reaction i.e. heavy arene or colloid, asphalitine plus hydrogen saturation instead It answers, certainly, while hydrofining reaction (including demetalization plus hydrogen hydrogenolysis, olefins hydrogenation reaction plus hydrogen can occur Removing impurities matter (oxygen, sulphur, nitrogen) reaction plus hydrogen aromatic hydrocarbons saturation or fractional saturation reaction, removal of ccr by hydrotreating reaction) and/or be hydrocracked anti- It answers.The typical feedstock of the up flow type hydrogenation modification reaction process CR of hydrocarbon CRF inferior is exactly that the up flow type heat from hydrogenation of heavy oil R10F is split Change the product residual oil in reaction process R10, in general, in the tower bottom residual oil that it is enriched in vacuum fractionation tower in product fractionation process, This residual oil THC-VR usually contains catalyst conversion product such as molybdenum sulfide of addition etc., the R10 product metal from heavy oil R10FL Sulfide, the coke that may be accumulated.

When hydrocarbon CRF inferior includes in the up flow type heat from hydrogenation cracking reaction process R10 product R10P from heavy oil R10F When normal boiling point is higher than 530 DEG C of hydro carbons R10-VR, the carbon residue content of part heavy oil R10-VR is usually above in raw material R10F The carbon residue content of the identical fraction of boiling range, the liquid phase in hydrocarbon material up flow type heat from hydrogenation cracking reaction process R10 is suitable in other words The colloid of heat from hydrogenation cracking reaction process as hydrocarbon CRF inferior, asphalitine, liquid phase coke dispersion solution, therefore, the present invention The up flow type that heavy hydrocarbon in the up flow type hydrogenation modification reaction process CR reaction product of hydrocarbon CRF inferior introduces heavy oil R10F is added into hydrogen The second half section of heat cracking reaction process R10 carries out appropriate heat from hydrogenation cracking reaction, can control the heat of hydro carbons poor quality hydrocarbon CRF simultaneously Cracking level, the yield for preventing excessively high hot tearing rate from leading to thermal condensation object such as asphalitine are more than limitation and lead to second liquid phase The generation of (pitch phase).

In the up flow type hydrogenation modification reaction process CR of hydrocarbon CRF inferior, when reactive hydrogen is supplied not in time, colloid, Condensation reaction will occur for the thermal cracking free radical of asphalitine, and production molecular weight bigger molecule or structure group repeatedly take off Hydrogen and the final result of condensation reaction are to generate coke, and certainly, this is the negative reaction for needing inhibition or reduction.

The reactor types of the up flow type hydrogenation modification reaction process CR of poor quality hydrocarbon CRF of the present invention, can be any Suitable form can be one in the combination cot reactor of fluidized bed reactor, suspended-bed reactor, ebullated bed and suspension bed Kind or several combinations.

The up flow type hydrogenation modification reaction process CR of poor quality hydrocarbon CRF of the present invention, the reactor used can be 1 or 2 or more, reactor working method can be any suitable form, and usually up flow type expanded bed reactor or carrying liqs produce The up flow type expanded bed reactor of object circulation, the W-response area of separate unit up flow type expanded bed reactor may be considered that division For 2 or multiple reaction zones.The control mode of the inlet temperature of any reaction zone of up flow type expanded bed reactor of the present invention, can To be the temperature and/or flow for adjusting hydrogen, the temperature and/or flow for adjusting oil product can be.

The up flow type hydrogenation modification reaction process CR of hydrocarbon CRF inferior, the reactor used, liquid phase, gas in reaction compartment The volume ratio of phase (or vapour phase), can be with liquid phase be it is main the case where, define reaction compartment in " liquid phase actual volume/(liquid Phase actual volume+gas phase actual volume) " be reaction compartment liquid phase fraction KL, a point rate KL is typically larger than 0.5, generally higher than 0.65, Even greater than 0.80, actual reinforcing liquid-phase hydrogenatin mode is formed, it, may in order to keep reaction compartment hydrogen partial pressure sufficiently high It needs the position of the different height of reactor 2 times or repeatedly to add hydrogen.

It, can be former by a part of liquid in order to adjust reaction feed property, or in order to control reaction process property of liquid phase Expect that R10F introduces the up flow type hydrogenation modification reaction process CR of hydrocarbon CRF inferior.

It, can be by the upper of heavy oil R10F in order to adjust reaction feed property, or in order to control reaction process property of liquid phase A part of product liquid or final liquid of the intermediate liquid product such as front conversion zone of streaming heat from hydrogenation cracking reaction process R10 A part of product liquid of body product such as rear portion conversion zone, is introduced directly into the up flow type of hydrocarbon CRF inferior under high-temperature high-pressure state Hydrogenation modification reaction process CR.

The residue fraction in up flow type heat from hydrogenation cracked reaction product R10P in order to shorten heavy oil R10F enters hydrocarbon inferior The path of the up flow type hydrogenation modification reaction process CR of CRF, when the distillate (normal boiling point that the liquid phase of reaction product R10P contains Hydro carbons lower than 530 DEG C) be rich in hydrogen supply agent or precursor of hydrogen donor when, directly the liquid phase of part reaction product R10P can be drawn The up flow type hydrogenation modification reaction process CR for entering hydrocarbon CRF inferior, at this point, foring the short circulation loop of tail oil high pressure；When reaction produces The distillate (normal boiling point is lower than 530 DEG C of hydro carbons) that the liquid phase of object R10P contains only contains a small amount of hydrogen supply agent or hydrogen supply agent predecessor When object, it usually needs obtain the miscella of residual oil or residual oil and wax slop in the oily separation and recovery system of the generation of reaction product R10P Up flow type hydrogenation modification reaction process CR is introduced as heavy hydrocarbon inferior, at this point, foring conventional tail oil long circulating circuit.

Hydrogen supply in the up flow type hydrogenation process CR reaction product CRP of hydrocarbon CRF inferior of the invention described in detail below The whereabouts of solvent composition, heavy oil component, working method can be any suitable form, and the present invention lists some common schemes. The crucial purpose of of the invention one is as needed, to reuse hydrogen supply dissolvent component in reaction product CRP and (be recycled, string Connection is recycled), the heavy oil component in reaction product CRP can be made in the up flow type heat from hydrogenation cracking reaction process of heavy oil R10F R10 (rear portion conversion zone) carries out Unionfining thermal cracking.

The up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F of the invention described in detail below.

The heavy-oil hydrogenation that the up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F of the present invention can be carried out is described below Heat cracking reaction process.

The hydro carbons of the raw material heavy oil R10FL of the up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F of the present invention 470 DEG C of the usual > of normal boiling point, 500 DEG C of general >, particularly 530 DEG C of >；The up flow type of heavy oil R10F of the present invention adds Heat cracking reaction, the thermal cracking free radical stabilized hydrogenation of at least part heavy oil R10FL occur for hydrogen heat cracking reaction process R10 Reaction generates the lower hydrocarbon product of at least part boiling point；Heavy oil up flow type heat from hydrogenation cracking reaction process R10, usual nothing Method realizes that one way reacts whole lightings, i.e., its usual rationally high thermal cracking depth is usually 70~85% conversion per pass Rate, there are the tail oils of certain amount such as 15~30% in such heat from hydrogenation cracked reaction product R10P, and in order to reduce outlet Tail oil quantity, it is often necessary to the heat from hydrogenation cracking reaction process of tail oil is set, and in order to simplify overall procedure, reduce investment and energy Consumption, usually forms the heat from hydrogenation cracking reaction process of tail oil and the up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F Group technology.

Although the up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F is with the heat cracking reaction of macromolecule hydrocarbon, heat The reaction of cracking free radical stabilized hydrogenation is goal response, but due to the up flow type heat from hydrogenation cracking reaction process of heavy oil R10F R10 usually used hydrogenation catalyst itself has the function of that hydrofinishing and existing reactive hydrogen also can induce hydrocarbon molecule hair Therefore raw hydrofining reaction in the up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F, also necessarily occurs Hydrofining reaction.

In the up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F, when reactive hydrogen is supplied not in time, glue Matter, asphalitine thermal cracking free radical will occur condensation reaction, production molecular weight bigger molecule or structure group, repeatedly The final result of dehydrogenation and condensation reaction is to generate coke, and certainly, this is the negative reaction for needing inhibition or reduction.

Main application of the invention is the up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F, and what is used is anti- Device is answered to can be 1 or 2 or more, usually used reactor is 2~4；The up flow type heat from hydrogenation cracking of heavy oil R10F The reactor working method of reaction process R10 can be any suitable form, usually up flow type expanded bed reactor or with liquid The up flow type expanded bed reactor of body product circulation, the W-response area of separate unit up flow type expanded bed reactor, may be considered that It is divided into 2 or multiple reaction zones.The controlling party of the inlet temperature of any reaction zone of up flow type expanded bed reactor of the present invention Formula can be the temperature and/or flow for adjusting hydrogen, can be the temperature and/or flow for adjusting oil product.

The up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F, the reactor used, liquid phase in reaction compartment, The volume ratio of gas phase (or vapour phase), can be with liquid phase be it is main the case where, define reaction compartment in " liquid phase actual volume/ (liquid phase actual volume+gas phase actual volume) " is reaction compartment liquid phase fraction KL, and a point rate KL is typically larger than 0.45, is generally higher than 0.55, it is even greater than 0.70, actual reinforcing liquid-phase hydrogenatin mode is formed, in order to keep reaction compartment hydrogen partial pressure enough It is high, it may be necessary to the different height of reactor position 2 times or repeatedly add hydrogen.

When the second half reaction process R10B joint processing of the up flow type heat from hydrogenation cracking reaction process R10 of heavy oil R10F is bad When heavy oil component CRPVR in the reaction product CRP of the up flow type hydrogenation modification reaction process CR of matter hydrocarbon CRF, the second half reaction The residence time of process R10B usually meets the requirement of the heat from hydrogenation cracking rate of control heavy oil component CRPVR first, is usually arranged The heat from hydrogenation cracking rate upper limit of heavy oil component CRPVR is to prevent conversion per pass excessively high.

The reactor types of heavy oil up flow type heat from hydrogenation cracking reaction process R10 of the present invention, can be any appropriate Form, there are many known form, for example upflow fixed bed reactor, up flow type slight expanded-bed reactor, up flow type move Dynamic bed reactor, up flow type replace bed reactor, fluidized bed reactor, suspended-bed reactor, ebullated bed and suspension bed online The combination of combination cot reactor and its particular form, and it is most of have industrial application case, form relatively fixed technology Feature.

Gluey pitch shape component contained by petroleum base residual oil is usually to analyze data with dispersed phase existing for supramolecular structure Show that gluey pitch shape group dispersed phase therein is that molecular weight is up to thousands of to tens of thousands of or even hundreds of thousands rock-steady structure group, when These right groups contain a large amount of condensed-nuclei aromatics units and containing elements, the main tasks of lighting process such as metal, sulphur, nitrogen These macromoleculars are disassociated plus hydrogen saturation, cracking are ten times few compared with its original object charcoal number, hundred times even thousand times small molecules, very Obviously, the thermal cracking task of process is occupied an leading position, this can not rely solely on hydrodemetallization, hydrodesulfurization, hydrodenitrogeneration, Add hydrogen aromatic hydrocarbons saturation to realize, hydrodemetallization, hydrodesulfurization, hydrodenitrogeneration plus hydrogen aromatic hydrocarbons saturation of petroleum base residual oil etc. are pre- Hydrogenation process is substantially the unifining process for being subsequent hydrocracking reaction preparation feedstock oil, otherwise conventional downflow system Hydrocracking catalyst activated centre in fixed bed reactors by rapid Cover is caused to operate because of metal deposit and quick coking Period is too short, is unable to maintain that the minimum economic cycle of operation of course of industrialization requirement；Even with conventional downflow system The processes such as hydrodemetallization, hydrodesulfurization, hydrodenitrogeneration in fixed bed reactors plus hydrogen aromatic hydrocarbons are full, are also unable to reach higher Conversion ratio because being difficult the rapid, high volume coking problem for overcoming high temperature thermal cracking process to necessarily lead to, this is the heating power of process Learn what property was determined；In order to overcome the defect of above-mentioned fixed bed reactor system, up flow type, which occur, in reactor types to be fixed Bed, up flow type slight expanded-bed, up flow type replace the strong expanded bed of bed, up flow type i.e. ebullated bed, up flow type limiting equation expanded bed online I.e. suspension bed boiling, downflow system replace the diversified forms such as bed online.

