CN105623724A

CN105623724A - Hydrogenation thermal cracking method for producing low-carbon-number single-six-membered ring hydrocarbon from high aromatic hydrocarbon

Info

Publication number: CN105623724A
Application number: CN201511007856.2A
Authority: CN
Inventors: 何巨堂; 何艺帆
Original assignee: Individual
Current assignee: Individual
Priority date: 2015-12-24
Filing date: 2015-12-24
Publication date: 2016-06-01

Abstract

The invention relates to a hydrogenation thermal cracking method for producing low-carbon-number single-six-membered ring hydrocarbon from high aromatic hydrocarbon. C6-C10 cyclohexane hydrocarbon or benzene hydrocarbon can be economically and productively prepared from medium and low temperature coal tar, benzene hydrocarbon is obtained through catalytic reforming and aromatics extraction, and a way for preparing mononuclear aromatic hydrocarbons from polycyclic aromatic hydrocarbons is opened up.

Description

A kind of high aromatic hydrocarbons produces the heat from hydrogenation cracking method of low carbon number list six-ring hydrocarbon

Technical field

The present invention relates to the heat from hydrogenation cracking method that a kind of high aromatic hydrocarbons produces low carbon number list six-ring hydrocarbon, available middle coalite tar economy ground fecund C₆��C₁₀Hexanaphthene system hydrocarbon or benzene hydrocarbon, after catalytic reforming, aromatic hydrocarbons extracting, obtain benzene class hydrocarbon.

Background technology

The present invention relates to the heat from hydrogenation cracking method of middle coalite tar.

High aromatic hydrocarbons of the present invention, refer to containing three rings and or the high oil product of the density of aromatic hydrocarbon of polycyclic aromatic hydrocarbons such as middle coalite tar.

Tricyclic structure aromatic hydrocarbons of the present invention refer to containing three ring structures and wherein at least one ring belong to the hydrocarbon class of aromatic ring, such as fluorenes, dibenzofuran, thia fluorenes, carbazole, dibenzopyridine, anthracene, phenanthrene and band side chain component thereof or its partial hydrogenation saturated products.

Polynuclear plane aromatic hydrocarbons of the present invention refer to containing four or more ring structure and wherein at least one ring belong to the hydrocarbon class of aromatic ring.

Low carbon number list six-ring hydrocarbon of the present invention, refers to C₆��C₁₀Benzene hydrocarbon or hexanaphthene system hydrocarbon, be suitable for be used as catalytic reforming aromatic hydrocarbons stock oil.

At present, the upgrading target product of this wide fraction height aromatic hydrocarbons being rich in impurity of middle coalite tar, mainly concentrate on and produce fine-quality diesel oil or diesel oil blending component, supporting means are hydrogenation upgrading approach DPU-AH, multiple method DPU-AH-P has occurred, due to the fragrant low hydrogen of height and be rich in nitrogen, sulphur, the material characteristic of oxygen impurities, this process must comprise hydrogenation removing impurities matter, deep hydrogenation is saturated, hydrogenation open loop, the steps such as hydrocracking, but it is limited by high aromatic hydrocarbons its own molecular structure feature, it is limited by existing hydrogenation catalyst technology, the net result that hydro-upgrading process molecule is reformed but may not be long straight-chain alkane, therefore, current any hydrogenation upgrading combination process DPU-AH-P, there is hydrogen consumption all unavoidably high, high-pressure hydrogenation step is many, the processing result that diesel quality is low, unit amount of finish hydrogen consumption is caused up to 5.5��6.5% and to invest coalite tar in up to 2.0��3.0 hundred million yuan/100,000 tons, diesel oil density height and cetane value is low, define " investment height, hydrogen consumption is high, energy consumption height, product quality is low " defective workmanship, once oil price reduction, such technique will lose economy.

The hydrogenation method for coal tar suspension bed of a Chinese patent ZL201010217358.1 heterogeneous catalyst, produces diesel oil.

The method of a Chinese patent application CN104593060A coal tar boiling bed hydrogenation, produces diesel oil.

Chinese patent application CN104946306A full fraction of coal tar floating bed hydrocracking and fixed bed hydrogenation modification combined method, produce diesel oil.

Method described by Chinese patent ZL201010217358.1, Chinese patent application CN104593060A, Chinese patent application CN104946306A, coalite tar in all can processing, its product summary is high-quality diesel component, " rich impurity, wide boiling range, rich aromatic ring, short-side chain " the molecular structure feature being limited by middle coalite tar, all there is the following shortcoming that cannot avoid in above-mentioned technique:

1. because target product is diesel oil, namely conventional boiling point is the hydrocarbon class of 180��350 DEG C, and containing tricyclic structure aromatic hydrocarbons more than the source of these product components, so no matter being middle coalite tar heat from hydrogenation cracking process, or the hydro-upgrading process of heat from hydrogenation cracked fuel oil component, in order to realize degree of depth aromatic saturation, it is necessary to operate under high hydrogen partial pressure, therefore plant investment is extremely high;

2. it is rich in aromatic ring event hydrogen richness because of coalite tar in raw material extremely low, adds enough hydrogen and just can reach the necessary protium content of fine-quality diesel oil, so the hydrogenation process hydrogen consumption of " middle coalite tar production fine-quality diesel oil " must be very high;

3. because of " rich aromatic ring, short-side chain " molecular structure feature of middle coalite tar, its diesel quality can not be very good, if the side group not having cetane number improver, the minimum requirement of country's diesel oil standard regulation almost may do not reached: cetane value is not less than 49,20 DEG C of density and is not more than 850kg/m³; In fact, except production part low-coagulation diesel oil is except having sales advantage the winter of cold district, coal tar hydrogenating product is all in a disadvantageous position state;

4. because its product summary is diesel component, due to requirements such as air environmental protection, the excise of diesel oil or bunker surcharge form immense pressure, on December 17th, 2015, and the current diesel oil excise is 1.2 yuans/liter, and diesel oil 20 DEG C of density press 860kg/m³Calculate, amount to the excise 1395 yuans/ton.

In order to change this situation, the upgrading appreciation space of coalite tar in raising, the feature of himself molecular structure " rich aromatic ring, short-side chain " can only be relied on, the mononuclear aromatics of the long-term thriving demand in production world market, in brief, the efficient road DPU-GB-P of " cutting mononuclear aromatics in polycyclic aromatic hydrocarbons " is walked.

The raw material petroleum naphtha of the conventional catalystic reforming method of manufacture order Polycyclic aromatic hydrocarbons, usually primarily of C₅��C₁₀, general primarily of C₆��C₉Composition, owing to the restriction of raw material sources and world market are to the thriving demand of mononuclear aromatics, mononuclear aromatics belongs to high value petroleum products for a long time, therefore, widen catalytic reforming raw material source or reduce catalytic reforming raw material unit price, the wide fraction height aromatic hydrocarbons that such as this is rich in impurity from middle coalite tar efficiently produces mononuclear aromatics, will have benefit steady in a long-term.

In brief, the present invention relates to the two ring of a kind of use, technique that three rings, polynuclear plane hydrocarbon produce single six-membered ring structure hydrocarbon, follow-up target is to produce aromatic hydrocarbon product by catalytic reforming.

It is contemplated by the invention that " wide boiling range, rich aromatic ring, short-side chain " molecular structure feature of coalite tar in relying on, by the molecular structure of target product the production low carbon number list six-ring hydrocarbon even benzene hydrocarbon of shallow satisfaction as far as possible of low hydrogen content " medium molecule that is saturated by the height of high hydrogen richness and open loop be adjusted to ", significantly reduce hydrogen consumption and or reduce process operation pressure, low carbon number list six-ring hydrocarbon even benzene hydrocarbon produce aromatic hydrocarbons Chemicals by catalytic reforming unit, avoid diesel product the excise or bunker surcharge 1395 yuans/ton.

The DPU-GB-P course of processing, the main molecules feature of its raw material and product is compared as follows:

1. the characterization of molecules of middle coalite tar is " rich impurity, wide boiling range, rich aromatic ring, short-side chain ";

2. the characterization of molecules of product mononuclear aromatics is " inclusion-free, narrow boiling range, pure aromatic ring, short-side chain ".

Very obvious, the DPU-GB-P course of processing, must comprise " adding hydrogen purification and selective hydrogenation destructing process and hydrogenation aromatic ring deformation process STEP1, catalysis dehydrogenation reformation process and aromatic ring construction process STEP2, reformation hydrogen producing as hydrogenating materials hydrogen process and hydrogen transfer process STEP3, aromatic hydrocarbons Extraction and isolation process STEP-SK " these 4 basic steps. For the process of " equivalent like products produced by same stock oil ", the quantity reducing " transfer hydrogen TH " can improve transfer hydrogen " structure target chemical key " efficiency, it is possible to obtain following effect:

1. because reducing the quantity of " transfer hydrogen TH ", for " hydrogenation aromatic ring deformation process STEP1 " reaction process, the thermal discharge that namely reaction quantity reduce catalytic hydrogenation reaction process can be reduced, thus reduce hydrogenation catalyst consumption, reduction gas products receipts rate, reduction raw material consumption, reduction investment;

2. because reducing the quantity of " transfer hydrogen TH ", for " aromatic ring construction process STEP2 ", the heat absorption amount that namely reaction quantity reduce catalytic reforming reaction process can be reduced, thus reduce catalytic reforming catalyst consumption, reduction gas products receipts rate, reduction unit scale, reduction investment and fuel consumption;

3. because reducing the quantity of " transfer hydrogen TH ", for " hydrogen transfer process STEP3 " process, it is possible to reduce hydrogen transfer amount and namely reduce investment and energy consumption;

4. because reducing the quantity of " transfer hydrogen TH ", for " aromatic hydrocarbons Extraction and isolation process STEP-SK ", when in stock oil, the character of coalite tar is identical with quantity, it is possible to reduce Low investment and energy consumption, it is to increase the quantity of liquid product and non-aromatic product.

For improving transfer hydrogen " structure target chemical key " this process goal of efficiency, compared with aromatic ring construction process STEP2, hydrogenation aromatic ring deformation process STEP1 is leading side, and aromatic ring construction process STEP2 can only be time side of leading, the hydrogenation distortion process selection that is improving hydrogenation aromatic ring deformation process STEP1 is the technology key of the DPU-GB-P course of processing.

Owing in raw material, coalite tar contains polycyclic aromatic hydrocarbons, in whole technique, hydrogenation aromatic ring deformation process STEP1 has the dual function destroying big aromatic hydrocarbons with retaining single ring architecture hydrocarbon, so its hydrogenation is out of shape the moderate control of process or says that the selectivity technology of hydrogenation deform reaction process becomes core technology naturally.

Based on this conceptual understanding, the present invention proposes guarantor's ring reformation combined method that a kind of hydrogen transfer type wide fraction height aromatic hydrocarbons produces mononuclear aromatics, optimizes integrated artistic by improving the hydrogenation distortion process selection of hydrogenation aromatic ring deformation process STEP1. Its core is, it is proposed to the method for hydrotreating of a kind of middle coalite tar main product low carbon number monocyclic hydrocarbon.

Conventional boiling point of the present invention refers to the vapour of material under a barometric point, liquid equilibrium temperature. Conventional liq hydrocarbon of the present invention refers under normal condition in liquid hydrocarbon class, comprises pentane and the higher hydrocarbon class of boiling point thereof. Impurity composition of the present invention refers to the hydrogenation products of non-hydrogen in stock oil, non-carbon, comprises water, hydrogen sulfide, ammonia, hydrogenchloride etc. Proportion of the present invention, unless stated otherwise, refers to the ratio of water-mass density under fluid density and normal pressure, 15.6 DEG C of conditions under normal pressure, 15.6 DEG C of conditions. The composition of component of the present invention or concentration or content value, unless stated otherwise, be weight basis value, and weight percent represents for weight %.

Single six-ring hydrocarbon of the present invention, it is possible to be hexanaphthene system hydrocarbon can also be benzene hydrocarbon, is generally C₆��C₁₀Hydrocarbon.

Naphtha Cut of the present invention refers to the hydrocarbon class that conventional boiling point is generally 60��180 DEG C, is generally 60��165 DEG C.

Fraction of diesel oil of the present invention refers to the hydrocarbon class that conventional boiling point is generally 160��370 DEG C, is generally 180��360 DEG C.

Solar oil fraction of the present invention refers to the hydrocarbon class that conventional boiling point is generally 155��280 DEG C, is generally 165��270 DEG C.

Heavy gas oil fraction of the present invention refers to the hydrocarbon class that conventional boiling point is generally 250��370 DEG C, is generally 260��360 DEG C.