In the hydrocracking process of petroleum base residual oil, it is normal boiling point less than 530 that normal boiling point, which is greater than 530 DEG C of fraction crackings, The conversion ratio of DEG C fraction is usually 40~80% even higher, must in order to reach so high cracking rate and improve reaction speed Hot conditions necessary to the stronger thermal cracking of right usage degree, the quick coking of catalyst active center are inevitable, In order to by reactor bed because metal deposit, coking remove the catalyst of active rapid decrease and replacement, technical staff The biggish up flow type expanded bed reactor of both catalyst bed expansion ratios of ebullated bed, suspension bed is developed, and will be subsequent High pressure hot separator and reactor merge into a unit equipment, between devices by high viscosity, the easy residual oil for foaming, easily solidifying The movement system of (between reactor and hot high score) greatly simplifies, and reliability, safety, the thermal insulation of system can be improved, mention The uniformity of temperature of charge, saves occupied area in high reactor；It is said in terms of advantageous, the cracking of residual oil boiling bed hydrogenation is hanged The high conversion that floating bed is hydrocracked is that fixed bed reactors are unable to reach, and the cracking reaction of heat absorption and exothermic plus hydrogen is anti- Should mix and carry out utilization conducive to reaction heat, be conducive to reduce reaction temperature rising, be recycled a large amount of hot reaction generation it is oily or in Between reaction generate oil and directly heat feedstock oil and can reduce fuel oil preheating temperature；It is said in terms of unfavorable, catalyst bed expansion It is bigger, compared with fixed bed reactors, the complexity of system is increased, the stationarity of operation is reduced, increases considerably Construction investment；Because increasing the abrasion and collision of catalyst, the loss of reason other than the coking of catalyst is increased；Because of bed There are the violent back-mixing of catalyst and liquid phase, the product quality containing the low conversion degree product of part fresh feed is necessarily poor.

Residual oil boiling bed hydrogenation cracking industrialization technology has H-OIL technique, LC-FINING technique, in order to optimize and stablize The fluidized state for controlling catalyst, is provided with recycle oil circulating pump system, the collector of recycle oil is placed in catalyst in reactor On bed, be equivalent to one for circulating pump provide the high-temperature high-pressure separator that must be placed in high elevation location of recycle oil with Fluidized bed reactor group, which merges, simplifies the structure of high-temperature high-pressure separator, but in order to not influence the fluidized state of ebullated bed, Position, size and the form of the collector of recycle oil all must be carefully designed；Usually by the collector arrangements of recycle oil In the underface of reactor upper spherical end socket, the collector catheter of recycle oil is mounted in reactor, the catheter There is certain rectified action to the gas, liquid, solid Multiphase Flow of suspension bed or ebullated bed bed, solve the heat preservation companion of catheter Heat problem, the stabilization of equipment performance bring adverse effect for weakening or eliminating the flowing of water conservancy diversion tube fluid to reactor；Residual oil boiling Rise bed hydroprocessing reaction system, it is necessary to catalyst interval discharge system, catalyst interval charging system are set, because system complex, Invest big, trivial operations；Residual oil boiling bed hydrogenation reaction system has another disadvantage that portion of product belongs to height plus hydrogen saturation Hydro carbons, therefore product liquid phase dissolved residue colloid, the ability of asphalitine are poor, and therefore, conversion ratio is lower, tail oil yield compared with Greatly, this limits the economy of the technique to a certain extent；Residual oil boiling bed hydrogenation reaction system has another disadvantage that not The poor-quality heavy residuum that carbon residue content is excessively high, tenor is excessively high can be handled, because tenor is excessively high so that catalyst for demetalation Consumption cause catalyst cost too big greatly very much, the excessively high conversion ratio for making reaction process of carbon residue content is too low or quick coking Cause quickly to stop work, which has limited the application ranges of the technique.

Up flow type boiling bed hydrogenation technology, be characterized in that makes to urge with the uplink flowing of reaction mass (mainly liquid phase) Agent bed generates violent expansion, and expansion rate is typically in the range of 25~45%, to lose part fixed bed hydrogenation catalyst The advantages of " high activity, high interception rate, material hydro-conversion depth are uniform " is cost, forms " ability for destroying catalyst agglomeration " " the wide area channel of little particle impurity being freely discharged ", so as to process, tenor is higher, residual carbon content is higher heavy Oil, product quality have declined too much compared with bed technology, but its quality is preferably far beyond suspension bed；It is swollen due to ebullated bed Swollen power is mainly derived from the carrying of liquid phase material, and process should not usually prevent the liquid phase of reactor using a large amount of hydrogen Volume efficiency is too low, and therefore, the exothermic effect for also limiting reaction process cannot be excessively high, and usual boiling bed hydrogenation technology is more suitable The thermal discharge of hydrogen is added to support together in processing paraffinic base or paraffin intermediate crude base weight oil, caloric receptivity and the free radical of heat scission reaction Macroscopical fuel factor after disappearing is smaller, and reactor overall temperature rise is lower, and the Unit Weight hydrogen consumption of feedstock oil is usually 1.4~2.3%. But even so, the deactivation rate of catalyst is still too high, for this purpose, the old catalyst low by regular discharge part activity Then amount of activated high raw catelyst is filled into maintain the average activity of catalyst, therefore is formed expensive high activity and added The consuming cost of hydrogen catalyst, in fact, less economic when processing petroleum base poor residuum.Meanwhile the feature of thermal response Hydrogenation tail oil poor quality when leading to high conversion, vaporizes raw material after can only making fuel oil, therefore, the raw material of boiling bed hydrogenation is light Matter conversion ratio is usually 60~75%, i.e. conversion ratio is low.Since the pellet type catalyst that boiling bed hydrogenation technology uses is basic It is same as conventional fixed bed graininess (preferably spherical) Hydrobon catalyst, is still fallen within rich in a large amount of inner ducts, high inner surface Long-pending high activity, pellet type catalyst, are unable to satisfy diffusion and the hydro-conversion of poor residuum macromolecular, normal boiling point is higher than The heavy end or forming aperture blocking to catalyst duct loses the duct that 530 DEG C of molecular dimension is huge, polarity is strong Activity or Long-Term Sorption are in inner wall activated centre generation shadowing effect, under conditions of lacking reactive hydrogen, because being difficult to add hydrogen solid It is difficult to solve adsorption desorption, thermal condensation leading reaction occurs, formed in the road of duct and blocked.Too fast catalyst inactivation speed forms nothing The hydrogenation catalyst consuming cost that method is born, and more importantly the aromatic hydrocarbons saturation hydrogen of flood tide consumes released flood tide reaction Heat makes boiling bed hydrogenation technology not have safety, the quick coking of the gum asphalt of high-temperature induction, also in reactor Bottom distribution plate, center liquid circulation pipe form a large amount of cokings, and device is forced quickly to be stopped work.If selection up flow type ebullated bed adds Hydrogen technology processes the poor residuum that tenor is high, carbon residue content is high, result necessarily a large amount of green cokes, operation in reactor device Period is too short, reaction temperature is unable to control that i.e. dangerous, catalyst inactivation cost is odd high, these effects have been the poor quality of test manufacture The Industrial Operation of heavy oil boiling bed hydrogenation device is confirmed.

The development of residue slurry-bed hydrocracking technology is the direct hydrogenation liquefaction of coal technology hair based on the 1940s What exhibition was got up, it is under conditions of facing hydrogen and fully dispersed catalyst and/or additive coexists, and leading reaction makes in height The process of warm elevated pressure raw thermal cracking residue reaction and the reaction of thermal cracking free radical stabilized hydrogenation.Floating bed hydrocracking is anti- Process is answered, the catalyst and/or additive of dispersion used are fine grain powders, are suspended in reactant, can be effectively suppressed Coke generates.Hydrogenation of residual oil suspended bed technology to the content of impurities of raw material almost without limitation, can be with formed asphalt and oil Sand.

Typically there is the residue slurry-bed hydrocracking technology of industrialization operating achievement, there is Canadian CANMET residual oil to suspend Bed hydroprocessing thermocracking process, Italian eni company EST hydrogenation of residual oil suspended bed thermocracking process.It is other it is dreg-oil suspension bed plus Hydrogen cracking technology has the BPVCC technology path of British Petroleum Company, there is BPVCC technology, the state, Venezuela of British Petroleum Company HDHPLUS technology, the Uniflex technology of Uop Inc., the U.S., the VRSH technology of U.S. Chevron of family oil company (PDVSA) Etc..

The shortcomings that in order to overcome beaded catalyst hydrogen addition technology, floating bed hydrogenation technology has casted off once and for all " is urged using particle The flood tide inner surface of agent is as hydrogenation reaction place " mode, be characterized in that " using high degree of dispersion particle catalyst Outer surface is as hydrogenation reaction place ", so that the diffusion path for completely eliminating gum asphalt arrival hydrogenation reaction place is asked Topic, can handle that tenor is higher, the higher inferior heavy oil of carbon residue content, and certainly, tenor is high, carbon residue content The most handy coking process of high inferior heavy oil such as delay coking process is handled；The reaction compartment of floating bed hydrogenation reactor, Bed expansion rate has reached maximum, and solid catalyst additional amount is usually less than 10% (with feedstock oil poidometer), forms " having the advantages that coking material bearer capabilities " and " the discharge clear passage of suspended particulate impurity ".However in fact, suspension bed adds Hydrogen reactor do not have bed concept, reaction compartment thoroughly lose fixed bed hydrogenation catalyst " high activity, high interception rate, Material hydro-conversion depth is uniform " the advantages of, then the double characteristic of " backmixing of liquid phase " with height and " liquid phase short circuit ", because This, product quality had declined compared with bed technology it is extremely more, so floating bed hydrogenation technology can only be used as poor oil pre- place Reason process, and high quality of products can not be produced.

The reaction efficiency of the catalyst surface of floating bed hydrogenation reactor depends strongly on the renewal frequency of catalyst surface The stable replacement rate with reaction compartment, therefore, the more new tool and catalyst replacement means of catalyst surface are one important The reactor of the technological means for the raising catalyst efficiency that can not be lacked, the heavy oil floating bed hydrogenation device of some industrialization at present is adopted Circulating pump is not provided with bubbling bed, this is a huge technological deficiency, as a result, interior back-mixing amount of liquid phase is uncontrollable, interior When back-mixing catalytic amount (catalyst deposit amount) is uncontrollable, catalyst appropriate particle size range is too narrow and uncontrollable, liquid phase stops Between it is uncontrollable, and its uncontrollability is stronger with the expansion of reactor diameter, these effects have been the poor quality of test manufacture The Industrial Operation of heavy oil floating bed hydrogenation device is confirmed.The suspension bed that the present invention is recommended to use carrying liqs product circulation is anti- Device is answered, to realize the stable replacement rate of the renewal frequency and reaction compartment of expected catalyst surface.

The reaction efficiency of the catalyst surface of floating bed hydrogenation reactor, also by the polar impurity in gas phase in reactor The influence that occupies of absorption, coal tar hydrogenating process, tar and coal refine altogether process generate a large amount of polar impurity such as H2O, NH3, CO, CO2 can be strongly adsorbed in catalyst surface and form shadowing effect, therefore international well-known oil product technology suppliers CHEVRON Company is arranged the scheme of the timely impurity removal gas of gas-liquid separator and in subsequent floating bed hydrogenation between proposing in the reactor The lower part of reactor introduces high-purity hydrogen, but big independent gas-liquid separator investment, Liquid level difficulty, operation danger is arranged It is dangerous big；For this purpose, this project recommends that " gas short route " technology can be used, it, will under conditions of not increasing gas-liquid separator The space that gas-liquid mixed phase material containing gas introduces at the top of suspended-bed reactor carries out gas-liquid separation, and gas phase is expelled directly out, and liquid The major part of phase enters liquid phase reactor space by circulation pipe, in the lower part of subsequent floating bed hydrogenation reactor, introduces high-purity Hydrogen gas stream forms the gaseous environment of extremely low impurity, has been formed simultaneously the highly concentrated condition of hydrogen volume, to give full play to catalysis Agent activity creates condition, and is conducive to reduce device stagnation pressure, improves conversion per pass, reduce thermal cracking gas making reaction, reduce pyrocondensation Close reaction；The scheme of above-mentioned timely impurity removal gas also has and low boiling hydrocarbon component is discharged in time, reduces its thermal cracking rate Advantage is conducive to improve liquid receipts, reduces hydrogen consumption.