Middle coalite tar of the present invention, refer to from the coal-tar products of pyrolysis of coal or coal generating gas or other process, can be the coal-tar middle oil (pyrolysis temperature is between 700��950 DEG C) from the coalite tar of semi-coking process (pyrolysis temperature is lower than 700 DEG C) or middle temperature process of coking or their mixing oil, usually containing coal tar heavy duty oil ingredient. Owing to raw coal character and coking or gas-making process condition change all within the specific limits, the character of middle coalite tar also changes within the specific limits. The character proportion of middle coalite tar of the present invention is generally 0.89��1.15, and to be 5��200PPm, sulphur content be usual metal content 0.1��0.7%, nitrogen content is 0.6��1.6%. Middle coalite tar of the present invention, inorganic water-content is 0.2��5.0% sometimes, sometimes organic oxygen level be generally 2.5��11%, especially be 3.5��10%, be more particularly 5��10%.

Table 1 is that in typical case's coal-tar middle oil, different boiling ranges evaporates a point content cartogram.

In table 1 typical case's coal-tar middle oil, different boiling ranges evaporates a point content cartogram

Coal-tar middle oil of the present invention, normally comprising conventional boiling range is 120��450 DEG C of hydrocarbon components and the conventional boiling point mixture higher than 450 DEG C of hydrocarbon components, usually the conventional boiling range comprising 10��20% is the lighting end FD1 (evaporating point containing double ring arene) of 120��260 DEG C, usually the conventional boiling range comprising 30��40% is evaporate a point FD2 in 260��370 DEG C (containing two ring, thrcylic aromatic hydrocarbon evaporates point), the conventional boiling range comprising 20��35% is that the conventional boiling range of the last running FD3 (containing two ring to Fourth Ring aromatic fraction) and 8��20% of 370��450 DEG C is higher than the residue oil fraction FD4 (i.e. coal-tar pitch evaporate point) of 450 DEG C.

Middle coalite tar light fraction of the present invention oil, refers to fixed bed hydrogenation technology usually to be adopted to carry out hydro-upgrading by the coal tar distillate oil that conventional boiling point is generally 60��480 DEG C, is generally 60��450 DEG C.

Middle coalite tar heavy fraction of oil of the present invention, refer to conventional boiling point usually above 370 DEG C, generally evaporate point higher than the middle coalite tar of 400 DEG C, their heat from hydrogenation cracking process, refer to occur hydrocracking reaction at least partially to produce the process of molecular weight lower than cracking stock molecular weight, this process comprises parallel hydrodemetallation (HDM), hydrofining, heat from hydrogenation cracking reaction usually, and suitable reactor types is that upflowing expanded bed is such as suspended-bed reactor or ebullated bed reactor.

Residue oil fraction FD4 is difficult to adopt conventional bed technology to realize long period usually, high receipts rate hydrogenation lighting thus adopt upflowing expanded bed as suspension bed or boiling bed hydrogenation technical transform it, reunite to prevent gum asphalt and cause unnecessary coking reaction, usually must use and have with cinder oil distillate the solvent hydrocarbon class of ability of well dissolving each other that it dissolves the dilute solution that dispersion forms gum asphalt, solvent hydrocarbon class can be conventional boiling range is the last running FD3 of 370��450 DEG C, it can also be the conversion product of the hydrogenation aromatic hydrocarbons fractional saturation of last running FD3 and residue oil fraction FD4, the conversion product of the hydrogenation aromatic hydrocarbons fractional saturation of point FD2 is evaporated in can also being. in evaporate point FD2 the conversion product of hydrogenation aromatic hydrocarbons fractional saturation belong to excellent hydrogen supply dissolvent, be rich in for hydrogen hydrocarbon.

Described herein for hydrogen hydrocarbon, refer to that there is the hydrocarbon component for hydrogen function in the high temperature hydrogenation heat cracking reaction process of low hydrogen content hydrocarbon ils such as residue oil fraction FD4, comprising the double ring arene of fractional saturation, the polycyclic aromatic hydrocarbons of fractional saturation for hydrogen hydrocarbon, the kind for hydrogen hydrocarbon used with gelatin liquefaction is identical with function or close. For, in hydrogen hydrocarbon, the hydrogen speed that supplies of two hydrogen bodies is all greater than tetrahydrochysene body, and two hydrogen bodies of thrcylic aromatic hydrocarbon are compared with two hydrogen bodies of double ring arene, and it is low that it has height to have for hydrogen speed; Test proves, although polycyclic aromatic hydrocarbons is without hydrogen supply capacity, but has the ability transmitting hydrogen. When 400 DEG C, the relative of following component supplies hydrogen speed as follows:

Table 2 lists in coal-tar middle oil the part aromatic component existed and contrast hydride boiling point, condensation point and density data, for illustration of the change of typical case's aromatic component with contrast hydride boiling point, condensation point and density.

According to the present invention, entirely the evaporating point of coal tar (need the specific components of separation and Extraction as phenol except) all needs through hydroconversion process, boiling point data hint listed by table 2: with reference to the conventional boiling point (278 DEG C) of acenaphthene, the conventional boiling point (340 DEG C) of anthracene and the conventional boiling point (450 DEG C) of naphthacene, with 260 DEG C, 370 DEG C and 450 DEG C is dividing point, approximately conventional boiling point point contains a large amount of one lower than 260 DEG C evaporate, the aromatic hydrocarbons of two ring structures, approximately conventional boiling point is that 260��370 DEG C evaporate point contains a large amount of two, the aromatic hydrocarbons of tricyclic structure, approximately conventional boiling point is that 370��450 DEG C evaporate point contains a large amount of three, the aromatic hydrocarbons of tetracyclic structure, the aromatic hydrocarbons overwhelming majority of five rings and more number of rings structures thereof concentrates and is present in conventional boiling point and evaporates point higher than a formation coal-tar pitch in 450 DEG C evaporate point.

Table 2 typical case's aromatic component and contrast hydride boiling point, condensation point and density summary sheet

Table 3 typical case's aromatic component structure and molecular structure desired deflection step cartogram thereof

It is an object of the invention to propose the method for hydrotreating that a kind of middle coalite tar produces low carbon number list six-ring hydrocarbon, narrow fraction typical case's aromatic hydrocarbons of comparison raw material and the chemical structure of target compound can directly point out the change approach of molecular structure, and then analyze the processing method of the demand that draws.

Table 3 is typical case's aromatic component structure and molecular structure desired deflection step cartogram thereof.

Table 3 is analyzed and is shown, under carbon retention rate maximumization prerequisite, most desired product under target of the present invention is: low carbon number list six-ring hydrocarbon and be used as the high-carbon number list six-ring hydrocarbon of low solidifying solar oil component, if high-carbon number list six-ring hydrocarbon abatement side chain carbon number is produced gaseous product very high market value, then the most desired product under target of the present invention is single low carbon number list six-ring hydrocarbon, that is low carbon number list six-ring hydrocarbon maximum yield technique will be become, certainly this needs the shape hydrocracking process of selecting of combination selection abatement side chain carbon number to select shape cracking technique as used or form the �� position fracture that circulation heat from hydrogenation cracking process performs six-ring side chain.

Table 3 analytic explanation:

1. taking benzene or hexanaphthene as the low carbon number list six-ring hydrocarbon of representative, namely in, conventional boiling point in coalite tar raw material F1 or in raw material F1 hydrogenation intermediate product is lower than 180 DEG C evaporate point, optimal path is that hydrofining degree of depth removing impurities matter retains circular structure simultaneously, and its suitable hydroprocessing pressure is middle low pressure;

2. two six-ring hydrocarbon by the low carbon number of representative of naphthalene or naphthane, namely in, conventional boiling point 180��260 DEG C in coalite tar raw material F1 or in raw material F1 hydrogenation intermediate product evaporates point, optimal path is hydrofining degree of depth removing impurities matter, selectively opened saturated rings, retains existing aromatic ring structure simultaneously, and its suitable hydroprocessing pressure is middle pressure;

3. taking anthracene or dihydroanthracene as the thrcylic aromatic hydrocarbon of representative or its either shallow hydrotreated lube base oil product, namely in, conventional boiling point 260��370 DEG C in coalite tar raw material F1 or in raw material F1 hydrogenation intermediate product evaporates point, existing target product is the conventional route NPC of fine-quality diesel oil, i.e. two sections of high pressure flow processs of deep hydrofinishing-overhydrocracking, its shortcoming is:

A1: hydrocracking poor selectivity, the receipts rate of target product low carbon number list six-ring hydrocarbon is low, and aromatic ring retention rate is low

Based on a partial impurities nitrogen contained by the evaporating point of conventional boiling point 260��370 DEG C, sulphur, oxygen is dibenzofuran, thia fluorenes, carbazole, the fact of dibenzopyridine, the starting-up process of anthracene deep hydrofinishing process must be deep hydrogenation removing impurities matter, object is protection and improves follow-up hydrocatalyst for saturating arylhydrocarbon, the life-span of hydrocracking catalyst and efficiency, it is saturated that deep hydrogenation removing impurities matter process unavoidably will carry out aromatic hydrocarbons deep hydrogenation, then hydrofining oil product in low ammonia environment for low impurity, the hydrofined oil of low aromatic hydrocarbons carries out hydrocracking, this is a kind of typical two sections of flow processs, its suitable hydroprocessing pressure is high pressure, use supporting catalyzer,

Because secondary hydrogenation cracking stock belongs to the saturated product of aromatic hydrocarbons deep hydrogenation, in unifining process, anthracene is except center ring is saturated, 1 outer ring of major part anthracene is also saturated, even 2 outer rings of part anthracene are all saturated, such dihydroanthracene system component concentration is too low, all saturated carbon carbon bond ionic dissociation energyes of anthracene molecule hydrofining component are close to all belonging to possible cracking position, its hydrocracking reaction does not have selectivity like this, and also deep hydrogenation is saturated in the hydrocracking catalyst absorption that its aromatic hydrocarbons generated also can be possessed acidity in addition;

A2: two sections of flow processs must be adopted, energy consumption height;

A3: one section, two sections are high top pressure operation, and investment is big.

Above-mentioned analytic explanation, in order to improve the carbon retention rate of single six-ring hydrocarbon, cracking reaction selectivity must be improved, that is must abandon conventional route NPC, be defined as approach target realizing to greatest extent " 1 anthracene molecule is just cracked into 2 benzene series things immediately after partial hydrogenation is saturated ".

The constructional feature of the hydrogenation intermediate product " dihydroanthracene " of anthracene is that the carbon-carbon bond ionic dissociation energy E2 of the non-common carbon atom of inner side ring KRI is significantly lower than the carbon-carbon bond ionic dissociation energy E1 of outside aromatic ring KRO, can provide for heat cracking reaction " selective cracking position ", also be applicable to Fourth Ring and the heat from hydrogenation cracking of above structure aromatic hydrocarbons thereof with reason, this is that the core technology building the inventive method finds.

Based on above-mentioned analysis, the present invention proposes new and innovative ways DPC i.e. " mesohigh heat from hydrogenation cracking--medium-pressure hydrocracking is refined " technique, adopt one section or two sections of flow processs, it is theoretical according to being: in order to " the selective cracking position " that efficiently utilize anthracene hydrogenation intermediate product dihydroanthracene to provide, the most effective method can only be in mesohigh heat from hydrogenation cracking reaction process, start at once to carry out heat cracking reaction in the very first time that anthracene hydrogenation intermediate product dihydroanthracene occurs, then the unsaturated carbon atom that disconnected key is formed is by hydrotreated lube base oil, due to a large amount of impurity, the competitive adsorption of macromole aromatic hydrocarbons, part benzene series produce thing can depart from catalyst surface and enter in gas phase because of the low majority of boiling point by fast desorption, owing to carbolineum heat from hydrogenation cracking catalyst inner duct diameter is necessarily much larger than the required channel diameter of benzene series thing diffusion, also due to benzene hydrocarbon or hexanaphthene system hydrocarbon molecule amount is little therefore feature that its heat movement speed is necessarily fast, benzene hydrocarbon or the quick autocatalysis agent entity of hexanaphthene system hydrocarbon leave in the reaction zone main flow logistics entered outside catalyzer entity, this sample technique not only has selective hydrogenation cracking function, also will have the function that the suppression benzene series thing excessive hydrogenation of part " inconceivable " is saturated, suppress stable hydrocarbon thermally splitting function, form the technical foundation that fluid present invention hydrocarbon receipts rate is high.

New and innovative ways DPC of the present invention i.e. " mesohigh heat from hydrogenation cracking one medium-pressure hydrocracking is refined " technique, and its principal feature is:

1. first carry out heat from hydrogenation cracking process, it is easy to " the selective cracking position " that efficiently utilize the dihydroanthracene in raw material and hydrogenation intermediate product to provide, it is possible to " effectively improving the carbon retention rate that single six-ring hydrocarbon process is produced in anthracene hydrocracking "; Namely formed " the desirable cracking reaction " of fracture center ring; At heat from hydrogenation cracking process, due to the existence of other competitive adsorption thing, the probability that split product retains aromatic hydrocarbons attribute increases substantially;

2. owing to raw material during thermally splitting processes without deep hydrofinishing, heat from hydrogenation cracking catalyst deactivation rate is fast, and suitable reactor types is that upflowing expanded bed is such as suspended-bed reactor or ebullated bed reactor;

3. owing to upflowing expanded bed must be used, it is possible to process coal-tar pitch component altogether;

4. based on above-mentioned condition, it is possible to the conventional boiling range containing anthracene system component or dihydroanthracene system component that coal heavy oil is processed generation altogether is evaporate a point R1FD2 in 260��370 DEG C, the heat from hydrogenation cracking stock as excellent " producing single six-ring hydrocarbon " recycles;

5. based on above-mentioned condition, the stable hydrocarbon in heat from hydrogenation cracking stock is endowed certain thermally splitting immunological competence, this is because:

C1: the free radical that thermally splitting relies on can be saturated rapidly by hydroconversion condition;

C2: a large amount of impurity, macromole aromatic hydrocarbons, rudimentary aromatic hydrocarbons, cracked olefin intermediate product electrical provided strong adsorption competitive power is provided, make stable hydrocarbon in the hydrocarbon class competitive adsorption process on heat from hydrogenation cracking catalyst surface " candidly acknowledging one's inferiority ", enjoy " exempting from cracking treatment ";

6. in order to suppress the coking reaction of the coal tar heavy oil of common processing, the pre-unifining process R999A of a coal tar heavy oil using upflowing expanded bed reactor can be arranged, become oil to introduce the heat from hydrogenation cracking process of anthracene the pre-hydrogenation refined raw of coal tar heavy oil;

7. the conventional boiling point in heat from hydrogenation crackate can be returned heat from hydrogenation cracking process higher than point circulation that evaporates of 400 DEG C, in order to suppress their coking reaction, the pre-unifining process R999B of a coal tar heavy oil using upflowing expanded bed reactor can be arranged, become oil to introduce the heat from hydrogenation cracking process of anthracene the pre-hydrogenation refined raw of coal tar heavy oil;

Certainly, it is possible to unifining process pre-described in R999A, R999B is combined and carries out with simple flow;

In order to optimize the heat cracking reaction time of different boiling ranges coal tar fraction, can by evaporate the 2nd or the downstream reaction district that point FD2 introduces the heat from hydrogenation cracking process R1 of the middle coalite tar heavy oil using multiple reaction zone, each reaction zone can be the overall reaction zone of a platform independent reactor, it is also possible to be the subregion space of the overall reaction zone of a reactor;

8. higher than point circulation that evaporates of 400 DEG C, the conventional boiling point in heat from hydrogenation crackate being returned heat from hydrogenation cracking process, for gum asphalt component, equivalence, in providing a kind of excellent hydrogen supply dissolvent, is beneficial to coke inhibiting reaction;

9. in order to suppress the coking reaction of heat from hydrogenation cracking reaction process to greatest extent, the ratio of component being rich in condensed-nuclei aromatics in heat from hydrogenation crackate, if conventional boiling point is higher than the heat from hydrogenation cracking tail oil of the hydrocarbon composition of 530 DEG C, does not return heat from hydrogenation cracking process in circulation;

10. due to the hydrocarbon class that the charging of secondary hydrogenation grading process is two rings and following structure thereof, hydrofining pressure only needs middle press operation, therefore energy consumption can be significantly low; According to one section of flow process, energy consumption is lower;

The operation of (11) one sections of mesohighs, press operation in two sections, investment significantly reduces;

(12) in order to suppress the coking reaction of heat from hydrogenation cracking reaction process to greatest extent, feed coal tar restriction carbon residue content and metal content, such as not obvious affect tar utilization ratio when, middle coalite tar is through deep drawing fractionation, the conventional boiling point cut out higher than 540 DEG C be rich in metal, the heavy matter coal-tar pitch of gum asphalt do not enter heat from hydrogenation cracking process, only conventional boiling point point is introduced the first hydrogenation process R10 as hydrocarbon feed R10F hydrocarbon lower than 540 DEG C evaporate;

Put before this, in order to improve once by the transformation efficiency of flow process, suppress excessive heat cracking, it is possible to adopt hot high score flow process between device, the overcracking of step-down process low-boiling point liquid product simultaneously.

So far, the present invention has proposed the heat from hydrogenation cracking method that a kind of middle coalite tar produces low carbon number list six-ring hydrocarbon.

The core of the present invention is, the present inventor has found that the committed step improving the carbon retention rate of single six-ring hydrocarbon is " just starting to carry out heat cracking reaction in the very first time that anthracene hydrogenation intermediate product dihydroanthracene occurs ", and has found associated operating conditions and flow process relation. This technology is equally applicable to fluorenes, dibenzofuran, thia fluorenes, carbazole, dibenzopyridine, owing to middle coalite tar contains a large amount of polycyclic aromatic hydrocarbonss containing heterocycle, a large amount of polycyclic aromatic hydrocarbonss or its fractional saturation hydrocarbon, therefore, the present invention " gets good out of misfortune " and obtains " the location cracking effect " longed for.

The guarantor ring reformation anabolic process DPU-GBP that hydrogen transfer type wide fraction height aromatic hydrocarbons produces mononuclear aromatics is formed based on the present invention; comprise " adding hydrogen purification and selective hydrogenation destructing process and hydrogenation aromatic ring deformation process STEP1, catalysis dehydrogenation reformation process and aromatic ring construction process STEP2, reformation hydrogen producing as hydrogenating materials hydrogen process and hydrogen transfer process STEP3, aromatic hydrocarbons Extraction and isolation process STEP-SK " these 4 basic steps, wherein the position of aromatic hydrocarbons Extraction and isolation process STEP-SK in main-process stream have two kinds may:

1. the hydrofining thing of heat from hydrogenation pressure naphtha, if aromatic hydrocarbons/naphthenic hydrocarbon ratio is lower, then catalysis dehydrogenation reformation process and aromatic ring construction process STEP2 are positioned at the upstream of process process STEP-SK, i.e. positive sequence flow process " hydrogenation process product petroleum naphtha �� catforming process product �� aromatic hydrocarbons Extraction and isolation process STEP-SK �� return catalytic reforming ";

2. the hydrofining thing of heat from hydrogenation pressure naphtha, if aromatic hydrocarbons/naphthenic hydrocarbon ratio is higher, then catalysis dehydrogenation reformation process and aromatic ring construction process STEP2 are positioned at the downstream of process process STEP-SK, i.e. inverted sequence flow process " hydrogenation process product petroleum naphtha �� aromatic hydrocarbons Extraction and isolation process STEP-SK �� catforming process product �� return aromatic hydrocarbons extraction step ".

Therefore, an object of the present disclosure is to propose a kind of to contain 260��370 DEG C of high aromatic hydrogenation method for thermal cracking evaporated point, the heat from hydrogenation cracking process being suitable in raw material or intermediate product or final product containing conventional boiling point being the high aromatic hydrocarbons of 260��370 DEG C of aromatic components, target is fecund low carbon number list six-ring hydrocarbon.

The present invention the 2nd object is to propose the heat from hydrogenation cracking method of a kind of carbolineum fecund low carbon number list six-ring hydrocarbon.

The present invention the 3rd object is to propose the heat from hydrogenation cracking method of a kind of middle coalite tar heavy oil fecund low carbon number list six-ring hydrocarbon.

The present invention the 4th object is to propose the heat from hydrogenation cracking method of a kind of coal tar heavy oil fecund low carbon number list six-ring hydrocarbon.

The present invention the 5th object is to propose the heat from hydrogenation cracking method of a kind of wide fraction coal tar fecund low carbon number list six-ring hydrocarbon.

The present invention the 6th object is to propose a kind of heat from hydrogenation cracking method entirely evaporating the voluminous low carbon number list six-ring hydrocarbon of point coal tar.

The present invention the 7th object is to propose guarantor's ring reformation combined method of coalite tar heavy oil fecund mononuclear aromatics in a kind of hydrogen transfer type.

Certain the present invention can form multiple combination process, and can combine mutually with other technique, and in such as, coalite tar heavy oil and middle coalite tar light oil can combine processing.

The method of the invention has no report.

Summary of the invention

A kind of high aromatic hydrocarbons of the present invention produces the heat from hydrogenation cracking method of low carbon number list six-ring hydrocarbon, it is characterised in that comprise following step:

(1) at the first hydrogenation process R10, under hydrogen and the first hydrogenation catalyst R10C existence condition, high aromatic hydrocarbons hydrocarbon feed R10F carries out the first hydrogenation reaction effluent R10P that the first hydrogenation reaction R10R obtains comprising hydrogen, low boiling hydrocarbon, high boiling hydrocarbon;

The hydrocarbon feed R10F of the first hydrogenation process R10 and or the first hydrogenation process R10 intermediate product and or the first hydrogenation reaction effluent R10P, containing tricyclic structure aromatic hydrocarbons at least partially and or polynuclear plane aromatic hydrocarbons;

First hydrogenation reaction R10R comprises hydrofining reaction and at least partially hydrocracking reaction at least partially, produces low carbon number list six-ring hydrocarbon at least partially;

In the first hydrogenation process R10, at least partially three rings and or polynuclear plane aromatic hydrocarbons complete heat from hydrogenation cracking reaction generate low carbon number list six-ring hydrocarbon;

The quantity of the low carbon number list six-ring hydrocarbon in the first hydrogenation reaction effluent R10P, more than the quantity of the low carbon number list six-ring hydrocarbon in the first whole charging of hydrogenation process R10;

Hydrocarbon feed R10F at least partially is had hydrofining function and hydrocracking function by the first hydrogenation process R10;

First hydrogenation catalyst R10C totally has hydrofining function and hydrocracking function;

First hydrogenation reaction effluent R10P, it is possible to containing solid particulate;

(2) at recycling step, reclaiming the first hydrogenation reaction effluent R10P, obtain hydrogen rich gas gas RH and hydrocarbon ils logistics, hydrogen rich gas gas RH goes hydrogenation process to recycle at least partially;

Reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate LN2 of conventional boiling point lower than the hydrocarbon component composition of 180 DEG C;

Reclaiming the first hydrogenation reaction effluent R10P to obtain comprising the logistics that the first hydrogenation generates oil, conventional boiling point is higher than the first hydrogenation generation oil hydrocarbon of 350 DEG C at least partially, returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C;

Reclaim the first hydrogenation reaction effluent R10P and obtain comprising the logistics that the first hydrogenation generates oil, at least partially conventional boiling point be 260��350 DEG C the first hydrogenation generate oil hydrocarbon, return the first hydrogenation process R10 and contact with the first hydrogenation catalyst R10C.

The present invention first target product is petroleum naphtha, therefore, in order to increase naphtha yield to greatest extent, at recycling step, reclaim the first hydrogenation reaction effluent R10P to obtain comprising the logistics that the first hydrogenation generates oil, at least partially conventional boiling point be 180��250 DEG C the first hydrogenation generate oil hydrocarbon, return the first hydrogenation process R10 and contact with the first hydrogenation catalyst R10C.

In order to increase naphtha yield to greatest extent, take into account increase liquid yield simultaneously, target product of the present invention, it is preferably petroleum naphtha and solar oil, therefore, at recycling step, reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate LN3 that the hydrocarbon component that conventional boiling point is 170��260 DEG C forms.

The present invention, the first hydrogenation process R10, usually uses at least one heat from hydrogenation cracking reaction district, and beds mode of operation is up-flow reactor, be selected from following in a kind or several combinations:

1. suspension bed and slurry bed system;

2. ebullated bed;

3. upflowing moving-bed;

4. upflowing slight expanded-bed.

The present invention, the hydrocarbon feed R10F of suitable processing, is selected from one or more of following materials, and containing the hydrocarbon component of conventional boiling point higher than 450 DEG C:

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

3. coal-tar heavy oil or its distillate;

4. coal liquefaction gained liquefied coal coil or its distillate, coal liquefaction craft is selected from DCL/Direct coal liquefaction or oil coal refines altogether;

5. shale oil hot procedure gained oil product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;

6. ethylene cracking tar;

7. petroleum based heavy fuel oils hot procedure gained oil product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process;

8. oil sand base heavy oil hot procedure gained oil product, hot procedure is coking heavy oil process or heavy oil catalytic cracking process or heavy oil catalytic pyrolysis process; Oil sand base heavy oil forms primarily of the hydrocarbon component of conventional boiling point higher than 500 DEG C;

9. other aromatic hydrocarbons weight content of stone higher than 50%, organonitrogen weight content higher than 0.10% hydrocarbon ils.