The typical heavy oil lighting reaction that the floating bed hydrogenation inside reactor of inferior heavy oil occurs, is substantially one The double-bond hydrogenation of the liquid phase macromolecular carried out in the liquid phase is cracked into the string of free radical, free radical stabilized hydrogenation at singly-bound, singly-bound Connection process, high thermal cracking temperature (400~480 DEG C) generate a large amount of free radicals and relatively uniform point in entire state of aggregation liquid phase It is distributed in entire liquid Space, in order to prevent thermal condensation that prestissimo is needed to make free radical stabilized hydrogenation, it is evident that rely on catalyst The reactive hydrogen on surface is unable to reach purpose (because the probability of the liquid phase hydrocarbon molecule of catalyst contact is too low, reactive hydrogen moving process Also can group be combined into inactive hydrogen molecule), preferably reactive hydrogen and free radical uniformly adjacent presence, and same when free radical generates Step release, to realize efficiently for reactive hydrogen.The hydrogen supply agent that boiling point is suitable for is added in due course and can just cross and meets this requirement, prevents heat Condensation improves light product retention rate, these effects have been the Shenhua direct hydrogenation liquefaction of coal dress using hydrogen supply agent for running 8 years The successful longtime running result set is confirmed.The heavy that normal boiling point is huge higher than 530 DEG C of molecular dimension, polarity is strong is evaporated Point, if reactive hydrogen cannot be provided in due course, a large amount of colloids, asphalitine thermal cracking free radical will be condensed more compared with its cracking precursor Big condensation product is to reduce heat from hydrogenation cracked distillate oil (normal boiling point is lower than 530 DEG C of hydro carbons) yield, or even generates and exceed Thermal condensation the object such as coke or precursors of coke that reaction process liquid phase can dissolve, carry cause device quickly to be stopped work, these effects It should be confirmed by abundant experimental results.The present invention uses the operation mode of enough hydrogen supply agents, it is therefore intended that by mentioning in due course For the enough inhibition cokings of reactive hydrogen, the thermal cracking conversion ratio or the more stringent feed residue of working properties of residual oil are provided, is expanded The scope of application of technique, operational stability, the economy for improving process.

The possibility of thermal high separation process of the invention described in detail below or warm high pressure separation process uses air lift process XHBM。

Air lift process XHBM of the present invention, liquid hydrocarbon W material separate number with the counter current contacting of air lift hydrogen XBH: one As for 1~8 time, be usually 2~4 times；The quantity of air lift hydrogen XBH separates the needs of target according to air lift process XHBM component It determines；The operating pressure of air lift process XHBM, the typically slightly lower than operating pressure of its charging；The operation temperature of air lift process XHBM Degree, according to air lift process XHBM component separate target it needs to be determined that, usually 180~480 DEG C, generally 250~440 DEG C.

Up-flow reactor of the present invention, working method can choose:

1. floating bed hydrogenation reactor；

2. boiling bed hydrogenation reactor usually draws off the decreased catalysis of activity from bed bottom in an intermittent fashion Agent fills into fresh catalyst from bed top in an intermittent fashion and maintains bed catalyst reserve；

3. the combined type hydrogenator of suspension bed and ebullated bed

4. slight expanded-bed.

Hydrocarbon catalytic heat cracking reaction process of the present invention, refers to the raw material hydrocarbon under hot cracking catalyst existence condition What is occurred is broken heat cracking reaction process as the main purpose with carbon-carbon bond, including the usually catalytic cracking reaction process or urges Change cracking reaction process, the body material oil usually processed is wax oil, reduced crude, records a document T001 of this kind of technology It is: 1. publication title: " catalytic cracking process and engineering "；2. retrieval is encoded with books: ISBN coding: 7-80043-537-7； Chinese depository library CIP data core word: (2004) No. 131193；3. chief editor: Chen Junwu；4. publishing house: Sinopec goes out Version society.It is (light to describe typical catalytic cracking light diesel fuel for pages 459 to page 488 of document T001 " catalytic cracking process and engineering " Recycle oil), catalytic cracking recycle oil (heavy-cycle oil), catalytic cracking clarified oil physical data.According to the operation of specific device The difference of condition and product separation scheme, catalytic cracking light diesel fuel (light cycle oil), are urged at catalytic cracking recycle oil (heavy-cycle oil) The boiling point range for changing cracking clarified oil fluctuates in a certain range, and based on the present invention, it is raw that catalytic thermal cracking reaction can be improved It is reduced in the processing ratio of catalytic thermal cracking reaction process at the yield of the wax oil of oil, then goes up flow type hydrogenation modification mistake Cheng Jinhang hydrogenation reaction.

Coking heavy oil reaction process of the present invention is referred to the mink cell focus of poor hydrogen (such as decompression residuum, cracked residue Deng) it is raw material, under the conditions of high temperature and long reaction time, carry out the hot procedure of depth thermal cracking and condensation reaction, raw material It is converted into gas, naphtha, gasoline, diesel oil, heavy distillate (coking light wax oil, coking wax slop) and coke.Coking Technology type include autoclave coking, open hearth coking, delayed coking, contact coking, fluid coking, flexicoking.Modern heavy The techniques such as oily coking, including delayed coking, contact coking, fluid coking, flexicoking.Record a text of this kind of technology Offering T002 is: 1. publication title: " delay coking process and engineering "；2. retrieval is encoded with books: ISBN coding: 978-7- 80229-456-1；Chinese depository library CIP data core word: (2007) No. 168082；3. chief editor: Qu Guohua；4. publishing Society: Sinopec publishing house.Pages 188 to page 254 of document T002 " delay coking process and engineering ", describe typical delay The physical data of wax tailings.According to the difference of the operating condition of specific device and product separation scheme, the boiling range of wax tailings Range fluctuates in a certain range, and based on the present invention, coking can be improved and generate the yield of oily heavy wax oil and reduce it In the processing ratio of pyrogenetic reaction process, up flow type hydrogenation modification process is then gone to carry out hydrogenation reaction.

Due to catalytic cracking recycle oil (heavy-cycle oil), catalytic cracking clarified oil, wax tailings poor quality, it is difficult to directly Catalytic cracking is hydrocracked, and using the present invention to carry out heat from hydrogenation cracking then realizes optimization processing.

Characteristic of the invention described in detail below.

1. catalyst solid particle；

2. sulphur powder；

3. hydrocarbon ils coking material carrier semicoke particle；

1. suspended-bed reactor, that is, paste state bed reactor；

2. fluidized bed reactor；

3. suspension bed and ebullated bed combination type reactor.

Option 15, empty cylinder bubbling bed suspended-bed reactor system；

1. heat from hydrogenation cracking reaction conversion ratio is 5~25%；

1. the 80~98% of overall conversion per pass；

Selection 1, passes through front conversion zone R10A；

1. delay coking process；

2. fluidized coking process；

3. flexicoking technique.

1. the middle matter wax oil of petroleum base viscous crude；

The present invention, mode of operation CASE-A feature are as follows:

1. catalyst solid particle；

2. the particle being mainly made of carbon；

3. sulphur powder；

1. suspended-bed reactor, that is, paste state bed reactor；

2. fluidized bed reactor；

3. suspension bed and ebullated bed combination type reactor.

Option 15, empty cylinder bubbling bed suspended-bed reactor system；

The present invention, when joint processes poor quality hydrocarbon CRF, in general, in hydrocarbon CRF hydrogenation modification reaction process CR inferior, using extremely Few a part of hydrogen supply dissolvent CR~DS；

The general control principle of the gas-phase presulfiding hydrogen concentration of hydrogenation process of the invention described in detail below.

As needed, any hydrogenation process can be added in any supplement sulphur, but be typically incorporated into most upstream Hydrogenation process entrance, to guarantee reaction process necessary minimum concentration of hydrogen sulfide such as 500PPm (v) or 1000PPm (v) or the expected specified value such as 3000PPm (v), with guarantee the necessary hydrogen sulfide sectional pressure of catalyst not less than minimum specified value, with Guarantee the necessary vulcanization kenel of catalyst.The supplement sulphur can be sulfide hydrogen or can be converted into hydrogen sulfide to adding hydrogen Material of the conversion process without ill-effect, such as hydrogen sulfide containing gas or oil product, or vulcanization is generated after contacting with high-temperature hydrogen The molten sulfur or carbon disulfide of hydrogen or dimethyl disulfide etc..

The rule of the high pressure separation process of hydrogenation reaction effluent of the invention described in detail below.

The high pressure separation process of hydrogenation reaction effluent generally comprises cold high pressure separator, when hydrocarbon in hydrogenation reaction effluent When oil density big (such as close with water density) or viscosity are difficult to separate or contain solid particle greatly or with water emulsification, it is also necessary to set The high pressure hot separator that operation temperature is usually 150~450 DEG C is set, hydrogenation reaction effluent enters high pressure hot separator point at this time It by conventional liq hydrocarbon and may mainly be deposited from the hot high score gas gas being mainly made of hydrogen in volume for one and one Solid composition hot high score oil liquid body, hot high score gas enters the cold high pressure separator point that operation temperature is usually 20~80 DEG C Following target is realized: cold since a large amount of high boiling components enter in hot high score oil liquid body from for cold high score oil and cold high score gas High score oil density becomes smaller or viscosity becomes smaller or is easily isolated with water.Thermal high is arranged in the high pressure separation process of hydrogenation reaction effluent Separator is also equipped with the advantages of reducing thermal loss, because hot high score oil liquid body can be to avoid hot high score gas experience using empty The process that cools of cooler or water cooler.Meanwhile the hot high score oil liquid body in part can be returned to the hydrogenation process of upstream Be recycled, with improve receive the recycle oil hydrogenation process overall raw material property, or to the cycling hot high score oil into Row circulation plus hydrogen.

Between thermal high separate section and cold anticyclone separate section, as needed, warm high pressure separate section can be set, Become gas-liquid two-phase material after hot high score air cooling at this time, one is separated into warm high-pressure separator in volume mainly by hydrogen The warm high score gas gas and the warm high score oil liquid being mainly made of conventional liq hydrocarbon and solid that may be present of gas composition Body, warm high score gas gas enter cold anticyclone separate section and carry out cooling and gas-liquid separation.

Hydrogenation reaction effluent or hot high score gas or warm high score gas enter before cold anticyclone separate section, usually first reduce temperature (temperature should be higher than that in the hydrogenation reaction effluent gas phase degree (usually with reactive moieties feed exchange heat) to about 220~100 DEG C Crystallization temperature, the crystallization temperature of sal-ammoniac of sulphur hydrogenation ammonia), then usually injection washing water formation water filling back end hydrogenation is anti-thereto Answer effluent, it may be necessary to which 2 or multiple injection points are set, and washing water is used for absorbing ammonia and issuable other impurity such as chlorine Change hydrogen etc., and the aqueous solution after absorbing ammonia necessarily absorbs hydrogen sulfide.In cold anticyclone separate section, the water filling back end hydrogenation reaction stream Object separates out are as follows: the cold high score gas being mainly made of hydrogen in volume, one mainly by conventional liq hydrocarbon and dissolved hydrogen The cold high score oil of composition, a cold high score water be mainly made of water and dissolved with ammonia, hydrogen sulfide.The cold high score water, The content of middle ammonia is generally 0.5~15% (w), preferably 1~8% (w).One purpose of note washing water is to absorb hydrogenation reaction Ammonia and hydrogen sulfide in effluent prevent from forming sulphur hydrogenation ammonia or more sulphur ammonia Crystallization Plugging heat exchanger channels, increase system pressure Drop.The injection rate of the washing water should be determined according to following principles: on the one hand, washing water divides after injecting hydrogenation reaction effluent For vapour phase water and liquid phase water, liquid phase water has to be larger than zero, preferably washs 30% or more of water inventory；In another aspect, washing Water is washed for absorbing the ammonia in hydrogenation reaction effluent, prevents the ammonia density of high score gas too high, reduces catalyst activity, usually height Divide the ammonia volumetric concentration of gas more lower better, generally no greater than 200PPm (v), desirably no more than 50PPm (v).The cold anticyclone Separator operation pressure be hydrogenation reaction partial pressure subtract actual pressure drop, cold anticyclone separate section operating pressure with add hydrogen it is anti- The difference of pressure is answered, it is unsuitable too low or excessively high, it is usually generally 0.35~3.2MPa, 0.5~1.5MPa.The cold high score The hydrogen volume concentration value of gas, should not too low (cause device operating pressure rise), generally should not less than 70% (v), it is preferably not low In 80% (v), preferably not below 85% (v).As previously described at least part, be usually 85~100% cold high score gas return It is recycled in hydrogenation reaction part, to provide the necessary amounts of hydrogen in hydrogenation reaction part and hydrogen concentration；It is thrown to improve device Provide efficiency, it is necessary to assure circulation hydrogen concentration be not less than lower limit value above-mentioned, for this purpose, according to specific feedstock property, reaction condition, Product distribution can exclude a part of cold high score gas to exclude methane, the ethane that reaction generates.For the cold high score of discharge Gas can realize hydrogen and non-hydrogen gas component point using conventional membrane separation process or pressure swing adsorption technique or oil wash technique From, and the hydrogen of recycling is used as new hydrogen.It, can be using conventional membrane separation process or change for the cold high score gas of recycling It presses absorbing process or oil wash technique to realize hydrogen and the separation of non-hydrogen gas component, and the hydrogen of recycling is used as new hydrogen

New hydrogen enters plus hydrogen partial is to supplement the hydrogen that hydrogenation process consumes, and the higher the better for new hydrogen hydrogen concentration, generally Not preferably less than 95% (v), preferably not below 99% (v).All new hydrogen can be introduced any hydrogenation reaction part, be preferably introduced the One hydrogenator.

The present invention, in any reaction process, it can be entirely recycle hydrogen that the hydrogen gas stream used, which can be entirely new hydrogen, It can be the gaseous mixture of new hydrogen and recycle hydrogen.