The present invention, common hydrocarbon feed R10F, its conventional boiling point is greater than 50% higher than the weight content of the hydrocarbon component of 250 DEG C, simultaneously containing the hydrocarbon component of conventional boiling point higher than 500 DEG C; Hydrocarbon feed R10F is selected from one or more of following materials:

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

3. the conventional boiling point of coal-tar heavy oil is lower than the distillate of 530 DEG C.

The present invention, the first hydrogenation process R10, in order to avoid excessive heat condensation coking reaction and thermo-cracking air-generating reaction, the heat from hydrogenation cracking conversion rate KY of hydrocarbon feed R10F, is generally 20��65%, is generally 30��45%;

The heat from hydrogenation cracking conversion rate KY of hydrocarbon feed R10F is defined as: KY=(PNLL-FNLL)/FNHH;

FNLL, represents that conventional boiling point in raw material hydrocarbon is lower than the hydrocarbon composition weight of 250 DEG C;

FNHH, represents that conventional boiling point in raw material hydrocarbon is higher than the hydrocarbon composition weight of 250 DEG C;

PNLL, represents that conventional boiling point in product hydrocarbon is lower than the hydrocarbon composition weight of 250 DEG C;

PNHH, represents that conventional boiling point in product hydrocarbon is higher than the hydrocarbon composition weight of 250 DEG C.

The present invention, the first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, conventional boiling point is the part by weight of the hydrocarbon component R10P-N of 70��180 DEG C: is generally 20��90%, is generally 30��80%, be preferably 40��70%.

The present invention, first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, conventional boiling point be the hydrocarbon component R10P-N of 70��180 DEG C part by weight: be usually not less than 30%, be generally not less than 40%, preferably be not less than 50%.

The present invention, during main product petroleum naphtha, first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, conventional boiling point is the part by weight of the hydrocarbon component R10P-N of 70��260 DEG C: be usually not less than 60%, be generally not less than 70%, preferably be not less than 75%.

The present invention, the first hydrogenation process R10, when adopting floating bed hydrogenation operating method, operational condition is generally: temperature of reaction is 320��480 DEG C, reaction pressure 6��25MPa, volume space velocity 0.2��5.0h^-1, hydrogen to oil volume ratio 200��3000.

The present invention, the first hydrogenation process R10, when adopting floating bed hydrogenation operating method, operational condition is generally: temperature of reaction is 360��480 DEG C, reaction pressure 8��18MPa, volume space velocity 0.2��5.0h^-1, hydrogen to oil volume ratio 200��1500.

The present invention, the first hydrogenation process R10, when adopting boiling bed hydrogenation operating method, operational condition is generally: temperature of reaction is 320��480 DEG C, reaction pressure 6��25MPa, volume space velocity 0.2��5.0h^-1, hydrogen to oil volume ratio 200��3000. ;

The present invention, the first hydrogenation process R10, when adopting boiling bed hydrogenation operating method, operational condition is generally: temperature of reaction is 320��480 DEG C, reaction pressure 6��25MPa, volume space velocity 0.2��5.0h^-1, hydrogen to oil volume ratio 200��3000.

The present invention, the first hydrogenation process R10, it is possible to comprise the reaction zone of at least two serial operations, the first mode of operation is:

(1) at the first hydrogenation process R10, the reaction zone of at least two serial operations is comprised, even if the first reaction zone R10RF1 of spent hydroprocessing catalyst R10RF1C, making the second reaction zone R10RF2 of spent hydroprocessing catalyst R10RF2C;

(2) at recycling step, reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate LN2 of conventional boiling point lower than the hydrocarbon component composition of 180 DEG C;

Reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate RN of conventional boiling point higher than the hydrocarbon component composition of 180 DEG C, distillate RN enters the first hydrogenation process R10 at least partially second reaction zone R10RF2 and the first hydrogenation catalyst R10RF2C contact and not by the first reaction zone R10RF1.

The present invention, the first hydrogenation process R10, it is possible to comprise the reaction zone of at least two serial operations, the 2nd kind of mode of operation is:

Reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate LN3 that the hydrocarbon component that conventional boiling point is 170��260 DEG C forms;

Reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate RN of conventional boiling point higher than the hydrocarbon component composition of 260 DEG C, distillate RN enters the first hydrogenation process R10 at least partially second reaction zone R10RF2 and hydrogenation catalyst R10RF2C contact and not by the first reaction zone R10RF1.

The present invention, the first hydrogenation process R10, it is possible to comprise the reaction zone of at least two serial operations, the third mode of operation is:

Reclaim the first hydrogenation reaction effluent R10P, obtaining is the distillate RN1 of the hydrocarbon component composition of 260��450 DEG C primarily of conventional boiling point, distillate RN1 enters the first hydrogenation process R10 at least partially second reaction zone R10RF2 and hydrogenation catalyst R10RF2C contact and not by the first reaction zone R10RF1;

Reclaim the first hydrogenation reaction effluent R10P, obtaining primarily of the distillate RN2 of conventional boiling point higher than the hydrocarbon component composition of 450 DEG C, the first reaction zone R10RF1 that distillate RN2 enters the first hydrogenation process R10 at least partially contacts with the first hydrogenation catalyst R10RF1C.

The present invention, the first hydrogenation process R10, in order to reduce raw burnt amount, at recycling step, reclaiming the first hydrogenation reaction effluent R10P, obtain primarily of the distillate DO of conventional boiling point higher than the hydrocarbon component composition of 530 DEG C, distillate DO does not return the first hydrogenation process R10.

The present invention, the first hydrogenation process R10, it is possible to comprise the reaction zone of at least two serial operations, different boiling ranges raw material can combine processing, and the first mode of operation is:

(1) at the first hydrogenation process R10, the reaction zone of at least two serial operations is comprised, even if the first reaction zone R10SF1 of spent hydroprocessing catalyst R10SF1C, making the second reaction zone R10SF2 of spent hydroprocessing catalyst R10SF2C;

Hydrocarbon feed R10F comprises the different stock oil of two-way boiling point, primarily of conventional boiling point lower than the first hydrocarbon feed R10F1 of the hydrocarbon component composition of 350 DEG C, primarily of the two hydrocarbon feed R10F2 of conventional boiling point higher than the hydrocarbon component composition of 350 DEG C;

Second reaction zone R10SF2 and hydrogenation catalyst R10SF2C that first hydrocarbon feed R10F1 enters the first hydrogenation process R10 contact and not by the first reaction zone R10SF1;

The first reaction zone R10SF1 that second reaction zone R10S2 enters the first hydrogenation process R10 contacts with hydrogenation catalyst R10SF1C, and the first reaction zone product R10SF-P enters second reaction zone R10SF2.

The present invention, the first hydrogenation process R10, it is possible to comprise the reaction zone of at least two serial operations, different boiling ranges raw material can combine processing, and the 2nd kind of mode of operation is:

(1) at the first hydrogenation process R10, reaction zone i.e. the first reaction zone R10S1, the second reaction zone R10S2 of at least two serial operations is comprised;

Hydrocarbon feed R10F comprises the different stock oil of two-way boiling point, primarily of conventional boiling point be the hydrocarbon component composition of 260��350 DEG C the first hydrocarbon feed R10F1, primarily of the two hydrocarbon feed R10F2 of conventional boiling point higher than the hydrocarbon component composition of 350 DEG C;

The present invention, the first hydrogenation process R10, it is possible to comprise the reaction zone of at least two serial operations, different boiling ranges raw material can combine processing, and the third mode of operation is:

Hydrocarbon feed R10F forms primarily of the hydrocarbon component of conventional boiling point higher than 260 DEG C, and raw material R10F enters the first reaction zone R10S1; First reaction zone product R10S1-P enters thermal high sepn process RMS and is separated into gas RMSV and comprises the mixed phase logistics RMSL of solid, liquid;

Mixed phase logistics RMSL enters second reaction zone R10S2, and second reaction zone product R10S2-P and gas RMSV forms the first hydrogenation reaction effluent R10P jointly.

The present invention, the hydrogenation grading process of the first hydrogenation reaction effluent R10P, it is possible to combining other raw material hydrocarbon of processing, the first mode of operation is:

(2) at recycling step, unifining process RL10 is set;

At unifining process RL10, under hydrogen and Hydrobon catalyst RL10C existence condition, there is hydrofining reaction RL10R primarily of conventional boiling point lower than the hydrocarbon feed RL10F of the hydrocarbon component composition of 260 DEG C, obtain hydrofining reaction effluent RL10P; Hydrofining reaction effluent RL10P mixes with the first hydrogenation reaction effluent R10P.

The present invention, the hydrogenation grading process of the first hydrogenation reaction effluent R10P, it is possible to combining other raw material hydrocarbon of processing, the 2nd kind of mode of operation is:

(2) at recycling step, thermal high sepn process S10 and unifining process RL10 is set;

At thermal high sepn process S10, first hydrogenation reaction effluent R10P completes high boiling hydrocarbon component and the relative separation of low boiling hydrocarbon component, obtains the oil S1L of the hot high score containing solid ingredient and comprises the gas S10-PV formed primarily of hydrogen on volume of low boiling hydrocarbon component;

At unifining process RL10, under hydrogen and Hydrobon catalyst RL10C existence condition, there is hydrofining reaction RL10R primarily of conventional boiling point lower than the hydrocarbon feed RL10F of the hydrocarbon component composition of 260 DEG C, obtain hydrofining reaction effluent RL10P; Hydrofining reaction effluent RL10P mixes with gas S10-PV.

The present invention, at recycling step, it is possible to arranging thermal high sepn process S10, its mode of operation is as follows:

1. at thermal high sepn process S10, first hydrogenation reaction effluent R10P completes high boiling hydrocarbon component and the relative separation of low boiling hydrocarbon component, obtains the oil S1L of the hot high score containing solid ingredient and comprises the gas S10-PV formed primarily of hydrogen on volume of low boiling hydrocarbon component.

The present invention, the high boiling fraction in the first hydrogenation reaction effluent R10P, it is possible to return the first hydrogenation process R10 circulation cracking, as formed high voltage short circuit circulation, the first mode of operation is:

(2) at recycling step, at thermal high sepn process S10, hot high score oil S1L returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C at least partially.

The present invention, the high boiling fraction in the first hydrogenation reaction effluent R10P, it is possible to return the first hydrogenation process R10 circulation cracking, as formed high voltage short circuit circulation, the 2nd kind of mode of operation is:

(2) at recycling step, at thermal high sepn process S10, hot high score oil S1L is de-at least partially contacts with the first hydrogenation catalyst R10C except returning the first hydrogenation process R10 after solid particulate.

The present invention, at recycling step, it is possible to arranging thermal high sepn process S10 and depressurization step 1DPS, its mode of operation is as follows:

At depressurization step 1DPS, carry out the logistics logistics S1L-VLS after step-down equipment obtains step-down containing solid impurity of self-heating high score oil S1L.

The present invention, the high boiling fraction in the first hydrogenation reaction effluent R10P, it is possible to return the first hydrogenation process R10 circulation cracking, as formed low-voltage short-circuiting circulation, the first mode of operation is:

(2) at recycling step, at depressurization step 1DPS, after step-down, logistics S1L-VLS deviates from gas and becomes liquid-solid logistics S1L-VLS-DV at least partially, and liquid-solid logistics S1L-VLS-DV returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C at least partially.

The present invention, the high boiling fraction in the first hydrogenation reaction effluent R10P, it is possible to return the first hydrogenation process R10 circulation cracking, as formed low-voltage short-circuiting circulation, the 2nd kind of mode of operation is:

(2) at recycling step, at depressurization step 1DPS, after step-down, logistics S1L-VLS deviates from gas, deviates from solid at least partially and become logistics S1L-VLS-DVI at least partially, and logistics S1L-VLS-DVI returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C at least partially.

The present invention, the high boiling fraction in the first hydrogenation reaction effluent R10P, it is possible to return the first hydrogenation process R10 circulation cracking, as formed low pressure long road circulation, mode of operation is:

(2) at recycling step, reclaim the effluent stream of thermal high sepn process S10 and the effluent stream of depressurization step 1DPS, obtain primarily of conventional boiling point higher than 180 DEG C or higher than 260 DEG C or higher than the distillate VGO2 of 300 DEG C or hydrocarbon component composition higher than 330 DEG C, distillate VGO2 goes the 3rd unifining process R3X to contact with the 3rd hydrogenation catalyst R3XC at least partially, obtains the 3rd hydrofining reaction effluent R3XP; 3rd hydrofining reaction effluent R3XP enters the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C.

The present invention, the high boiling fraction in the first hydrogenation reaction effluent R10P, it is possible to return the first hydrogenation process R10 circulation cracking, as formed the circulation from sepn process FRAC1, the first mode of operation is:

(2) at recycling step, at sepn process FRAC1, after separation step-down, logistics S1L-VLS obtains primarily of the distillate LN2 of conventional boiling point lower than the conventional liquid hydrocarbon composition of 180 DEG C, distillate LN2 enters hydrogenation upgrading reaction process R20 at least partially, under hydrogen and hydrogenation upgrading catalyzer R20C existence condition, carry out hydrogenation upgrading reaction, obtain hydrogenation upgrading reaction effluent R20P;

After separation step-down, logistics S1L-VLS obtains primarily of the distilled oil FRAC1-VH of conventional boiling point higher than the hydrocarbon component composition of 180 DEG C, and distilled oil FRAC1-VH returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C at least partially.

The present invention, the high boiling fraction in the first hydrogenation reaction effluent R10P, it is possible to return the first hydrogenation process R10 circulation cracking, as formed the circulation from sepn process FRAC1, the 2nd kind of mode of operation is:

At sepn process FRAC1, after separation gas, liquid, solid step-down, logistics S1L-VLS obtains being the distilled oil FRAC1-MH of the composition of the hydrocarbon class of 170��260 DEG C primarily of conventional boiling point, and distilled oil FRAC1-MH enters hydrogenation upgrading reaction process R30;

At sepn process FRAC1, after separation step-down, logistics S1L-VLS obtains primarily of the distilled oil FRAC1-VH of conventional boiling point higher than the hydrocarbon component composition of 260 DEG C, and distilled oil FRAC1-VH returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C at least partially.

The present invention, the high boiling fraction in the first hydrogenation reaction effluent R10P, it is possible to return the first hydrogenation process R10 circulation cracking, as formed the circulation from sepn process FRAC1, the third mode of operation is:

(2) at recycling step, containing hot high score gas S1V enters hydrogenation upgrading reaction process R20 primarily of conventional boiling point lower than the logistics S1V-L of the composition of the hydrocarbon class of 180 DEG C, under hydrogen and hydrogenation upgrading catalyzer R20C existence condition, logistics S1V-L occurs hydrogenation upgrading reaction R20R to carry out hydrogenation upgrading reaction, obtains hydrogenation upgrading reaction effluent R20P;

Containing hot high score gas S1V is that the logistics S1V-M of composition of hydrocarbon class of 170��260 DEG C enters hydrogenation upgrading reaction process R30 primarily of conventional boiling point, under hydrogen and hydrogenation upgrading catalyzer R30C existence condition, logistics S1V-M occurs hydrogenation upgrading reaction R30R to carry out hydrogenation upgrading reaction, obtains hydrogenation upgrading reaction effluent R30P;

At sepn process FRAC1, after separation gas, liquid, solid step-down, logistics S1L-VLS obtains primarily of the distilled oil FRAC1-LH of conventional boiling point lower than the composition of the hydrocarbon class of 180 DEG C, and distilled oil FRAC1-MH enters hydrogenation upgrading reaction process R20;

At sepn process FRAC1, after separation gas, liquid, solid step-down, logistics S1L-VLS obtains primarily of the distilled oil FRAC1-VH of conventional boiling point higher than the hydrocarbon component composition of 260 DEG C, and distilled oil FRAC1-VH returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C at least partially.

The present invention, the high boiling fraction in the first hydrogenation reaction effluent R10P, it is possible to return the first hydrogenation process R10 circulation cracking, as formed the circulation from sepn process FRAC1, the 4th kind of mode of operation is:

Containing hot high score gas S1V is that the logistics S1V-M of composition of hydrocarbon class of 170��300 DEG C enters hydrogenation upgrading reaction process R30 primarily of conventional boiling point, under hydrogen and hydrogenation upgrading catalyzer R30C existence condition, logistics S1V-M occurs hydrogenation upgrading reaction R30R to carry out hydrogenation upgrading reaction, obtains hydrogenation upgrading reaction effluent R30P;

At sepn process FRAC1, after separation gas, liquid, solid step-down, logistics S1L-VLS obtains being the distilled oil FRAC1-MH of the composition of the hydrocarbon class of 170��300 DEG C primarily of conventional boiling point, and distilled oil FRAC1-MH enters hydrogenation upgrading reaction process R30;

At sepn process FRAC1, after separation gas, liquid, solid step-down, logistics S1L-VLS obtains primarily of the distilled oil FRAC1-VH of conventional boiling point higher than the hydrocarbon component composition of 300 DEG C, and distilled oil FRAC1-VH returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C at least partially.

The present invention, it is possible to hydrogenation upgrading reaction process R20 is set, it is characterised in that:

(2) at recycling step, hydrogenation upgrading reaction process R20 is set;

Reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate LN2 of conventional boiling point lower than the conventional liquid hydrocarbon composition of 180 DEG C, distillate LN2 enters hydrogenation upgrading reaction process R20 at least partially, under hydrogen and hydrogenation upgrading catalyzer R20C existence condition, carry out hydrogenation upgrading reaction, obtain hydrogenation upgrading reaction effluent R20P.

The present invention, it is possible to arranging thermal high sepn process S10 and hydrogenation upgrading reaction process R20, the first mode of operation is:

(2) at recycling step, thermal high sepn process S10 and hydrogenation upgrading reaction process R20 is set;

At thermal high sepn process S10, first hydrogenation reaction effluent R10P completes high boiling hydrocarbon component and the relative separation of low boiling hydrocarbon component, obtains the oil S1L of the hot high score containing solid ingredient and comprises the gas S10-PV formed primarily of hydrogen on volume of low boiling hydrocarbon component; Substantially containing the conventional liquid hydrocarbon of conventional boiling point lower than 180 DEG C in hot high score oil S1L;

Gas recovery S10-PV, obtains primarily of the distillate LN2 of conventional boiling point lower than the conventional liquid hydrocarbon composition of 180 DEG C, and distillate LN2 enters hydrogenation upgrading reaction process R20 at least partially.

The present invention, it is possible to thermal high sepn process S10 and hydrogenation upgrading reaction process R20 is set, the 2nd kind of mode of operation is:

At thermal high sepn process S10, first hydrogenation reaction effluent R10P completes high boiling hydrocarbon component and the relative separation of low boiling hydrocarbon component, obtains the oil S1L of the hot high score containing solid ingredient and comprises the gas S10-PV formed primarily of hydrogen on volume of low boiling hydrocarbon component; Containing the conventional liquid hydrocarbon of conventional boiling point lower than 180 DEG C in hot high score oil S1L;

At depressurization step 1DPS, carry out the logistics logistics S1L-VLS after step-down equipment obtains step-down containing solid impurity of self-heating high score oil S1L;

Reclaiming logistics S1L-VLS after step-down, obtain primarily of the distillate F-LN1 of conventional boiling point lower than the conventional liquid hydrocarbon composition of 180 DEG C, distillate F-LN2 enters hydrogenation upgrading reaction process R20 at least partially.

(2) at recycling step, primarily of the hydrocarbon feed R20AF that be rich in low carbon number list six-ring hydrocarbon containing impurity of conventional boiling point lower than the conventional liquid hydrocarbon composition of 180 DEG C, enter hydrogenation upgrading reaction process R20 and contact with hydrogenation upgrading catalyzer R20C.

The present invention, it is possible to hydrogenation upgrading reaction process R30 is set, it is characterised in that:

(2) at recycling step, hydrogenation upgrading reaction process R30 is set;

Reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate LN3 that the conventional liquid hydrocarbon that conventional boiling point is 170��260 DEG C forms, distillate LN3 enters hydrogenation upgrading reaction process R30 at least partially, under hydrogen and hydrogenation upgrading catalyzer R30C existence condition, carry out hydrogenation upgrading reaction, obtain hydrogenation upgrading reaction effluent R30P.

The present invention, it is possible to arranging thermal high sepn process S10 and hydrogenation upgrading reaction process R30, the first mode of operation is:

At thermal high sepn process S10, first hydrogenation reaction effluent R10P completes high boiling hydrocarbon component and the relative separation of low boiling hydrocarbon component, obtains the oil S1L of the hot high score containing solid ingredient and comprises the gas S10-PV formed primarily of hydrogen on volume of low boiling hydrocarbon component; In hot high score oil S1L substantially containing conventional boiling point be 170��260 DEG C conventional liquid hydrocarbon;

Gas recovery S10-PV, obtains primarily of the distillate LN3 that the conventional liquid hydrocarbon that conventional boiling point is 170��260 DEG C forms, and distillate LN3 enters hydrogenation upgrading reaction process R30 at least partially.

The present invention, it is possible to thermal high sepn process S10 and hydrogenation upgrading reaction process R30 is set, the 2nd kind of mode of operation is:

At thermal high sepn process S10, first hydrogenation reaction effluent R10P completes high boiling hydrocarbon component and the relative separation of low boiling hydrocarbon component, obtains the oil S1L of the hot high score containing solid ingredient and comprises the gas S10-PV formed primarily of hydrogen on volume of low boiling hydrocarbon component; It hot high score oil S1L is the conventional liquid hydrocarbon of 170��260 DEG C containing conventional boiling point;

Logistics S1L-VLS after recovery step-down, obtains primarily of the distillate F-LN3 that the conventional liquid hydrocarbon that conventional boiling point is 170��260 DEG C forms, and distillate F-LN3 enters hydrogenation upgrading reaction process R30 at least partially.

The present invention, it is possible to arranging thermal high sepn process S10 and hydrogenation upgrading reaction process R30, the third mode of operation is:

(2) at recycling step, hydrogenation upgrading reaction process R30 is set;

It is the hydrocarbon feed R30AF being rich in high-carbon number list six-ring hydrocarbon containing impurity of the conventional liquid hydrocarbon composition of 170��260 DEG C primarily of conventional boiling point, enters hydrogenation upgrading reaction process R30 and contact with hydrogenation upgrading catalyzer R30C.

The present invention, it is possible to arrange hydrogenation upgrading reaction process R30X, combines conventional boiling point in processing the first hydrogenation reaction effluent R10P lower than the conventional liquid hydrocarbon of 260 DEG C, it is characterised in that:

(2) at recycling step, hydrogenation upgrading reaction process R30X is set;

Reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate MN2 of conventional boiling point lower than the conventional liquid hydrocarbon composition of 260 DEG C, distillate MN3 enters hydrogenation upgrading reaction process R30X at least partially, under hydrogen and hydrogenation upgrading catalyzer R30XC existence condition, carry out hydrogenation upgrading reaction, obtain hydrogenation upgrading reaction effluent R30XP.

The present invention, it is possible to arrange hydrogenation upgrading reaction process R30X, combines conventional boiling point in processing the first hydrogenation reaction effluent R10P lower than the conventional liquid hydrocarbon of 260 DEG C, and the first mode of operation is:

(2) at recycling step, thermal high sepn process S10 and hydrogenation upgrading reaction process R30X is set;

At thermal high sepn process S10, first hydrogenation reaction effluent R10P completes high boiling hydrocarbon component and the relative separation of low boiling hydrocarbon component, obtains the oil S1L of the hot high score containing solid ingredient and comprises the gas S10-PV formed primarily of hydrogen on volume of low boiling hydrocarbon component; In hot high score oil S1L substantially containing conventional boiling point lower than 260 DEG C conventional liquid hydrocarbon;

Gas recovery S10-PV, obtains primarily of the distillate MN3 of conventional boiling point lower than the conventional liquid hydrocarbon composition of 260 DEG C, and distillate MN3 enters hydrogenation upgrading reaction process R30X at least partially.

The present invention, it is possible to arrange hydrogenation upgrading reaction process R30X, combines conventional boiling point in processing the first hydrogenation reaction effluent R10P lower than the conventional liquid hydrocarbon of 260 DEG C, and the 2nd kind of mode of operation is:

At thermal high sepn process S10, first hydrogenation reaction effluent R10P completes high boiling hydrocarbon component and the relative separation of low boiling hydrocarbon component, obtains the oil S1L of the hot high score containing solid ingredient and comprises the gas S10-PV formed primarily of hydrogen on volume of low boiling hydrocarbon component; Containing the conventional liquid hydrocarbon of conventional boiling point lower than 260 DEG C in hot high score oil S1L;

Reclaiming logistics S1L-VLS after step-down, obtain primarily of the distillate F-MN3 of conventional boiling point lower than the conventional liquid hydrocarbon composition of 260 DEG C, distillate F-MN3 enters hydrogenation upgrading reaction process R30X at least partially.

The present invention, it is possible to arrange hydrogenation upgrading reaction process R30X, combines conventional boiling point in processing the first hydrogenation reaction effluent R10P lower than the conventional liquid hydrocarbon of 260 DEG C, and the third mode of operation is:

(2) at recycling step, hydrogenation upgrading reaction process R30X is set;

Primarily of the hydrocarbon feed R30XAF that be rich in high-carbon number list six-ring hydrocarbon containing impurity of conventional boiling point lower than the conventional liquid hydrocarbon composition of 260 DEG C, enter hydrogenation upgrading reaction process R30X and contact with hydrogenation upgrading catalyzer R30XC.