For direct hydrogenation liquefaction of coal reaction process, because of conventional gas hydrocarbon, CO, CO₂Yield is huge, usually most of cold Cold high score gas of the high score gas than such as from about 70~100%, after being purified as membrane separation process obtained by permeated hydrogen pressurization after return plus Hydrogen reaction process, do not permeate gas by PSA mention hydrogen or after " steam reforming hydrogen manufacturing+PSA mentions hydrogen " pressurization return plus hydrogen it is anti- Process is answered to be recycled.

Hydrogen angle is added to say that the present invention may be implemented from the circulation of the fractionation narrow fraction oil of heavy-oil hydrogenation hot cracked product R10P Classify sub-path circulation plus hydrogen, per recycle stream all the way that there are purposes is different with effect:

1. heat from hydrogenation crackate residual oil THC-VR preferably realizes long path circulation plus hydrogen, first passes through up flow type expanded bed Hydrogenation modification reaction process CR carries out sufficient colloid, the removal of ccr by hydrotreating reaction of asphalitine turns under the conditions of there are hydrogen supply hydrocarbon Low aromatic carbon rate heavy hydrocarbon component KVRC is turned to, heat from hydrogenation is carried out subsequently into heavy oil up flow type heat from hydrogenation cracking reaction process R10 and splits Change；

2. matter wax oil THC-MVGO in heat from hydrogenation crackate, preferably realization short path circulation plus hydrogen, i.e., anti-by rear portion Answer section R10B without front conversion zone R10A, reduce hydrogenation depth, serve as far as possible colloid, asphalitine, liquid phase coke point Dissipate solvent, stable colloidal solutions system；

3. heat from hydrogenation crackate intermediate oil THC-MD, can according to need progress, front conversion zone can be passed through R10A, can be by rear portion conversion zone R10B without front conversion zone R10A；

4. lightweight hydrogen supply dissolvent, can be in up flow type expanded bed hydrogenation modification reaction process CR and/or front conversion zone R10A It is recycled；Method is that lightweight hydrogen supply dissolvent in product or its mistake hydrogen hydrocarbon are passed through the side of flash separation or air lift flash separation Method is collected in flash steam, then the hydro carbons based on flash steam is recycled, or to the hydro carbons based on flash steam Hydrogenation modification hydrocarbon products are recycled.

Certainly, in order to change the property of liquid phase of heavy-oil hydrogenation reaction process, foreign liquid has been used, such as the lightweight of outer confession supplies Hydrogen solvent, rich aromatic hydrocarbons wax oil of outer confession etc..

Reference examples

Table 1 is the property list of decompression residuum.

Table 2 is floating bed hydrogenation heat cracking reaction experimental result.

Table 3 is floating bed hydrogenation hot cracked product diesel oil (180~350 DEG C) property.

Table 4 is floating bed hydrogenation hot cracked product wax oil fraction (350~485 DEG C) property.

Table 5 is floating bed hydrogenation hot cracked product residue oil (485 DEG C of >) property.

Using the decompression residuum R10F of property such as table 1 as floating bed hydrocracking raw material, using high dispersive addition method phosphorus molybdenum The addition of sour aqueous ammonium catalyst is distributed in feed residue, and ammonium phosphomolybdate additive amount is 0.10 mass % of residual oil, make its Reaction process is converted into MoS₂；Hydrogenation Experiment carries out in high-pressure stirring reaction kettle, and hydrogen first pressing is 9.0MPa, normal reaction Journey average pressure is 14.0~14.5MPa, the reaction time is setting value, and stirring number is 180 times/min, reaction temperature 436 DEG C, gaseous product through gas chromatographic analysis, liquid consolidates product and is centrifugated out benzene insoluble (coke), and benzene soluble matter is distilled through kirschner It is divided into naphtha (C5~180 DEG C), diesel oil distillate (180~350 DEG C), wax oil fraction (350~485 DEG C) and residue oil (> 485 ℃)。

Based on above-mentioned data, the slurry-bed hydrocracking process R10 of 1,000,000 tons/year of decompression residuum R10F is built, is made With 2 floating bed hydrogenation reactors, residual oil is about 40 weights by the heat from hydrogenation cracking conversion rate that First reactor R10A is realized % is measured, residual oil is about 32 weight % by the heat from hydrogenation cracking conversion rate that second reactor R10B is realized.

The property list of 1 decompression residuum of table

Serial number	Physical property	Unit	Numerical value
				1	Relative density	g/cm³	0.997
2	Viscosity (100 DEG C)	mm²/s	1715
				3	Carbon residue (electric furnace process)	Quality %	15.4
4	Ash content	Quality %	0.025
				5	Molecular weight (VPO)		1162
6	Saturation point	Quality %	15.6
				7	Fragrance point	Quality %	33.2
8	Colloid	Quality %	48.1
				9	n-c₇Asphalitine	Quality %	3.10
10	Carbon	Quality %	85.4
				11	Hydrogen	Quality %	11.4
12	Sulphur	Quality %	2.26
				13	Nitrogen	Quality %	0.81
14	Metal amounts to	ppm	130

2 floating bed hydrogenation heat cracking reaction experimental result of table

Serial number	Physical property	Unit	Numerical value
				1	Catalyst adding manner		High degree of dispersion is added
2	Ammonium phosphomolybdate additive amount	Residual oil quality %	0.10
				3	Reaction time	Minute	65
4	Reaction pressure	MPa	14.0~14.5MPa
				5	Reaction temperature	℃	430~440
6	Bottoms conversion	Quality %	71.9
				7	Hydrogen consumption	m³/t	141
8	Products collection efficiency
				8.1	C₁~C₄	To material quality %	2.55
8.2	H₂S	To material quality %	1.22
				8.3	Naphtha	To material quality %	23.1
8.4	Diesel oil	To material quality %	19.8
				8.5	Wax oil (350~485 DEG C)	To material quality %	25.0
8.6	Residue oil (485 DEG C of >)	To material quality %	26.0
				8.7	Benzene insoluble	To material quality %	2.23

Table 3 floating bed hydrogenation hot cracked product diesel oil (180~350 DEG C) property

Serial number	Physical property	Unit	Numerical value
				1	Conversion ratio	To material quality %	71.9
2	Index of refraction (n²⁰ _D)		1.4862
				3	20 DEG C of relative densities	g/cm³	0.871
4	Condensation point	℃	7.3
				5	Iodine number	G iodine/100g oil	141
6	Aniline point	℃	66.0
				7	Cetane number		43.7
8	Element composition
				8.1	C	Quality %	85.37
8.2	H	Quality %	12.73
				8.3	N	Quality %	0.60
8.4	S	Quality %	0.89

Table 4 floating bed hydrogenation hot cracked product wax oil fraction (350~485 DEG C) property

Serial number	Physical property	Unit	Numerical value
				1	Conversion ratio	To material quality %	71.9
2	Index of refraction (n²⁰ _D)		1.5024
				3	Viscosity (100 DEG C)	mm²/s	7.21
4	Viscosity (50 DEG C)	mm²/s	36.6
				5	20 DEG C of relative densities	g/cm³	0.9424
6	Condensation point	℃	48.5
				7	Carbon residue	Quality %	0.44
8	Molecular weight (VPO)		363
				9	Element composition
9.1	C	Quality %	85.30
				9.2	H	Quality %	11.82
9.3	N	Quality %	0.98
				9.4	S	Quality %	0.87
10	Structural group composition	N-d-M method
				10.1	C_P	Quality %	36.1
10.2	C_N	Quality %	44.4
				10.3	C_A	Quality %	19.5

5 floating bed hydrogenation hot cracked product residue oil of table (485 DEG C of >) property.

Serial number	Physical property	Unit	Numerical value
				1	Conversion ratio	To raw material oil quality %	71.9
2	20 DEG C of relative densities	g/cm³	1.06
				3	Softening point	℃	76
4	Carbon residue (electric furnace process)	Quality %	30.6
				5	Molecular weight (VPO)		810
6	Element composition
				6.1	C	To quality %	86.41
6.2	H	To quality %	9.27
				6.3	N	To quality %	1.81
6.4	S	To quality %	1.29
				7	Four component analyses
7.1	Saturation point	Quality %	16.2
				7.2	Fragrance point	Quality %	23.0
7.3	Colloid	Quality %	32.3
				7.4	N-C7 asphalitine	Quality %	28.5

Embodiment one

Based on reference examples, in order to improve the overall conversion of heat from hydrogenation cracked stock oil decompression residuum, using of the invention rich Aromatic hydrocarbons wax oil is in the usage of heavy oil up flow type heat from hydrogenation cracking reaction process, and its step are as follows:

By wax catalysis cracking heavy-cycle oil (catalytic cracking wax oil) as rich aromatic hydrocarbons wax oil (matter wax oil in rich aromatic hydrocarbons), add Enter in second reactor of the floating bed hydrogenation heat cracking reaction R10 of decompression residuum R10F without by First reactor R10A, the ratio of matter wax oil weight and decompression residuum R10F weight is 20% in rich aromatic hydrocarbons；

The benzene insoluble yield in oil is generated in the heat from hydrogenation cracking reaction of decompression residuum R10F not increase (no more than 2.2 To raw material oil quality %) under the conditions of, the conversion per pass of decompression residuum R10F can be increased at least 77~78% by 72%, i.e., At least increase by the thermal cracking conversion ratio of 5.0~6.0 weight %, operating method is to extend second reactor reaction time about 6~8 Minute, while second reactor operation temperature increases by 2~3 DEG C to quality % (raw material decompression residuum R10F).

Embodiment two

It is right using the present invention in order to improve the overall heat from hydrogenation cracking conversion rate of decompression residuum R10F based on embodiment one Heat from hydrogenation crackate wax slop, residual oil carry out circulation heat from hydrogenation cracking.

The matter wax oil THC-KVGO in heat from hydrogenation crackate fractionating step, vacuum fractionation deep drawing heat from hydrogenation cracking, will hang Floating bed heat from hydrogenation crackate residue oil (475 DEG C of >) is separated into three fractions:

First fraction be in heavy-oil hydrogenation heat cracking reaction process R10 product matter wax oil THC-MVGO (mainly by routinely boiling Point forms for 400~520 DEG C of hydrocarbon；

Second fraction is heat from hydrogenation crackate heavy wax oil THC-HVGO, is mainly 510~550 DEG C by normal boiling point Hydrocarbon composition, that is, the cold oil of heavy-oil hydrogenation heat cracking reaction process R10 product at reduced pressure input of column washing section, containing solid Body；

Third fraction is heat from hydrogenation cracked residue THC-VR, and mainly the hydrocarbon by normal boiling point higher than 550 DEG C forms；

Heat from hydrogenation crackate heavy wax oil THC-HVGO is all recycled back to the floating bed hydrogenation heat of decompression residuum R10F During cracking reaction R10；

It is 2 parts, weight of the first via as outlet containing solid material THC-VR-OUT by heat from hydrogenation cracked residue THC-VR points About 12 weight % i.e. 120,000 tons/year of decompression residuum R10F weight, remaining second road decompression residuum THC-VR-TO-R10 are complete Portion is recycled back in the front conversion zone R10A of floating bed hydrogenation heat cracking reaction R10 process of decompression residuum R10F；

Heat from hydrogenation crackate heavy wax oil THC-HVGO, the second road decompression residuum THC-VR-TO-R10, overall one way are received Rate is about 11 mass % (to raw material decompression residuum R10F), and control loop hot tearing rate is 40%, and internal circulating load is about 27.5 matter It measures % (to raw material decompression residuum R10F)；

In order to realize the target, the lightweight hydrogen supply dissolvent of outer confession is applied in combination, (is surpassed in aromatic hydrocarbons using arene content about 65% The hydro carbons for crossing 70% is naphthalene series substance) catalytic cracking diesel oil stabilized hydrogenation product as hydrogen supply dissolvent (enter front conversion zone In R10A, that is, First reactor R10A), additive amount is the 20 weight % of raw material decompression residuum R10F, in decompression residuum R10F Heat from hydrogenation cracking reaction generate the condition that the benzene insoluble yield in oil does not increase (no more than 2.2 couples of raw material oil quality %) Under, the conversion per pass of decompression residuum R10F improves about 10 mass % (to raw material decompression residuum R10F)；

The present embodiment two, decompression residuum heat from hydrogenation cracking reaction process R10 includes front conversion zone R10A, separation process R10AP-THPS and rear portion conversion zone R10B；

In front conversion zone R10A, hydrogen supply hydrocarbon, there are catalyst solids existing simultaneously there are hydrogen, conventional liq hydrocarbon Under the conditions of the mixed phase material of grain, hydrocarbon material R10F is converted into hydrogenation reaction product R10AP；

It is separated into separation process R10AP-THPS, front conversion zone product R10AP containing hydrogen supply hydrocarbon or hydrogen supply hydrocarbon predecessor The gas R10AP-THPS-V and liquid R10AP-THPS-L of the solvent hydrocarbon DSTC of object, at least part gas R10AP-THPS-V Rear portion conversion zone R10B is not entered as R10AP-THPS-VK；

In rear portion hydrogenation reaction section R10B, there are hydrogen, conventional liq hydrocarbon, there may be the mixed phases of solid particle simultaneously Under the conditions of material, liquid R10AP-THPS-L carries out hydrogenation reaction R10B-R and at least part heat from hydrogenation cracking reaction conversion occurs For hydrogenation reaction product R10BP.