The present invention, it is possible to arrange hydrogenation upgrading reaction process R30X, combines conventional boiling point in processing the first hydrogenation reaction effluent R10P lower than the conventional liquid hydrocarbon of 260 DEG C, and the 4th kind of mode of operation is:

(2) at recycling step, temperature high pressure separation process S20 and hydrogenation upgrading reaction process R30X in thermal high sepn process S10, first is set;

At thermal high sepn process S10, first hydrogenation reaction effluent R10P completes high boiling hydrocarbon component and the relative separation of low boiling hydrocarbon component, obtains the oil S1L of the hot high score containing solid ingredient and comprises the gas S10-PV formed primarily of hydrogen on volume of low boiling hydrocarbon component; Gas S10-PV comprises in the first hydrogenation reaction effluent R10P the conventional boiling point of major part lower than the hydrocarbon component of 260 DEG C;

In first temperature high pressure separation process S20, divided gas flow R10P-V obtain primarily of conventional boiling point be the conventional liquid composition of 70��260 DEG C first in temperature high score oil S2L and on volume primarily of temperature high score gas S2V in the first of hydrogen composition;

In separation first, temperature high score gas S2V obtains hydrogen rich gas gas and hydrocarbon ils liquid phase stream, and gained hydrogen rich gas gas goes hydrogenation reaction part to recycle at least partially;

In first, temperature high score oil S2L enters hydrogenation upgrading reaction process R30X as distillate MN2.

The present invention, it is possible to arrange hydrogenation upgrading reaction process R30X, combines conventional boiling point in processing the first hydrogenation reaction effluent R10P lower than the conventional liquid hydrocarbon of 260 DEG C, and the 5th kind of mode of operation is:

At cold anticyclone sepn process S40, separation first in temperature high score gas S2V obtain primarily of hydrocarbon component composition cold high score oil S40L and on volume primarily of hydrogen composition cold high score gas S40V;

Cold high score oil S40L or cold high score oil S40L takes off except conventional boiling point is lower than the cold high score oil S40L-DG of the de-light constituent of gained after the component of 40 DEG C, enters hydrogenation upgrading reaction process R20 as distillate LN2.

The present invention, it is possible to arranging in first temperature high pressure separation process S30, hydrogenation upgrading reaction process R20 and hydrogenation upgrading reaction process R30 in temperature high pressure separation process S20, the 2nd, mode of operation is generally:

(2) at recycling step, temperature high pressure separation process S30, hydrogenation upgrading reaction process R20 and hydrogenation upgrading reaction process R30 in temperature high pressure separation process S20, the 2nd is set in first;

In first temperature high pressure separation process S20, divided gas flow R10P-V obtain primarily of conventional boiling point be the hydrocarbon class composition of 170��260 DEG C first in temperature high score oil S2L and on volume primarily of temperature high score gas S2V in the first of hydrogen composition;

In the 2nd temperature high pressure separation process S30, divided gas flow S2V obtain primarily of conventional boiling point lower than temperature high score oil S3L in the 2nd of the hydrocarbon class composition of 180 DEG C the and on volume primarily of temperature high score gas S3V in the 2nd of hydrogen composition the;

Be separated in the 2nd temperature high score gas S3V obtain hydrogen rich gas gas and hydrocarbon ils liquid phase stream, gained hydrogen rich gas gas goes hydrogenation reaction part to recycle at least partially;

In first, temperature high score oil S2L enters hydrogenation upgrading reaction process R30 as distillate LN3;

In 2nd, temperature high score oil S3L enters hydrogenation upgrading reaction process R20 as distillate LN2;

Usually, from hydrogenation upgrading reaction effluent R20P generation oil, from hydrogenation upgrading reaction effluent R30P generation oil, be separated in the lump after mixing.

The present invention, it is possible to arranging hydrogenation upgrading reaction process R20 and hydrogenation upgrading reaction process R30, mode of operation is:

Reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate LN2 of conventional boiling point lower than the conventional liquid hydrocarbon composition of 180 DEG C, distillate LN2 enters hydrogenation upgrading reaction process R20 at least partially, under hydrogen and hydrogenation upgrading catalyzer R20C existence condition, carry out hydrogenation upgrading reaction, obtain hydrogenation upgrading reaction effluent R20P;

Reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate LN3 that the conventional liquid hydrocarbon that conventional boiling point is 170��260 DEG C forms, distillate LN3 enters hydrogenation upgrading reaction process R30 at least partially, under hydrogen and hydrogenation upgrading catalyzer R30C existence condition, carry out hydrogenation upgrading reaction, obtain hydrogenation upgrading reaction effluent R30P;

The sepn process of hydrogenation upgrading reaction effluent R20P, the sepn process of hydrogenation upgrading reaction effluent R30P, partly or entirely public.

The present invention, the foreign matter content of whole hydrocarbon-fraction in hydrogenation upgrading reaction effluent R20P: being generally nitrogen content lower than 2PPm, sulphur content lower than 2PPm, be generally nitrogen content lower than 1PPm, sulphur content is lower than 1PPm.

The present invention, the foreign matter content of whole hydrocarbon-fraction in hydrogenation upgrading reaction effluent R30P: usually non-nitrogen content lower than 10PPm, sulphur content lower than the cetane value of 10PPm, diesel component higher than 33, be generally nitrogen content lower than 5PPm, sulphur content lower than the cetane value of 5PPm, diesel component higher than 38.

The present invention, it is possible in fractionation, coalite tar obtains different boiling and evaporates point, then combines processing, and the first mode of operation is:

In fractionation, coalite tar obtains primarily of conventional boiling point higher than the hydrocarbon feed R10F of the hydrocarbon component composition of 250 DEG C with primarily of the hydrocarbon feed RL10F of conventional boiling point lower than the hydrocarbon component composition of 250 DEG C.

The present invention, it is possible in fractionation, coalite tar obtains different boiling and evaporates point, then combines processing, and the 2nd kind of mode of operation is:

Fractionating coal tar obtains primarily of conventional boiling point higher than the hydrocarbon feed R10F of the hydrocarbon component composition of 300 DEG C with primarily of the hydrocarbon feed RL10F of conventional boiling point lower than the hydrocarbon component composition of 300 DEG C.

The present invention, it is possible in fractionation, coalite tar obtains different boiling and evaporates point, then combines processing, and the third mode of operation is:

Fractionating coal tar obtains primarily of conventional boiling point higher than the hydrocarbon feed R10F of the hydrocarbon component composition of 350 DEG C with primarily of the hydrocarbon feed RL10F of conventional boiling point lower than the hydrocarbon component composition of 350 DEG C.

The present invention, it is possible to combining coalite tar in processing different boiling and obtain evaporating point, mode of operation is:

(2) at recycling step, unifining process RLK1 and hydrogenation upgrading reaction process R30 is set;

At unifining process RLK10, under hydrogen and Hydrobon catalyst RLK10C existence condition, there is hydrofining reaction RLK10R primarily of conventional boiling point lower than the hydrocarbon feed RLK10F of the hydrocarbon component composition of 260 DEG C, obtain hydrofining reaction effluent RLK10P;

Hydrogenation upgrading reaction process R30 comprises the first hydrogenation upgrading reaction process R301 of the use first hydrogenation upgrading catalyzer R30C1 of serial operation, uses the 2nd hydrogenation upgrading reaction process R302 of the 2nd hydrogenation upgrading catalyzer R30C2; Hydrofining reaction effluent RLK10P enters the 2nd hydrogenation upgrading reaction process R302 and contacts with the 2nd hydrogenation upgrading reaction process R302, and without upstream reaction process i.e. the first hydrogenation upgrading reaction process R301.

The present invention, it is possible to arrange thermal high sepn process S10, carries out the flash vaporization process S1F and air lift process 1HBM of the first hydrogenation reaction effluent R10P in a separation gas stripper S10-TE,

The flash zone, top that first hydrogenation reaction effluent R10P enters separation gas stripper S10-TE is separated into liquid hydrocarbon R10P-L and gas R10P-V; Air lift hydrogen 1BH enters the bottom of separation gas stripper S10-TE; At the lower mass transfer section S10-TE-DCM of separation gas stripper S10-TE, liquid hydrocarbon R10P-L flows downward and carries out at least 1 counter current contact with the air lift hydrogen 1BH upwards flowed and be separated, and obtains hot high score oil S1L and rich oil air lift hydrogen 1BHP; Rich oil air lift hydrogen 1BHP and gas R10P-V is mixed into the top that separation gas stripper overhead gas S10-TE-V discharges separation gas stripper S10-TE;

Separation gas stripper overhead gas S10-TE-V, as gas S10-PV.

The present invention, it is possible to thermal high sepn process S10 and turning oil S1RL is set, the first mode of operation is:

(2) at recycling step, thermal high sepn process S10 is set;

The hot high score oil S1L containing solid impurity at least partially, as turning oil S1RL, returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C.

The present invention, it is possible to thermal high sepn process S10 and turning oil S1RL is set, the 2nd kind of mode of operation is:

(2) at recycling step, thermal high sepn process S10 is set;

Hot high score oil S1L is divided into two-way, and the hot high score oil S1L of the first via returns the first hydrogenation process R10 as turning oil S1RL and contacts with the first hydrogenation catalyst R10C, and the 2nd hot high score oil S1L in tunnel removes depressurization step 1DPS;

The present invention, it is possible to thermal high sepn process S10 and turning oil S1RL is set, the third mode of operation is:

(2) at recycling step, thermal high sepn process S10 is set;

At thermal high sepn process S10, the 2nd hot high score oil S1L in tunnel reclaims after going depressurization step 1DPS step-down, and spent catalyst and other solid impurity are discharged in its effect.

The present invention, it is possible to thermal high sepn process S10 and turning oil S1RL is set, the 4th kind of mode of operation is:

(2) at recycling step, before depressurization step 1DPS, high pressure-off slag filtration procedure F1S is set;

At high pressure-off slag filtration procedure F1S, the hot high score oil S1L containing solid impurity becomes the hot high score oil S1L-DI of de-slag after deviating from solid impurity by strainer, solid impurity contained by hot high score oil S1L is accumulated in strainer flow passage components composition filter residue; The hot high score oil S1L-DI of de-slag removes depressurization step 1DPS;

High pressure-off slag filtration procedure F1S, it may also be useful at least 2 filter F A and filter F B, when filter F A needs regeneration and filter residue is discharged in step-down, high pressure filter FB is in running status, and the de-filter residue process of filter F A regeneration comprises depressurization step 1DPS; At the de-slag step 1DPS-DI of step-down, the first step completes and high pressure isolation of system, the 2nd step-down low slag-accomodating chamber pressure, and the 3rd step crosses the de-filter residue except the accumulation of strainer flow passage components with regeneration filter filter element; 4th step completes boosting; 5th step, drops into again.

The present invention, before depressurization step 1DPS, it is possible to arranging high pressure-off slag filtration procedure F1S, mode of operation is:

At high pressure-off slag filtration procedure F1S, the hot high score oil S1L containing solid impurity becomes the hot high score oil S1L-DI of de-slag after deviating from solid impurity by strainer, solid impurity contained by hot high score oil S1L is accumulated in strainer flow passage components composition filter residue; The hot high score oil S1L-DIR of de-slag returns the first hydrogenation process R10 as turning oil DIRL and contacts with the first hydrogenation catalyst R10C;

At depressurization step 1DPS, solid impurity contained by hot high score oil S1L is accumulated in strainer flow passage components composition filter residue; At high pressure-off slag filtration procedure F1S, it may also be useful at least 2 filter F A and filter F B, when filter F A needs regeneration and filter residue is discharged in step-down, high pressure filter FB is in running status, and the de-filter residue process of filter F A regeneration comprises depressurization step 1DPS; At the de-slag step 1DPS-DI of filter F A step-down, the first step completes and high pressure isolation of system, the 2nd step-down low slag-accomodating chamber pressure, and the 3rd step crosses the de-filter residue except the accumulation of strainer flow passage components with regeneration filter filter element; 4th step completes boosting; 5th step, again drops into and filters working order;

Namely the process of filter residue is deviate from the step-down of above-mentioned strainer is depressurization step 1DPS, and in this process, the filter residue that the solid impurity of the oily S1L of the hot high score containing solid impurity from high pressure conditions and hydrocarbon ils form and portion gas, discharged high pressing system after step-down.