Embodiment three

It is anti-to be mitigated using the recycling method of lightweight hydrogen supply dissolvent for the cracking of decompression residuum heat from hydrogenation based on embodiment two The front conversion zone R10A operating condition (mainly reduction operation temperature) for answering process R10, it is former to further increase heat from hydrogenation cracking Expect the overall thermal cracking conversion ratio of oily decompression residuum R10F, reduction is outer to get rid of residual oil quantity.

In order to mitigate the front conversion zone R10A operating condition of decompression residuum heat from hydrogenation cracking reaction process R10 (mainly Reduce operation temperature), also for the overall thermal cracking conversion ratio for further increasing heat from hydrogenation cracked stock oil decompression residuum R10F, It is sufficiently improved in the reactor of front hydrogenation reaction section R10A present in polycyclic aromatic hydrocarbon, colloid, asphalitine collection outer for lightweight Hydrogen supply dissolvent DS for hydrogen efficiency, transmitting hydrogen efficiency under the premise of, using the recycling method of lightweight hydrogen supply dissolvent.

The hydrogenation process R10AP- of the material R10AP-RLK of the DSTC of hydrocarbon containing solvent is obtained based on gas R10AP-THPS-VK The hydrogen-containing hydrocarbon stream R10AP-RLKH that MR product R10AP-MRP is obtained returns to front conversion zone R10A and is recycled, confession therein Hydrogen hydrocarbon stream rate is the 50% of the outer stabilized hydrogenation product flow rate for catalytic cracking diesel oil, which is equivalent to 10 weights of feed residue Measure %.

Compared with embodiment two, in hydrogenation process R10, the conversion per pass of decompression residuum R10F increases 2~3 mass % (to raw material decompression residuum).

At this point, the quantity for getting rid of residual oil (disregarding solid) outside is reduced to 9~10 mass % (to raw material decompression residuum).

Example IV

Based on embodiment two, using the recycling method of lightweight hydrogen supply dissolvent, can reduce outer for hydrogen supply dissolvent quantity.

It is obvious that hydrogen supply dissolvent additive amount is the 20 of raw material decompression residuum R10F in maintaining front conversion zone R10A charging It, can be by outer for about 33 weight % of hydrogen supply dissolvent amount under the premise of weight %.

Embodiment five

Based on embodiment three, turn to further increase the overall thermal cracking of heat from hydrogenation cracked stock oil decompression residuum R10F Rate, reduction is outer to get rid of residual oil quantity, and CR hydrogenation modification reaction process is arranged, and first carries out to decompression residuum THC-VR-TO-R10 high Removal of ccr by hydrotreating reaction under the conditions of hydrogen supply dissolvent ratio, it is anti-to be then fully incorporated front for CR hydrogenation modification reaction product CRP It answers in section R10A, realizes the secondary use of hydrogen supply dissolvent, hydrogen, catalyst, to further improve outer for lightweight hydrogen supply Solvent DS for hydrogen efficiency, transmitting hydrogen efficiency.

Compared with embodiment three, in hydrogenation process R10, the conversion per pass of decompression residuum R10F increases 2~3 mass % (to raw material decompression residuum).At this point, the quantity for getting rid of residual oil (disregarding solid) outside is reduced to 6~7 mass % (to depressurize slag to raw material Oil).

Table 6 is the reaction condition summary sheet of CR hydrogenation modification reaction process.

The reaction condition summary sheet of 6 CR hydrogenation modification reaction process of table

Embodiment six

Based on embodiment five, change operation scheme, the product CRP of reaction process CR is introduced into residual hydrogenation heat cracking reaction Joint carries out heat from hydrogenation cracking reaction in the rear portion conversion zone R10B of process.

Claims

1. rich aromatic hydrocarbons wax oil is in the usage of heavy oil up flow type heat from hydrogenation cracking reaction process, it is characterised in that comprise the steps of:

(1) up flow type heat from hydrogenation cracking reaction conversion is carried out in heavy oil up flow type heat from hydrogenation cracking reaction process R10, heavy oil R10F For final product R10P；

In front conversion zone R10A, there are hydrogen, conventional liq hydrocarbon simultaneously there may be hydrogen supply hydrocarbon, there may be solid particles Mixed phase material under the conditions of, at least part heavy oil R10F carry out hydrogenation reaction R10A-R at least part heat from hydrogenation cracking occurs Reaction is converted into hydrogenation reaction product R10AP；Front conversion zone R10A, possible simultaneous processing is other to contain residual oil streams；

The hydrocarbonaceous liquid material for being higher than 530 DEG C of the hydrocarbon components containing at least part normal boiling point based on hydrogenation reaction product R10AP R10AP-LX enters rear portion conversion zone R10B；

In rear portion hydrogenation reaction section R10B, there are hydrogen, conventional liq hydrocarbon simultaneously there may be hydrogen supply hydrocarbon, there may be solids Under the conditions of the mixed phase material of particle, the hydrocarbonaceous liquid material R10AP-LX of at least part carries out hydrogenation reaction R10B-R generation at least one Partial hydrogenation heat cracking reaction is converted into hydrogenation reaction product R10BP；Rear portion hydrogenation reaction section R10B, possible simultaneous processing are other Containing residual oil streams；

The rich aromatic hydrocarbons wax oil for mainly containing solid particle between the possibility that 370~550 DEG C of the hydrocarbon component forms by normal boiling point KVGO adds hydrogen to turn into rear portion conversion zone R10B without front conversion zone R10A with hydrocarbonaceous liquid material R10AP-LX or its Compound contact carries out hydrogenation reaction, and the heat from hydrogenation cracking conversion product of rich aromatic hydrocarbons wax oil KVGO enters heat from hydrogenation cracked reaction product In R10BP；

(2) thermal high separate section S100, R10BP be separated into comprising conventional hydrogen, conventional gas hydrocarbon, conventional liq hydrocarbon gas Body S100V and the liquid material S100L that liquid phase component is mainly made of conventional liq hydrocarbon of solid may be contained；

(3) in liquid material recovery section S100L-GU, separation mainly may form liquid phase component by conventional liq hydrocarbon containing solid Liquid material S100L, richness that is obtaining mainly being made of normal boiling point higher than 520 DEG C of hydrocarbon and being higher than 570 DEG C containing normal boiling point Contain the heat from hydrogenation cracked vacuum residue THC-VR of solid particle containing colloid, the possibility of asphalitine.

2. according to the method described in claim 1, it is characterized by:

(4) it in gas recovery section S100V-GU, separates gas S100V and obtains hydrogen-rich gas HPV, at least part hydrogen rich gas gas Body HPV enters hydrogenation process use.

3. according to the method described in claim 2, it is characterized by:

(4) the hydrogen volume concentration of hydrogen rich gas gas HPV is greater than 75%.

4. according to the method described in claim 2, it is characterized by:

(4) the hydrogen volume concentration of hydrogen rich gas gas HPV is greater than 85%.

5. according to the method described in claim 1, it is characterized by:

Heavy oil R10F, mainly the hydrocarbon component by normal boiling point higher than 530 DEG C forms.

6. according to the method described in claim 1, it is characterized by:

Heavy oil up flow type heat from hydrogenation cracking reaction process R10 is there are powder, a kind or several in following of existing powder:

1. catalyst solid particle；

2. sulphur powder；

3. hydrocarbon ils coking material carrier semicoke particle；

7. according to the method described in claim 1, it is characterized by:

The working method of heavy oil up flow type heat from hydrogenation cracking reaction process R10, the hydrogenator R10UE used are in following 1 kind or several:

1. suspended-bed reactor, that is, paste state bed reactor；

2. fluidized bed reactor；

3. suspension bed and ebullated bed combination type reactor.

8. according to the method described in claim 1, it is characterized by:

Option 2, reactor R10UE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of device R10UE material inlet；

Option 3, reactor R10UE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of device R10UE material inlet；

Option 4, reactor R10UE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of device R10UE material inlet, while circulating pump conveys circulation fluid, downstream transport liquid material product；

Option 5, reactor R10UE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of device R10UE material inlet, while circulating pump conveys circulation fluid, downstream transport liquid material product；

Option 6, reactor R10UE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of device R10UE material inlet, be collected simultaneously cup discharge other collection liquids by other dedicated feeding engines to Downstream conveys liquid material product；

Option 7, reactor R10UE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of device R10UE material inlet, be collected simultaneously cup discharge other collection liquids by other dedicated feeding engines to Downstream conveys liquid material product；

Option 10, reactor R10UE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of device R10UE material inlet and the combination type reactor of ebullated bed；

Option 11, reactor R10UE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of device R10UE material inlet and the combination type reactor of ebullated bed, it is downstream defeated while circulating pump conveys circulation fluid Liquor charging material product；

Option 12, reactor R10UE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of device R10UE material inlet and the combination type reactor of ebullated bed, the other collection liquids for being collected simultaneously cup discharge are passed through Other dedicated feeding engine downstream transport liquid material products；

Option 15, empty cylinder bubbling bed suspended-bed reactor system；

It is anti-to form the dirty Returning reactor lower part of reactor top reaction zone liquid phase using the external circulation pipe of reactor for option 16 Answer the device outside circulation in area；

Option 17, in reactor R10UE, setting enters stripping step and the top liquid collecting of the end gas-liquid product of top liquid collecting cup Cup gas-liquid separation step, the average molecular weight for the balance liquid phase that hydrogen rich gas gas stripping gas is formed after mixing with end gas-liquid product are greater than The average molecular weight of the balance liquid phase of end gas-liquid product, the balance that hydrogen rich gas gas stripping gas is formed after mixing with end gas-liquid product The normal boiling point for the balance liquid phase that the concentration of the hydrocarbon component of the normal boiling point of liquid phase higher than 350 DEG C is greater than end gas-liquid product is higher than The concentration of 350 DEG C of the hydrocarbon component；The slurries that liquid collecting cup in the final reactor of autoreaction section is discharged through diversion pipe, as reaction Section product slurry or circular response liquid phase.

9. according to the method described in claim 1, it is characterized by:

In heavy oil up flow type heat from hydrogenation cracking reaction process R10, conversion zone obtains the mode of product liquid, in following manner 1 kind or several:

2. the final reactor of conversion zone uses pure counter-current reactor, the bottom liquid phase region of the final reactor of autoreaction section is discharged Slurries, as conversion zone product slurry；

3. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup in the final reactor of autoreaction section is through water conservancy diversion The slurries of pipe discharge, as conversion zone product slurry；

4. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup in the final reactor of autoreaction section is through water conservancy diversion The slurries of pipe discharge, as slurry to be de-gassed；

Possibility to be de-gassed contains the liquid of solid, is separated into liquid stream, all the way all the way rich in bubble by cyclonic separation step The liquid stream of lean gas bubble；The liquid stream of lean gas bubble, the possibility as conversion zone contain the product liquid of solid；

5. setting enters the stripping step and top collection of the end gas-liquid product of top liquid collecting cup in the final reactor of conversion zone Liquid cup gas-liquid separation step, the average molecular weight for the balance liquid phase that hydrogen rich gas gas stripping gas is formed after mixing with end gas-liquid product are big In the average molecular weight of the balance liquid phase of end gas-liquid product, hydrogen rich gas gas stripping gas is formed flat after mixing with end gas-liquid product The normal boiling point that the concentration of the hydrocarbon component of the normal boiling point for the liquid phase that weighs higher than 350 DEG C is greater than the balance liquid phase of end gas-liquid product is high In the concentration of 350 DEG C of the hydrocarbon component；The slurries that liquid collecting cup in the final reactor of autoreaction section is discharged through diversion pipe, as anti- Answer section product slurry or circular response liquid phase.

10. according to the method described in claim 1, it is characterized by:

(1) a kind or several in following of the mode of operation of heavy oil up flow type heat from hydrogenation cracking reaction process R10:

1. heavy oil up flow type heat from hydrogenation cracking reaction process R10, operating condition are as follows: reaction temperature is 400~485 DEG C, reactor Pressure is 6~30MPa, and vapor phase hydrogen volumetric concentration 50~95%, gas-liquid volume ratio is 300~1500Nm³/m³, hydrogenation catalyst Additive amount is 0.1~3 mass % of dry pulverized coal weight, and co-catalyst additive amount is sulphur/catalyst activity metal in co-catalyst Molar ratio be 1.0~2.0, coal slurry solid concentration be 40~60 mass %, reaction time TRU be 0.5~4 hour；

2. heavy oil up flow type heat from hydrogenation cracking reaction process R10, the heat from hydrogenation Cracking catalyst used is a kind of composite hydrogenation Catalyst includes high-activity component and low activity component；The weight ratio of the high-activity component metal and low activity component metals It is 1: 10 to 10: 1；The high-activity component contain molybdenum oil-soluble salt compounds water soluble salt compound or its mixing Object；The low activity group is divided into ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, heat from hydrogenation Cracking catalyst water content is lower than 2wt%；The powdered granule that heat from hydrogenation cracking catalyst particles diameter is 1~100 μm；

3. heavy oil up flow type heat from hydrogenation cracking reaction process R10, the heat from hydrogenation Cracking catalyst used includes nanometer ultra-fine grain Aqua oxidation iron catalyst and/or iron oxide and/or pyrite and/or bloodstone and/or molybdenum oxide and/or molybdenum sulfide and/or ammonium molybdate And/or nickel sulfide.

11. according to the method described in claim 1, it is characterized by:

Heavy oil up flow type heat from hydrogenation cracking reaction process R10, uses at least part hydrogen supply dissolvent R10-DS；

Hydrogen supply dissolvent R10-DS, it may be possible to the intermediate product institute based on heavy oil separation up flow type heat from hydrogenation cracking reaction process R10 Obtain the hydrocarbon component or its stabilized hydrogenation the hydrocarbon component contained in gas phase；

Hydrogen supply dissolvent R10-DS, it may be possible to be based on heavy oil separation up flow type heat from hydrogenation cracking reaction process R10 final reacting product The hydrocarbon component obtained by R10P or its stabilized hydrogenation the hydrocarbon component；

Hydrogen supply dissolvent R10-DS, it may be possible to the hydrogen supply the hydrocarbon component generated based on heavy oil up flow type heat from hydrogenation cracking reaction process R10 BRA-DSC；

12. according to the method described in claim 1, it is characterized by:

(1) heavy oil up flow type heat from hydrogenation cracking reaction process R10 uses at least part hydrogen supply dissolvent R10-DS；

Hydrogen supply dissolvent R10-DS is mainly 250~530 DEG C of hydro carbons by normal boiling point or is that 250~430 DEG C of hydro carbons form, middle part Dividing the weight content of saturation aromatic hydrocarbons to be greater than 15%, aromatic carbon rate is 0.35~0.70.

13. according to the method described in claim 1, it is characterized by:

Hydrogen supply dissolvent R10-DS is mainly 250~530 DEG C of hydro carbons by normal boiling point or is that 250~430 DEG C of hydro carbons form, middle part Dividing the weight content of saturation aromatic hydrocarbons to be greater than 25%, aromatic carbon rate is 0.45~0.60.

14. according to the method described in claim 1, it is characterized by:

(1) the raw material R10F of heavy oil up flow type heat from hydrogenation cracking reaction process R10 is the heavy oil being mainly made of heavy hydrocarbon HNBPC R10F；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；

In heavy oil up flow type heat from hydrogenation cracking reaction process R10, the hydro carbons group for being mainly 230~400 DEG C by normal boiling point is used At hydrogen supply hydrocarbon R10-DS；

The ratio of the weight flow rate heavy oil R10F-W of the weight flow rate R10-DS-W and heavy oil R10F of hydrogen supply hydrocarbon R10-DS are agent oil It is 0.05~2.0 than KP80, KP80=(R10-DS-W)/(R10F-W), KP80.

15. according to the method described in claim 1, it is characterized by:

The ratio of the weight flow rate heavy oil R10F-W of the weight flow rate R10-DS-W and heavy oil R10F of hydrogen supply hydrocarbon R10-DS are agent oil It is 0.2~0.6 than KP80, KP80=(R10-DS-W)/(R10F-W), KP80.

16. according to the method described in claim 1, it is characterized by:

(1) the raw material heavy oil R10F of heavy oil up flow type heat from hydrogenation cracking reaction process R10 is mainly made of heavy hydrocarbon HNBPC Heavy oil R10F；The heavy hydrocarbon HNBPC refers to that normal boiling point is higher than 450 DEG C of the hydrocarbon component；

It is anti-in the heavy hydrocarbon HNBPC heat from hydrogenation cracking of heavy oil up flow type heat from hydrogenation cracking reaction process R10, front conversion zone R10A Conversion ratio is answered, one of the following or several is selected from:

1. heat from hydrogenation cracking reaction conversion ratio is 5~25%；

17. according to the method described in claim 1, it is characterized by:

In heavy oil up flow type heat from hydrogenation cracking reaction process R10, heavy hydrocarbon HNBPC heat from hydrogenation cracking reaction conversion ratio is selected from down One or more of column:

1. the 80~98% of overall conversion per pass；

18. according to the method described in claim 1, it is characterized by:

It is anti-in the heavy hydrocarbon HNBPC heat from hydrogenation cracking of heavy oil up flow type heat from hydrogenation cracking reaction process R10, rear portion conversion zone R10B Conversion ratio is answered, one of the following or several is selected from:

3. raw material heavy oil R10F heavy oil up flow type heat from hydrogenation cracking reaction process R10 overall conversion per pass 5~20%.

19. according to the method described in claim 1, it is characterized by:

(3) in liquid material recovery section S100L-GU, separation may contain the liquid material of solid being mainly made of conventional liq hydrocarbon S100L obtains the heat from hydrogenation crackate intermediate distillates THC-MD being mainly made of the hydrocarbon that normal boiling point is 250~450 DEG C, obtains To the heat from hydrogenation cracking for mainly containing solid particle by the possibility rich in aromatic hydrocarbons that the hydrocarbon that normal boiling point is 450~570 DEG C forms Wax slop THC-HVGO is obtained that the hydrocarbon mainly by normal boiling point higher than 520 DEG C forms and is higher than 570 DEG C containing normal boiling point Contain the heat from hydrogenation cracked vacuum residue THC-VR of solid particle rich in colloid, the possibility of asphalitine；

At least part heat from hydrogenation crackate intermediate distillates THC-MD may be recycled into hydrocarbon material heat from hydrogenation cracking process R10 Reaction is participated in, the lower hydro carbons of boiling point is produced；

A part of heat from hydrogenation cracked vacuum residue THC-VR possibly serves for recycle stock THC-VR-TO-R10 and adds hydrogen into hydrocarbon material Thermal cracking process R10 participates in reaction；

A part of heat from hydrogenation cracked vacuum residue THC-VR, as the adjoint of discharge colloid, asphalitine and solid that may be present Material THC-VR-TO-OUT.

20. according to the method for claim 19, it is characterised in that: come from hydrocarbon material in material THC-VR-TO-OUT The 2~10% of the weight of the hydrocarbon component for weighing less than hydrocarbon material R10F of the hydrocarbon component of R10F.

21. according to the method for claim 19, it is characterised in that:

A part of heat from hydrogenation cracked vacuum residue THC-VR possibly serves for recycle stock THC-VR-TO-R10 and adds hydrogen into hydrocarbon material Thermal cracking process R10 participates in reaction, and working method is selected from one of the following or several:

Selection 1, passes through front conversion zone R10A；

22. according to the method described in claim 1, it is characterized by:

In heavy oil up flow type heat from hydrogenation cracking reaction process R10, raw material heavy oil R10F includes one or more of following materials:

Logistics containing oil product obtained by selection 1, middle coalite tar or its distillate or its hot procedure；Hot procedure is selected from coke Change process or catalytic cracking process or catalytic pyrolysis process or hydrogenation process；

Selection 3, direct hydrogenation liquefaction of coal liquefaction process gained logistics containing oil product, including using the coal hydrogenation of hydrogen supply dissolvent oil direct Liquefaction liquefaction process, coal refines process to oil altogether, coal faces hydrogen thermosol liquefaction process；

23. according to the method described in claim 1, it is characterized by:

(3) in liquid material recovery section S100L-GU, separation mainly may form liquid phase component by conventional liq hydrocarbon containing solid Liquid material S100L, obtain being mainly heat from hydrogenation cracking light wax oil THC-LVGO that 350~470 DEG C of hydrocarbon forms by normal boiling point；

At least part heat from hydrogenation cracking light wax oil THC-LVGO goes catalytic cracking reaction process UNIT600 to participate in reaction conversion For conventional gas hydrocarbon, conventional liq hydrocarbon and the coke that may be generated.

24. according to the method described in claim 1, it is characterized by:

(3) in liquid material recovery section S100L-GU, separation mainly may form liquid phase component by conventional liq hydrocarbon containing solid Liquid material S100L, obtain being mainly that the possibility rich in polycyclic aromatic hydrocarbon that 450~570 DEG C of hydrocarbon forms contains and consolidates by normal boiling point The heat from hydrogenation cracking wax slop THC-HVGO of body particle is obtained that the hydrocarbon mainly by normal boiling point higher than 520 DEG C forms and is contained The heat from hydrogenation cracked vacuum residue THC- that rich in colloid, the possibility of asphalitine contains solid particle of the normal boiling point higher than 570 DEG C VR；

At least part heat from hydrogenation cracked vacuum residue THC-VR and/or at least part heat from hydrogenation cracking wax slop THC-HVGO, It goes coking reaction process UNIT800 to participate in reaction and is converted into conventional gas hydrocarbon, conventional liq hydrocarbon, coke；

25. according to the method for claim 24, it is characterised in that:

The technique that pyrogenetic reaction process UNIT800 is used is selected from one of the following or several:

1. delay coking process；

2. fluidized coking process；

3. flexicoking technique.

26. according to the method described in claim 1, it is characterized by:

KVGO is the rich aromatic hydrocarbons wax oil rich in hydrogen supply hydrocarbon.

27. according to the method described in claim 1, it is characterized by:

KVGO, selected from one or more of following logistics:

1. logistics containing oil product obtained by middle coalite tar or its distillate or its hot procedure；Hot procedure is selected from coking Journey or catalytic cracking process or catalytic pyrolysis process or hydrogenation process；

3. logistics containing oil product obtained by direct hydrogenation liquefaction of coal liquefaction process, the direct hydrogenation liquefaction of coal including using hydrogen supply dissolvent oil Liquefaction process, coal refines process to oil altogether, coal faces hydrogen thermosol liquefaction process；

28. according to the method described in claim 1, it is characterized by:

Rich aromatic hydrocarbons wax oil KVGO, selected from one or more of following materials:

1. the middle matter wax oil of petroleum base viscous crude；

29. according to the method described in claim 1, it is characterized by:

Rich aromatic hydrocarbons wax oil KVGO is mainly made of the hydrocarbon component that normal boiling point is 450~510 DEG C and can contain solid particle.

30. according to the method described in claim 1, it is characterized by:

(3) in liquid material recovery section S100L-GU, separation mainly may form liquid phase component by conventional liq hydrocarbon containing solid Liquid material S100L, obtain being mainly that the possibility rich in aromatic hydrocarbons that 450~510 DEG C of hydrocarbon forms contains solid by normal boiling point Matter wax oil THC-MVGO in the heat from hydrogenation cracking of grain；

31. according to the method described in claim 1, it is characterized by:

In the rear portion conversion zone R10B of heavy oil up flow type heat from hydrogenation cracking reaction process R10, the heat from hydrogenation of rich aromatic hydrocarbons wax oil KVGO Cracking rate is lower than 40%.

32. according to the method described in claim 1, it is characterized by:

In the rear portion conversion zone R10B of heavy oil up flow type heat from hydrogenation cracking reaction process R10, the heat from hydrogenation of rich aromatic hydrocarbons wax oil KVGO Cracking rate is lower than 20%.

33. according to the method described in claim 1, it is characterized by:

Heavy oil up flow type heat from hydrogenation cracking reaction process R10 includes front conversion zone R10A, gas-liquid separation step R10AP-THPS With rear portion conversion zone R10B；

Being separated into separation process R10AP-THPS, front conversion zone product R10AP containing normal boiling point is 220~430 DEG C of hydrocarbon The gas R10AP-THPS-V of the component and liquid R10AP- for being higher than 530 DEG C of the hydrocarbon components containing at least part normal boiling point THPS-L, at least part gas R10AP-THPS-V are used as logistics R10AP-THPS-VK and do not enter rear portion conversion zone R10B；? Separation process R10AP-THPS may use hydrogen rich gas gas stripping gas to contact with liquid existing for separation process R10AP-THPS with gas Mention low boiling hydrocarbon；

The hydrocarbonaceous liquid material for being higher than 530 DEG C of the hydrocarbon components containing at least part normal boiling point based on liquid R10AP-THPS-L R10AP-THPS-LX enters rear portion conversion zone R10B；

In rear portion hydrogenation reaction section R10B, there are hydrogen, conventional liq hydrocarbon simultaneously there may be hydrogen supply hydrocarbon, there may be solids Under the conditions of the mixed phase material of particle, the hydrocarbonaceous liquid material R10AP-THPS-LX of at least part carries out hydrogenation reaction R10B-R generation At least part heat from hydrogenation cracking reaction is converted into hydrogenation reaction product R10BP；Rear portion hydrogenation reaction section R10B, may add simultaneously Work is other to contain residual oil streams；

The rich aromatic hydrocarbons wax oil for mainly containing solid particle between the possibility that 370~550 DEG C of the hydrocarbon component forms by normal boiling point KVGO, into separation process R10AP-THPS and/or rear portion conversion zone R10B without front conversion zone R10A, rich aromatic hydrocarbons wax The heat from hydrogenation cracking conversion product of oily KVGO enters in heat from hydrogenation cracked reaction product R10BP.