The present invention, it is possible to sepn process FRAC2 and turning oil are set, the first mode of operation is:

(2) at recycling step, reclaim the first hydrogenation reaction effluent R10P, obtain mainly comprising the hydrocarbon stream R10P-DP-M of single six-ring hydrocarbon, logistics R10P-DP-M enters hydrogenation upgrading reaction process RDP, under hydrogen and hydrogenation upgrading catalyzer RDPC existence condition, logistics R10P-DP-M comprises the hydrogenation upgrading reaction RDPR of hydrogenation depth removing impurities matter, obtains hydrogenation upgrading reaction effluent RDPP;

At sepn process FRAC2, separation hydrogenation upgrading reaction effluent RDPP, obtain primarily of single six-ring hydrocarbon composition hydrocarbon stream VGO2 and boiling point is higher and substantially containing the distillate VGO3 of single six-ring hydrocarbon, distillate VGO3 returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C at least partially.

The present invention, it is possible to sepn process FRAC2 and turning oil are set, the 2nd kind of mode of operation is:

(2) at recycling step, at sepn process FRAC2, separation hydrogenation upgrading reaction effluent RDPP, obtain mainly lower than the hydrocarbon composition of 260 DEG C hydrocarbon stream VGO2 and boiling point is higher and substantially containing the distillate VGO3 of single six-ring hydrocarbon, distillate VGO3 returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C at least partially.

The present invention, it is possible to sepn process FRAC2 and turning oil are set, the third mode of operation is:

(2) at recycling step, at sepn process FRAC2, separation hydrogenation upgrading reaction effluent RDPP, obtain mainly lower than the hydrocarbon composition of 300 DEG C hydrocarbon stream VGO2 and boiling point is higher and substantially containing the distillate VGO3 of single six-ring hydrocarbon, distillate VGO3 returns the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C at least partially.

The present invention, it is possible to hydrogenation upgrading reaction process R30, the disconnected side chain reaction process RTC30 of hydrogenation are set:

(2) at recycling step, hydrogenation upgrading reaction process R30, the disconnected side chain reaction process RTC30 of hydrogenation are set;

Reclaim hydrogenation upgrading reaction effluent R30P, obtain comprising the hydrocarbon stream R30P-PF that conventional boiling point is the conventional liquid hydrocarbon of 170��260 DEG C;

At the disconnected side chain reaction process RTC30 of hydrogenation, at hydrogen with under selecting the disconnected side chain hydrocracking catalyst RTC30C existence condition of shape, carry out the disconnected side chain reaction RTC30R of hydrogenation, obtain the disconnected side chain reaction effluent RTC30P of hydrogenation.

The present invention, it is possible to arranging hydrogenation upgrading reaction process R30, the disconnected side chain reaction process RTC30 of hydrogenation, the first mode of operation is:

Hydrogenation upgrading reaction effluent R30P, enters the disconnected side chain reaction process RTC30 of hydrogenation as hydrocarbon stream R30P-PF.

The present invention, it is possible to arranging hydrogenation upgrading reaction process R30, the disconnected side chain reaction process RTC30 of hydrogenation, the 2nd kind of mode of operation is:

At thermal high sepn process S100, hydrogenation upgrading reaction effluent R30P is separated into hot high score oil S100L and comprises the gas S100V formed primarily of hydrogen on volume of low boiling hydrocarbon component; It is the conventional liquid hydrocarbon of 170��260 DEG C that hot high score oil S100L comprises major part in hydrogenation upgrading reaction effluent R30P;

Hot high score oil S100L is used as hydrocarbon stream R30P-PF and enters the disconnected side chain reaction process RTC30 of hydrogenation;

(2) at recycling step, gas recovery S100V, obtains hydrogen rich gas gas and hydrocarbon ils logistics, and hydrogen rich gas gas RH goes hydrogenation process to recycle at least partially.

The present invention, hydrogenation breaks side chain reaction process RTC30, and preferential use selects the disconnected side chain hydrocracking catalyst TCR30C of shape, such as use ZSM-5 molecular sieve, its can be about 0.53nm �� 0.56nm that is 0.53 nanometer �� 0.56 nanometer by a few pore size.

Embodiment

The present invention is below described in detail.

Conventional gas hydrocarbon of the present invention, is the hydrocarbon class of gaseous state under referring to normal condition, comprises methane, ethane, propane, butane.

Conventional liq hydrocarbon of the present invention, refers under normal condition in liquid hydrocarbon class, comprises pentane and the higher hydrocarbon class of boiling point thereof.

High aromatic hydrocarbons hydrocarbon feed R10F of the present invention, it is possible to be a kind of wide fraction height aromatic hydrocarbons, it is also possible to be the high aromatic hydrocarbons of 2 kinds or multiple different boiling ranges; The hydrogenation process that first hydrogenation process R10 of the present invention carries out, it is possible to process a kind of high aromatic hydrocarbons, it is also possible to process the high aromatic hydrocarbons of 2 kinds or multiple different boiling ranges; When first hydrogenation process R10 of the present invention processes the high aromatic hydrocarbons of 2 kinds or multiple different boiling ranges, can be 2 roads or multiple feed, the beds that the raw material do not gone the same way flows through can be identical or different, it can be hydrogenation relation in parallel, can also be first, after enter the relation of serial hydrogenation process of multi-reaction-area respectively, can certainly be that first front-end hydrogenation, then front-end hydrogenation product in parallel combine the relation of rear repeated hydrogenation after converging, it is also possible to be other more complicated syntagmatic.

Hydrocarbon feed R10F is selected from one or more of following materials, and containing the hydrocarbon component of conventional boiling point higher than 450 DEG C:

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

3. coal-tar heavy oil or its distillate;

6. ethylene cracking tar;

Usually, the conventional boiling point in hydrocarbon feed R10F is greater than 50% higher than the weight content of the hydrocarbon component of 250 DEG C, simultaneously containing the hydrocarbon component of conventional boiling point higher than 500 DEG C; Hydrocarbon feed R10F is selected from one or more of following materials:

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

Coal tar of the present invention, refer to the coal tar of the process such as pyrolysis step from pyrolysis of coal or the dry distillation of coal or coal generating gas process or its evaporate point, can be the by product coalite tar of coal generating gas or its evaporate point, can also be coal coking pyrolysis of coal process (comprising semi-coking, middle temperature coking, high-temperature coking process) by product coal tar or its evaporate point, can be the mixing oil of above-mentioned coal tar, it is possible to the extracting oil ratio that to be above-mentioned coal tar obtain through light hydrocarbon solvent extracting is such as diasphaltene coal tar or its distillate.

High-temperature coking belongs to coal high temperature pyrolysis process, and the outlet temperature of pyrolytic process is generally greater than 900 DEG C, usually between 1000��1400 DEG C. Described coal-tar heavy oil refers to that coal high temperature pyrolysis produces coke and/or the thick tar of by product of town gas process production. Coal-tar heavy oil is in primary distillation process, usually following product is produced: the products such as light oil (topping tar), carbolic oil, naphtalene oil, lightweight washing oil, heavy wash oil, lightweight carbolineum, heavy matter carbolineum, pitch, carbolic oil can be separated into crude phenols and dephenolize oil further, and naphtalene oil can be separated into thick naphthalene and de-naphtalene oil further. Coal-tar heavy oil lighting end of the present invention refers to: carbolineum, washing oil, naphtalene oil, de-naphtalene oil, carbolic oil, dephenolize oil, light oil and mixing oil thereof.

Owing to raw coal character and coking or gas-making process condition change all within the specific limits, the character of coal tar also changes within the specific limits. Processing condition and the product requirement of coal tar primary distillation process also change within the specific limits, therefore the character of coal tar lighting end also changes within the specific limits. The character of coal tar lighting end, proportion is generally 0.92��1.25, conventional boiling point is generally 60��500 DEG C and is generally 120��460 DEG C, to be 5��80PPm, sulphur content be usual metal content 0.4��0.8%, nitrogen content is 0.6��1.4%, oxygen level is 0.4��9.0%, usual water-content is 0.2��5.0%, and carbon residue content is generally 0.5��13%.

Middle coalite tar, the foreign metal overwhelming majority concentrates on conventional boiling point higher than 350 DEG C particularly higher than in 450 DEG C evaporate point, and usually taking easy hydrogenolysis metal component iron, calcium, magnesium as main ingredient, normally oil soluble metal compound is such as iron naphthenate, calcium naphthenate etc., these easy hydrogenolysis metal components are that hydrogenolysis can be occurred at necessarily high temperature and hydrogen existence condition fast to be converted into sulfide such as iron sulphide, sulfurated lime, and granular precipitate thing or coprecipitate can be formed, under certain condition, particulate matter particle diameter can be grown up. experiment research and full scale plant running all show, in the hydrogenation process of middle coalite tar, according to being divided into from low to high, following step is realistic to raw material different components temperature of reaction substantially: easily hydrogenolysis metal thermolysis < high reactivity condensed-nuclei aromatics thermal condensation and the rudimentary sulphur compound hydrogenating desulfurization of hydrotreated lube base oil <, organometallic complex catalytic hydrogenolysis, rudimentary organic phenol catalytic deoxidation, polycyclic aromatic hydrocarbons takes off carbon residue, said temperature scope is generally 170��350 DEG C, it is generally 210��330 DEG C, very obvious, this is the temperature of reaction interval of a wide region, lighting end for middle coalite tar should be controlled to the first of differing temps section, 2nd, third step is according to carrying out stage by stage from low to high, it is beneficial to and reduces metallic sulfide formation speed, reduce pyrocondensation compound formation speed, prevent from forming superposition peak value, realize the depth profiles of easy hydrogenolysis metal deposit at beds, improve the controllability of deposition reaction.

According to the present invention, described middle coalite tar passed through the process of filtering solid particulate before being separated usually.

Middle coalite tar of the present invention, usually containing phenolic compound, before entering hydrogenation process, it is possible to extracts phenolic compound such as rudimentary phenol wherein.

The technical process scope of hydrocarbon feed R10F hydro-upgrading process UHP, usually the heat from hydrogenation cracking of hydrocarbon feed R10F is started from, end to obtain hydro-upgrading petroleum naphtha and or the flow process scope of LIGHT DIESEL OIL product, typical hydro-upgrading process UHP comprises the first hydrogenation process R10, first hydrogenation reaction effluent R10P sepn process, hydrogenation grading process R20, hydrogenation grading process R30, the hydrogenation that may exist breaks side chain reaction process RTC30, hydrogenation upgrading generates the fractionation process of oil, the circulation cracking process of heat from hydrogenation cracking tail oil, the circulation cracking process of hydrogenation upgrading tail oil.

Circulation cracking tail of the present invention oil, be commonly referred to as that the heat from hydrogenation cracking for concrete stock oil generates oil, hydrogenation upgrading generate and oil be not suitable as petroleum naphtha or the high boiling hydrocarbon of LIGHT DIESEL OIL component, such as conventional boiling point is higher than the hydrocarbon component of 180 DEG C or 260 DEG C or 300 DEG C. This point, it it is the significant difference that the present invention and middle coalite tar produce the technological method of fine-quality diesel oil component, produce in the technological method of fine-quality diesel oil component at middle coalite tar, described circulation cracking tail oil, be commonly referred to as that the heat from hydrogenation cracking for concrete stock oil generates oil, hydrogenation upgrading generate and oil be not suitable as solar oil or the high boiling hydrocarbon of heavy gas oil component, such as conventional boiling point is higher than the hydrocarbon component of 300 DEG C or 330 DEG C or 360 DEG C.

Hydrogenation grading process of the present invention, it is commonly referred to as the hydrogenation grading process that the heat from hydrogenation cracking for concrete stock oil generates the petroleum naphtha in oil or LIGHT DIESEL OIL component, major objective is the hydrofining reaction of hydrogenation removing impurities matter, because the raw material of processing and conventional boiling point lack 3 rings and polycyclic aromatic hydrocarbons thereof lower than in the hydrocarbon component of 180 DEG C or 260 DEG C or 300 DEG C, the working pressure of its hydrogenation grading process is generally middle low pressure, such as solar oil hydrogenation grading process hydrogen partial pressure is 9.0��12.0MPa, petroleum naphtha hydrogenation grading process hydrogen partial pressure is 3.0��8.0MPa, and matching used Hydrobon catalyst, undesirably it possesses too high aromatic saturation function, but expect to retain more aromatic ring structure, low hydrogen can be consumed on the one hand, the dehydrogenation task of follow-up Naphtha agent reformation process can also be reduced on the other hand. this point, it it is the significant difference that the present invention and middle coalite tar produce the technological method of fine-quality diesel oil component, produce in the technological method of fine-quality diesel oil component at middle coalite tar, described hydrogenation grading process, it is commonly referred to as the hydrogenation grading process that the heat from hydrogenation cracking for concrete stock oil generates the petroleum naphtha in oil and wide cut diesel fuel component, such as conventional boiling point is the hydrogenation upgrading of the hydrocarbon component of 170��350 DEG C, owing to hydrogenation upgraded material containing a large amount of 3 ring structure aromatic hydrocarbons, and ideal product component is height hydrotreated lube base oil, the hydrocracking product of open loop as far as possible, its advanced nitrogen comprised, degree of depth deoxidation, degree of depth aromatic saturation function, it is 13.5��15.0MPa that the working pressure of the hydrogenation grading process of degree of depth open loop is generally high pressure ratio such as hydrogen partial pressure.