34. according to the method for claim 33, it is characterised in that:

The material R10AP-THPS-RLK of the ADSC of hydrocarbon containing solvent is obtained based on gas R10AP-THPS-VK, into hydrogenation reaction mistake Journey participates in reaction, and working method is selected from one or more of following manner:

35. according to the method for claim 33, it is characterised in that:

The stabilized hydrogenation process of the material R10AP-THPS-RLK of the ADSC of hydrocarbon containing solvent is obtained based on gas R10AP-THPS-VK The R10AP-THPS-RLKH containing hydrogen-containing hydrocarbon stream that the product R10AP-THPS-MRP of R10AP-THPS-MR is obtained, into adding hydrogen anti- Process is answered to participate in reaction, working method is selected from one or more of following manner:

Aromatic moiety, which occurs, in stabilized hydrogenation process R10AP-THPS-MR, material R10AP-THPS-RLK adds hydrogen saturated reaction to turn Turn to the higher hydrocarbon stream of hydrogen supply hydrocarbon concentration；Stabilized hydrogenation process R10AP-THPS-MR may be received other containing hydrogen supply simultaneously The material of hydrocarbon or the solvent hydrocarbon ADSC of hydrogen supply hydrocarbon precursor.

36. according to the method described in claim 1, it is characterized by:

Hydrocarbon CRF inferior is the high carbon residue that the possibility that the hydrocarbon component mainly by normal boiling point higher than 570 DEG C forms contains solid particle Hydrocarbon, hydrocarbon CRF carbon residue content inferior are higher than the carbon residue content in hydrocarbon material R10F with boiling fraction；

In hydrocarbon CRF up flow type expanded bed hydrogenation modification reaction process CR inferior, there are hydrogen, conventional liq hydrocarbon may deposit simultaneously In hydrogen supply hydrocarbon, there may be under the conditions of the mixed phase material of solid particle, at least part glue occurs at least part poor quality hydrocarbon CRF The hydrogenation modification reaction CR-R that the removal of ccr by hydrotreating reaction of matter, asphalitine is converted into low aromatic carbon rate heavy hydrocarbon component KVRC, which is converted into, to be added Hydrogen modified-reaction product CRP；

The flow C RP- of conversion product wax oil component comprising inferior hydrocarbon CRF and residue fraction of at least part based on product CRP X contacts progress with hydrocarbonaceous liquid material R10F or its hydro-conversion object into heavy oil up flow type heat from hydrogenation cracking reaction process R10 The heat from hydrogenation cracking conversion product of hydrogenation reaction, at least part flow C RP-X enters in heat from hydrogenation cracked reaction product R10BP；

(3) in liquid material recovery section S100L-GU, separation mainly may form liquid phase component by conventional liq hydrocarbon containing solid Liquid material S100L, obtain mainly solid higher than containing rich in colloid, the possibility of asphalitine of forming of 530 DEG C of hydrocarbon by normal boiling point The heat from hydrogenation cracked vacuum residue THC-VR of body particle；

Partial hydrogenation thermal cracking decompression residuum THC-VR, possibly serves for hydrocarbon CRF inferior and enters hydrocarbon CRF hydrogenation modification inferior reacting Journey CR participates in reaction；

At least part heat from hydrogenation cracked vacuum residue THC-VR-TO-OUT is used as discharge colloid, asphalitine and that may be present The outlet residual oil THC-VR-TO-OUT discharge system of processing of solid is without entering hydroconversion process.

37. according to the method for claim 36, it is characterised in that:

The flow C RP- of conversion product wax oil component comprising inferior hydrocarbon CRF and residue fraction of at least part based on product CRP X adds into the front conversion zone R10A of heavy oil up flow type heat from hydrogenation cracking reaction process R10 with hydrocarbonaceous liquid material R10F or its The contact of hydrogen conversion product carries out hydrogenation reaction, and the heat from hydrogenation cracking conversion product of at least part flow C RP-X enters heat from hydrogenation cracking In reaction product R10BP.

38. according to the method for claim 36, it is characterised in that:

The flow C RP- of conversion product wax oil component comprising inferior hydrocarbon CRF and residue fraction of at least part based on product CRP X, into heavy oil up flow type heat from hydrogenation cracking reaction process R10 rear portion conversion zone R10B and without front conversion zone R10A, It is contacted with hydrocarbonaceous liquid material R10AP-LX or its hydro-conversion object and carries out hydrogenation reaction, the heat from hydrogenation cracking conversion of flow C RP-X Object enters in heat from hydrogenation cracked reaction product R10BP.

39. according to the method for claim 36, it is characterised in that:

Hydrocarbon CRF inferior, with a kind or several in lower Column Properties:

Option 1, hydrocarbon CRF inferior be mainly by normal boiling point higher than 570 DEG C of the hydrocarbon component form rich in colloid, asphalitine can It can be 20~65 weight % containing the hydrocarbon stream of solid particle, carbon residue content；

Option 2, hydrocarbon CRF inferior be mainly by normal boiling point higher than 560 DEG C of the hydrocarbon component form rich in colloid, asphalitine can It can be 30~45 weight % containing the hydrocarbon stream of solid particle, carbon residue content；

Option 3, hydrocarbon CRF inferior are mainly to be contained higher than what 550 DEG C of the hydrocarbon component formed rich in colloid, asphalitine by normal boiling point There is the high carbon residue hydrocarbon of solid particle, the weight concentration of solid particle is 0.010 weight of weight %~40.0 %；

Option 4, hydrocarbon CRF inferior are mainly to be contained higher than what 540 DEG C of the hydrocarbon component formed rich in colloid, asphalitine by normal boiling point There is the high carbon residue hydrocarbon of solid particle, the weight concentration of solid particle is 0.10 weight of weight %~20.0 %；

Option 5, hydrocarbon CRF inferior are mainly to be contained higher than what 530 DEG C of the hydrocarbon component formed rich in colloid, asphalitine by normal boiling point There is the high carbon residue hydrocarbon of solid particle, the weight concentration of solid particle is 0.10 weight of weight %~15.0 %.

40. according to the method for claim 36, it is characterised in that:

(3) in liquid material recovery section S100L-GU, separation mainly may form liquid phase component by conventional liq hydrocarbon containing solid Liquid material S100L, obtain mainly solid higher than containing rich in colloid, the possibility of asphalitine of forming of 500 DEG C of hydrocarbon by normal boiling point First heat from hydrogenation cracked vacuum residue THC-VR1 of body particle obtains the richness that the hydrocarbon mainly by normal boiling point higher than 550 DEG C forms Contain the second heat from hydrogenation cracked vacuum residue THC-VR2 of solid particle containing colloid, the possibility of asphalitine；Second heat from hydrogenation cracking The weight concentration of hydrocarbon of the normal boiling point lower than 550 DEG C is lower than the first heat from hydrogenation cracked vacuum residue in decompression residuum THC-VR2 The weight concentration of hydrocarbon of the normal boiling point lower than 550 DEG C in THC-VR1；

Part or all of first heat from hydrogenation cracked vacuum residue THC-VR1 enters hydrocarbon CRF inferior as hydrocarbon CRF inferior and hydrogen is added to change Property reaction process CR participate in reaction；

Part the second heat from hydrogenation cracked vacuum residue THC-VR2 possibly serves for hydrocarbon CRF inferior and enters hydrocarbon CRF hydrogenation modification inferior Reaction process CR participates in reaction；

Second heat from hydrogenation cracked vacuum residue THC-VR2 at least partially, as discharge colloid, asphalitine, solid outer deslagging Oily THC-VR2-TO-OUT discharge system of processing is without entering hydroconversion process.

41. according to the method for claim 36, it is characterised in that:

(3) weight of the hydrocarbon component from hydrocarbon material R10F in liquid material recovery section S100L-GU, material THC-VR-TO-OUT Amount is the 2~10% of the weight of the hydrocarbon component of hydrocarbon material R10F.

42. according to the method for claim 36, it is characterised in that:

In hydrocarbon CRF hydrogenation modification reaction process CR inferior, existing solid particle includes a kind or several in following:

1. catalyst solid particle；

2. the particle being mainly made of carbon；

3. sulphur powder；

43. according to the method for claim 36, it is characterised in that:

In hydrocarbon CRF hydrogenation modification reaction process CR inferior, the working method of the hydrogenation modification reactor CRUE used is selected from following In a kind or several:

1. suspended-bed reactor, that is, paste state bed reactor；

2. fluidized bed reactor；

3. suspension bed and ebullated bed combination type reactor.

44. according to the method for claim 36, it is characterised in that:

Option 2, reactor CRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of CRUE material inlet；

Option 3, reactor CRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of CRUE material inlet；

Option 4, reactor CRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of CRUE material inlet, while circulating pump conveys circulation fluid, downstream transport liquid material product；

Option 5, reactor CRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of CRUE material inlet, while circulating pump conveys circulation fluid, downstream transport liquid material product；

Option 6, reactor CRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The fluidized bed reactor of CRUE material inlet, the other collection liquids for being collected simultaneously cup discharge pass through other dedicated feeding engines downstream Convey liquid material product；

Option 7, reactor CRUE, forced circulation Returning reactor after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The suspended-bed reactor of CRUE material inlet, the other collection liquids for being collected simultaneously cup discharge pass through other dedicated feeding engines downstream Convey liquid material product；

Option 8, reactor CRUE, top are arranged liquid collecting cup and liquid material product are discharged by the production of dedicated feeding engine downstream transport liquid material Object is not provided with the fluidized bed reactor system of liquid material product forced circulation；

Option 9, reactor CRUE, top are arranged liquid collecting cup and liquid material product are discharged by the production of dedicated feeding engine downstream transport liquid material Object is not provided with the suspended-bed reactor system of liquid material product forced circulation；

Option 10, reactor CRUE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of device CRUE material inlet and the combination type reactor of ebullated bed；

Option 11, reactor CRUE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of device CRUE material inlet and the combination type reactor of ebullated bed, it is downstream defeated while circulating pump conveys circulation fluid Liquor charging material product；

Option 12, reactor CRUE, forced circulation returns to reaction after the collection liquid that liquid collecting cup is arranged in top is pressurizeed by circulating pump The ebullated bed of device CRUE material inlet and the combination type reactor of ebullated bed are collected simultaneously other collection liquids of cup discharge by it Its dedicated feeding engine downstream transport liquid material product；

Option 15, empty cylinder bubbling bed suspended-bed reactor system；

Option 17, in reactor CRUE, setting enters stripping step and the top liquid collecting of the end gas-liquid product of top liquid collecting cup Cup gas-liquid separation step, the average molecular weight for the balance liquid phase that hydrogen rich gas gas stripping gas is formed after mixing with end gas-liquid product are greater than The average molecular weight of the balance liquid phase of end gas-liquid product, the balance that hydrogen rich gas gas stripping gas is formed after mixing with end gas-liquid product The normal boiling point for the balance liquid phase that the concentration of the hydrocarbon component of the normal boiling point of liquid phase higher than 350 DEG C is greater than end gas-liquid product is higher than The concentration of 350 DEG C of the hydrocarbon component；The slurries that liquid collecting cup in the final reactor of autoreaction section is discharged through diversion pipe, as reaction Section product slurry or circular response liquid phase.

45. according to the method for claim 36, it is characterised in that:

In hydrocarbon CRF hydrogenation modification reaction process CR inferior, conversion zone obtains to be selected from containing the mode of the product liquid of solid 1 kind or several in following manner:

1. the possibility that the gas-liquid separation process of autoreaction section reaction product is discharged contains the liquid of solid, as final reaction section The product liquid of solid may be contained；

2. the final reactor of conversion zone uses pure counter-current reactor, the bottom liquid phase region of the final reactor of autoreaction section is discharged Possibility contain the liquid of solid, the possibility as conversion zone contains the product liquid of solid；

3. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup in the final reactor of autoreaction section is through water conservancy diversion The possibility of pipe discharge contains the liquid of solid, and the possibility as conversion zone contains the product liquid of solid；

4. top liquid collecting cup is arranged in the final reactor of conversion zone, the liquid collecting cup in the final reactor of autoreaction section is through water conservancy diversion The possibility of pipe discharge contains the liquid of solid, and the liquid of solid is contained as possibility to be de-gassed；

46. according to the method for claim 36, it is characterised in that:

In the heat from hydrogenation cracking rate of hydrocarbon CRF up flow type expanded bed hydrogenation modification reaction process CR, hydrocarbon CRF inferior inferior, it is selected from down 1 kind or several in column:

47. according to the method for claim 36, it is characterised in that:

Mesh is operated in the removal of ccr by hydrotreating rate of hydrocarbon CRF up flow type expanded bed hydrogenation modification reaction process CR, hydrocarbon CRF inferior inferior Mark, a kind or several in following:

48. according to the method for claim 36, it is characterised in that:

1 kind or several in following of the mode of operation of up flow type expanded bed hydrogenation modification reaction process CR:

1. the operating condition of up flow type expanded bed hydrogenation modification reaction process CR are as follows: reaction temperature is 390~445 DEG C, reactor Pressure is 6~30MPa, and vapor phase hydrogen volumetric concentration 50~95%, gas-liquid volume ratio is 100~2000Nm³/m³, hydrogenation modification urges Agent CR-CAT additive amount is the 0.001 mass % of mass %~5 of the weight of hydrocarbon CRF inferior, and co-catalyst additive amount is to help to urge Sulphur/catalyst activity metal molar ratio is 1.0~2.0 in agent, and reaction time TRU is 5 minutes~120 minutes；

2. the hydrogenation catalyst CR-CAT that up flow type expanded bed hydrogenation modification reaction process CR is used is that a kind of composite hydrogenation is urged Agent includes high-activity component and low activity component；The weight ratio of the high-activity component metal and low activity component metals is 1 : 10 to 1000: 1；The high-activity component contain molybdenum oil-soluble salt compounds water soluble salt compound or its mixing Object；The low activity component contains ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, catalysis Agent water content is lower than 2wt%；The powdered granule that hydrogenation catalyst particle diameter is 1~100 μm；

3. the hydrogenation catalyst CR-CAT that up flow type expanded bed hydrogenation modification reaction process CR is used includes nanometer ultra-fine grain water Close ferric oxide catalyst and/or iron oxide and/or pyrite and/or bloodstone and/or molybdenum oxide and/or molybdenum sulfide and/or ammonium molybdate and Or nickel sulfide.

49. according to the method for claim 36, it is characterised in that:

In hydrocarbon CRF hydrogenation modification reaction process CR inferior, at least part hydrogen supply dissolvent CR-DS is used；

Hydrogen supply dissolvent CR-DS, it may be possible to based on institute in gas phase obtained by the intermediate product for separating hydrocarbon material heat from hydrogenation cracking process R10 The hydrocarbon component contained or its stabilized hydrogenation the hydrocarbon component；

Hydrogen supply dissolvent CR-DS, it may be possible to based on the heat from hydrogenation cracking reaction final product R10P gained hydrocarbon for separating hydrocarbon material R10F Component or its stabilized hydrogenation the hydrocarbon component；

Hydrogen supply dissolvent CR-DS, it may be possible to based on gas phase obtained by the intermediate product for separating hydrocarbon CRF hydrogenation modification reaction process CR inferior Contained in the hydrocarbon component or its stabilized hydrogenation the hydrocarbon component；

Hydrogen supply dissolvent CR-DS, it may be possible to based on obtained by the final product CRP for separating hydrocarbon CRF hydrogenation modification reaction process CR inferior The hydrocarbon component or its stabilized hydrogenation the hydrocarbon component；

Hydrogen supply dissolvent CR-DS, it may be possible to the hydrogen supply the hydrocarbon component CR- generated based on hydrocarbon CRF hydrogenation modification reaction process CR inferior DSC；

50. according to the method for claim 36, it is characterised in that:

The weight flow rate CR-DS-W of hydrogen supply dissolvent flow C R-DS and the ratio of the weight flow rate CRF-W of hydrocarbon stream CRF inferior are Oil ratio BK100=(CR-DS-W)/(CRF-W), CK100 are 0.05~5.0.

51. according to the method for claim 36, it is characterised in that:

The weight flow rate CR-DS-W of hydrogen supply dissolvent flow C R-DS and the ratio of the weight flow rate CRF-W of hydrocarbon stream CRF inferior are Oil ratio BK100=(CR-DS-W)/(CRF-W), CK100 are 0.5~1.5.

52. according to the method for claim 36, it is characterised in that:

Hydrogen supply dissolvent flow C R-DS is mainly that 250~530 DEG C of hydro carbons form by normal boiling point, the weight of part saturation aromatic hydrocarbons Measuring content to be greater than 15%, aromatic carbon rate is 0.35~0.70.

53. according to the method for claim 36, it is characterised in that:

Hydrogen supply dissolvent flow C R-DS is mainly that 250~530 DEG C of hydro carbons form by normal boiling point, the weight of part saturation aromatic hydrocarbons Measuring content to be greater than 25%, aromatic carbon rate is 0.45~0.60.

54. according to the method for claim 36, it is characterised in that:

Operation target of the CRF in up flow type expanded bed hydrogenation modification reaction process CR are as follows: hydrogen consumption is high aromatic hydrocarbons wax oil BRF weight 0.1 mass of mass %~1.5 %, CRF heat from hydrogenation cracking reaction conversion ratio be 5~20 mass %；

Operation target of the CRF in the rear portion conversion zone R10B of up flow type expanded bed heat from hydrogenation cracking reaction process R10 are as follows: heat from hydrogenation Cracking reaction conversion ratio is 20~50 mass %；

CRF is after up flow type expanded bed hydrogenation modification reaction process CR, up flow type expanded bed heat from hydrogenation cracking reaction process R10 The operation target of the overall cascade process of portion conversion zone R10B are as follows: heat from hydrogenation cracking reaction conversion ratio is 25~65 mass %.

55. according to the method for claim 36, it is characterised in that:

Operation target of the CRF in up flow type expanded bed hydrogenation modification reaction process CR are as follows: hydrogen consumption is high aromatic hydrocarbons wax oil BRF weight 0.1 mass of mass %~1.5 %, CRF heat from hydrogenation cracking reaction conversion ratio be 5~15 mass %；

Operation target of the CRF in the rear portion conversion zone R10B of up flow type expanded bed heat from hydrogenation cracking reaction process R10 are as follows: heat from hydrogenation Cracking reaction conversion ratio is 25~35 mass %；

CRF is after up flow type expanded bed hydrogenation modification reaction process CR, up flow type expanded bed heat from hydrogenation cracking reaction process R10 The operation target of the overall cascade process of portion conversion zone R10B are as follows: heat from hydrogenation cracking reaction conversion ratio is 25~50 mass %.

56. according to the method for claim 38, it is characterised in that:

At least part richness aromatic hydrocarbons wax oil KVGO first passes through up flow type expanded bed hydrogenation modification as rich aromatic hydrocarbons wax oil CR-KVGO The rear portion conversion zone R10B of heavy oil up flow type heat from hydrogenation cracking reaction process R10 is entered back into after reaction process CR and without front Conversion zone R10A；

In up flow type expanded bed hydrogenation modification reaction process CR, at least part richness aromatic hydrocarbons wax oil KVGO and poor quality hydrocarbon CRF or its At least part hydrogenation reaction occurs for the contact of hydro-conversion object, and the hydro-conversion object of rich aromatic hydrocarbons wax oil KVGO enters reaction product In CRP；

Conversion product wax oil component comprising rich aromatic hydrocarbons wax oil CR-KVGO of at least part based on product CRP includes hydrocarbon inferior The conversion product wax oil component of CRF and the flow C RP-X of residue fraction, into heavy oil up flow type heat from hydrogenation cracking reaction process R10 Rear portion conversion zone R10B and without front conversion zone R10A, contacted with hydrocarbonaceous liquid material R10AP-LX or its hydro-conversion object Hydrogenation reaction is carried out, the heat from hydrogenation cracking conversion product of flow C RP-X enters in heat from hydrogenation cracked reaction product R10BP.

57. method according to claim 56, it is characterised in that:

Operation mesh of the rich aromatic hydrocarbons wax oil KVGO in the rear portion conversion zone R10B of up flow type expanded bed heat from hydrogenation cracking reaction process R10 Be designated as: KVGO heat from hydrogenation cracking reaction conversion ratio is 20~50 mass %；

Rich aromatic hydrocarbons wax oil KVGO is in up flow type expanded bed hydrogenation modification reaction process CR, up flow type expanded bed heat from hydrogenation cracking reaction The operation target of the overall cascade process of the rear portion conversion zone R10B of process R10 are as follows: KVGO heat from hydrogenation cracking reaction conversion ratio is 15~50 mass %.

58. method according to claim 56, it is characterised in that:

Operation mesh of the rich aromatic hydrocarbons wax oil KVGO in the rear portion conversion zone R10B of up flow type expanded bed heat from hydrogenation cracking reaction process R10 Be designated as: KVGO heat from hydrogenation cracking reaction conversion ratio is 15~30 mass %；

Rich aromatic hydrocarbons wax oil KVGO is in up flow type expanded bed hydrogenation modification reaction process CR, up flow type expanded bed heat from hydrogenation cracking reaction The operation target of the overall cascade process of the rear portion conversion zone R10B of process R10 are as follows: KVGO heat from hydrogenation cracking reaction conversion ratio is 20~40 mass %.

59. according to the method for claim 36, it is characterised in that:

Being separated into separation process CRP-THPS, hydrogenation modification reaction product CRP containing normal boiling point is 220~430 DEG C of hydrocarbon groups The gas CRP-THPS-V divided the and liquid CRP-THPS-L containing at least part normal boiling point higher than 530 DEG C of the hydrocarbon components, until Few a part of gas CRP-THPS-V is used as flow C RP-THPS-VK and does not enter rear portion conversion zone R10B；In separation process CRP- THPS may use hydrogen rich gas gas stripping gas to contact with liquid existing for separation process CRP-THPS with air lift low boiling hydrocarbon；

The hydrocarbonaceous liquid material CRP- for being higher than 350 DEG C of the hydrocarbon components containing at least part normal boiling point based on liquid CRP-THPS-L THPS-LX enters rear portion conversion zone R10B.

60. method according to claim 59, it is characterised in that:

The material CRP-THPS-RLK of the ADSC of hydrocarbon containing solvent is obtained based on gas CRP-THPS-VK, is joined into hydrogenation process With react, working method is selected from one or more of following manner:

61. method according to claim 59, it is characterised in that:

The stabilized hydrogenation process CRP- of the material CRP-THPS-RLK of the ADSC of hydrocarbon containing solvent is obtained based on gas CRP-THPS-VK CRP-THPS-RLKH containing hydrogen-containing hydrocarbon stream obtained from the product CRP-THPS-MRP of THPS-MR joins into hydrogenation process With react, working method is selected from one or more of following manner:

Aromatic moiety, which occurs, in CRP-THPS-MR, material CRP-THPS-RLK adds hydrogen saturated reaction to be converted into hydrogen supply hydrocarbon concentration more High hydrocarbon stream；Stabilized hydrogenation process CRP-THPS-MR may be received other containing hydrogen supply hydrocarbon or hydrogen supply hydrocarbon precursor simultaneously The material of solvent hydrocarbon ADSC.

62. according to the method described in claim 1, it is characterized by:

The flow C RP- of conversion product wax oil component comprising inferior hydrocarbon CRF and residue fraction of at least part based on product CRP X, into separation process R10AP-THPS, being isolated at least partially based on flow C RP-X is 220 containing normal boiling point The gas of~430 DEG C of the hydrocarbon components enters in gas R10AP-THPS-V, the liquid isolated at least partially based on flow C RP-X Body enters in liquid R10AP-THPS-L；

Use 1. entering in up flow type expanded bed hydrogenation modification reaction process CR as flow C R-KVGO, with hydrocarbon CRF inferior or its The reaction of at least part heat from hydrogenation occurs for the contact of hydro-conversion object, and it is anti-that the hydro-conversion object of flow C R-KVGO enters hydrogenation modification It answers in product CRP；

2. enter separation process R10AP-THPS in, it is understood that there may be at least part be based on richness aromatic hydrocarbons wax oil KVGO and isolate Containing normal boiling point be 220~430 DEG C of the hydrocarbon components gas enter in gas R10AP-THPS-V, at least partially based on richness Aromatic hydrocarbons wax oil KVGO and the waxy oil liquid isolated enters in liquid R10AP-THPS-L；

3. enter rear portion conversion zone R10B and without front conversion zone R10A, also without separation process R10AP-THPS, with Hydrocarbonaceous liquid material R10AP-THPS-LX or the contact of its hydro-conversion object carry out hydrogenation reaction, the heat from hydrogenation of rich aromatic hydrocarbons wax oil KVGO Cracking conversion product enters in heat from hydrogenation cracked reaction product R10BP.

63. according to the method described in claim 1, it is characterized by:

(1) heavy oil up flow type heat from hydrogenation cracking reaction process R10 includes front conversion zone R10A and rear portion conversion zone R10B；

Heavy oil up flow type heat from hydrogenation cracking reaction process R10, using the reactor of at least 2 serial operations, rich aromatic hydrocarbons wax oil KVGO enters in last reactor.

64. according to the method described in claim 1, it is characterized by:

Heavy oil up flow type heat from hydrogenation cracking reaction process R10, using the reactor of at least 2 serial operations, rich aromatic hydrocarbons wax oil KVGO enters in the second half reaction compartment of last reactor.