The heat from hydrogenation cracking process of hydrocarbon feed R10F of the present invention i.e. the first hydrogenation process R10, it is commonly referred to as the heat from hydrogenation cracking process for concrete stock oil, its major objective is three rings and polynuclear plane aromatic hydrocarbons thermally splitting manufacture order six-ring hydrocarbon, therefore in the matching relationship of catalyzer thermally splitting function and hydrotreated lube base oil function, do not wish that the saturated function of its aromatic hydrogenation is too strong, namely, handling hydrogen pressure need not be too high, certainly suitably high mesohigh condition is maintained to suppress the transmission of thermally splitting free radical under guarantee process continuous cycle of operation prerequisite, suppress the thermal condensation coking reaction of macromole condensed-nuclei aromatics thermally splitting free radical, hydrodemetallation (HDM) and the necessary hydrogen partial pressure of hydrogenation removing impurities matter are provided, the hydrogen partial pressure providing first ring hydrotreated lube base oil of 3 rings or polycyclic aromatic hydrocarbons necessary, maintain the necessary pressurized liquefied condition of hydrocarbon, it is such as 9.0��15.0MPa that the hydrogen partial pressure of the first hydrogenation process R10 is chosen as mesohigh condition usually. this point, it it is the significant difference that the present invention and middle coalite tar produce the technological method of fine-quality diesel oil component, produce in the technological method of fine-quality diesel oil component at middle coalite tar, described heat from hydrogenation cracking process, its major objective is that three rings and polynuclear plane aromatic hydrocarbons are through hydrotreated lube base oil, heat from hydrogenation cracking open loop, the saturated production wide cut diesel fuel of deep hydrogenation, therefore in the matching relationship of catalyzer thermally splitting function and hydrotreated lube base oil function, wish that the saturated function of its aromatic hydrogenation is strong, namely handling hydrogen pressure must be high, being generally high pressure ratio such as hydrogen partial pressure is 15.0��20.0MPa.

Usually in coalite tar lighting end such as conventional boiling point lower than 350 DEG C the olefin(e) centent height evaporated point, phenol content height, gum level height and containing the more component easily reacted when mitigation; therefore; the pre-hydrogenation process of described coal tar lighting end; usually use the single dose of hydrogenation protecting agent, olefins hydrogenation agent, hydrogenation deoxidation agent, removal of ccr by hydrotreating agent, hydrogen desulfurization agent etc. or the series combination of two agent or multi-agent or mixed loading combination, usually use down-flow fixed bed hydrogenator.

Usually in coalite tar last running such as conventional boiling point higher than 350 DEG C and middle coalite tar containing coal-tar pitch evaporate point, its metal content height, gum level height, asphalt content height, containing solid particulate matter, therefore, the heat from hydrogenation cracking process of described coal tar heavy fractioning, , usually upflowing expanded bed such as ebullated bed is used, the hydrogenators such as suspension bed, similar techniques is such as Chinese patent ZL201010217358.1, Chinese patent application CN104593060A, method described by Chinese patent application CN104946306A, so that in fast online replacement reaction zone because of metal deposit and or the raw burnt and hydrogenation catalyst of rapid deactivation, ensure that reactant circulates freely by the beds of reaction zone simultaneously, its catalyzer used, auxiliary agent has developed the catalyzer of diversified complex function, auxiliary agent. described heat from hydrogenation cracking reaction district, beds mode of operation is generally up-flow reactor, be selected from following in a kind or several combinations:

1. suspension bed and slurry bed system;

2. ebullated bed;

3. upflowing moving-bed;

4. upflowing slight expanded-bed.

The characteristic of the present invention is below described in detail.

1. suspension bed and slurry bed system;

2. ebullated bed;

3. upflowing moving-bed;

4. upflowing slight expanded-bed.

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

3. coal-tar heavy oil or its distillate;

6. ethylene cracking tar;

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

(2) at recycling step, unifining process RL10 is set;

(2) at recycling step, hydrogenation upgrading reaction process R20 is set;

(2) at recycling step, hydrogenation upgrading reaction process R30 is set;

(2) at recycling step, hydrogenation upgrading reaction process R30X is set;

Separation gas stripper overhead gas S10-TE-V, as gas S10-PV.

(2) at recycling step, thermal high sepn process S10 is set;

The each several part of the present invention is below described in detail.

The present invention first hydrogenation process R10 of the present invention is below described in detail.

At the first hydrogenation process R10, it is possible to coalite tar or its distillate in processing, such as conventional boiling point is lower than the middle coalite tar distillate of 450 DEG C, or conventional boiling point is higher than whole last running of the middle coalite tar of 350 DEG C.

First hydrogenation process R10 of the present invention, it may also be useful to reactor can be 1 or 2 or multiple stage; The beds mode of operation of the first hydrogenation process R10, it is possible to be any suitable form, is generally upflowing expanded bed reactor, the overall reaction zone of separate unit upflowing expanded bed reactor, it is possible to be considered to be divided into 2 or multiple reaction zone. The control mode of the temperature in of any reaction zone of upflowing expanded bed reactor of the present invention, it is possible to be regulate hydrogen temperature and or flow, it is possible to be regulate oil product temperature and or flow.

The air lift process 1HBM of the thermal high sepn process S10 of the present invention is below described in detail.

Air lift process 1HBM of the present invention, liquid hydrocarbon R10P-L is separated number of times with the counter current contact of air lift hydrogen 1BH: be generally 1��8 time, be generally 2��4 time; The quantity of air lift hydrogen 1BH, according to air lift process 1HBM Component seperation target it needs to be determined that; The working pressure of air lift process 1HBM, slightly lower than the working pressure of the first hydrogenation process R10; The service temperature of air lift process 1HBM, according to air lift process 1HBM Component seperation target it needs to be determined that, be generally 220��400 DEG C, be generally 280��380 DEG C.

The hydrogenation upgrading reaction process R20 of the present invention is below described in detail.

Hydrogenation upgrading reaction process R20, it may also be useful to reactor can be 1 or 2 or multiple stage; Hydrogenation grading process R20 beds mode of operation, it is possible to be any suitable form, it is possible to be the combination of two or more dissimilar reactors, it is possible to be fixed-bed reactor, it is possible to be fluidized-bed reactor; Fluidized-bed reactor, it is possible to be suspension bed, it is possible to be ebullated bed; Can be downflow reactor, it is also possible to be up-flow reactor. The reactor that hydrogenation upgrading reaction process R20 uses, its beds mode of operation is generally down-flow fixed bed. During hydrogenation upgrading reaction process R20 use fixed bed catalyst bed, it is possible to be 1,2 or multiple bed. Of the present invention the 2nd of hydrogenation upgrading reaction process R20 and the control mode of the temperature in of follow-up beds, it is possible to be use cold hydrogen and or cold oil.

Hydrogenation upgrading reaction process R20, the hydrogenation upgrading catalyzer R20C used, can be that the series combination of the hydrogenation upgrading catalyzer of 1,2 or multiple kind uses, along the flow direction of reaction logistics, the hydrogenation activity of downstream hydrogenation upgrading catalyzer, is generally equal to or higher than the hydrogenation activity of upstream hydrogenation upgrading catalyzer.

Hydrogenation upgrading reaction process R20, the reactor used, the volume ratio of liquid phase, gas phase (or vapour phase) in its beds, it can be the situation based on liquid phase, in definition hydrogenation upgrading beds, " liquid phase actual volume/(liquid phase actual volume+gas phase actual volume) " is bed liquid phase fraction KL, point rate KL can be greater than 0.75, even be greater than 0.95, form liquid-phase hydrogenatin pattern in fact, in order to keep the hydrogen partial pressure in hydrogenation upgrading beds enough high, it may be necessary to the entrance at each upgrading beds adds hydrogen.

The hydrogenation upgrading reaction process R30 of the present invention is below described in detail.

Hydrogenation upgrading reaction process R30, it may also be useful to reactor can be 1 or 2 or multiple stage; Hydrogenation upgrading reaction process R30 beds mode of operation, it is possible to be any suitable form, it is possible to be the combination of two or more dissimilar reactors, it is possible to be fixed-bed reactor, it is possible to be fluidized-bed reactor; Fluidized-bed reactor, it is possible to be suspension bed, it is possible to be ebullated bed; Can be downflow reactor, it is also possible to be up-flow reactor. The reactor that hydrogenation upgrading reaction process R30 uses, its beds mode of operation is generally down-flow fixed bed. During hydrogenation upgrading reaction process R30 use fixed bed catalyst bed, it is possible to be 1,2 or multiple bed. The 2nd of hydrogenation upgrading reaction process R30 and the control mode of the temperature in of follow-up beds, it is possible to be use cold hydrogen and or cold oil.

Hydrogenation upgrading reaction process R30, the hydrogenation upgrading catalyzer R30C used, can be that the series combination of the hydrogenation upgrading catalyzer of 1,2 or multiple kind uses, along the flow direction of reaction logistics, the hydrogenation activity of downstream hydrogenation upgrading catalyzer, is generally equal to or higher than the hydrogenation activity of upstream hydrogenation upgrading catalyzer.

Hydrogenation upgrading reaction process R30, the reactor used, the volume ratio of liquid phase, gas phase (or vapour phase) in its beds, it can be the situation based on liquid phase, in definition hydrogenation upgrading beds, " liquid phase actual volume/(liquid phase actual volume+gas phase actual volume) " is bed liquid phase fraction KL, point rate KL can be greater than 0.75, even be greater than 0.95, form liquid-phase hydrogenatin pattern in fact, in order to keep the hydrogen partial pressure in hydrogenation upgrading beds enough high, it may be necessary to the entrance at each upgrading beds adds hydrogen.

The disconnected side chain reaction process RTC30 of hydrogenation of the present invention is below described in detail.

Hydrogenation of the present invention breaks side chain reaction process RTC30, what use selects the disconnected side chain hydrocracking catalyst RTC30C of shape, usually catalyst for refining bed RTC30-DC after arranging after last hydrocracking catalyst bed, the mercaptan, the alkene that are produced by hydrocracking process carry out mercaptan hydrogenating desulfurization, olefins hydrogenation prevents hydrocracking product organic sulfur content from exceeding standard; For hydrocracking catalyst RTC30C, heat scission reaction is suppressed to improve liquid oil receipts rate in order to reduce its coking speed extending catalyst life-span, reduce its average reaction temperature, can arrange before the most front hydrocracking catalyst bed preposition Hydrobon catalyst bed RTC30C-UC carry out hydrodenitrification reaction and or hydrogenation aromatic saturation reaction, owing to this preposition unifining process carries out under extremely low vapor phase ammonia content environment, thus the hydrodenitrification of its per volume of catalyst reaction and or hydrogenation aromatic saturation reaction efficiency higher.

Hydrogenation of the present invention breaks side chain reaction process RTC30, what use selects the disconnected side chain hydrocracking catalyst RTC30C of shape, can be that the series combination of the hydrocracking catalyst of 1,2 or multiple kind uses, along the flow direction of reaction logistics, the hydrogenation activity of downstream hydrogenation cracking catalyst, is generally equal to or higher than the hydrogenation activity of upstream hydrocracking catalyst.

At the disconnected side chain reaction process RTC30 of hydrogenation, select the disconnected side chain hydrocracking catalyst TCR30C of shape, it is desirable to use ZSM-5 molecular sieve, its can be about 0.53nm �� 0.56nm that is 0.53 nanometer �� 0.56 nanometer by a few pore size.

Select the disconnected side chain hydrocracking catalyst TCR30C of shape, can be that the disconnected side chain hydrocracking catalyst of shape selected by any one suitable diesel oil, can be that typical petroleum based diesel selects the disconnected side chain hydrocracking catalyst of shape, these technology have the development technique etc. of technology that China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute develops, Beijing Research Institute of Petro-Chemical Engineering of limited-liability company of Sinopec, the document recording this kind of technology is shown in: 1. publication title: " hydroprocessing technique and engineering ", 390 pages extremely, 408 pages; 2. retrieval books encode: ISBN encodes: 7-80164-665-7; China's version Library CIP data core word: (2004) No. 128349; 3. edit: Li Dadong; 4. press: petrochemical industry press of China.

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

As required, any one supplementary sulphur can be added arbitrary hydrogenation process, but normally join the hydrogenation process entrance of most upstream, to ensure minimum concentration of hydrogen sulfide such as 500PPm (v) or 1000PPm (v) that reaction process is necessary or prescribed value, to ensure that the necessary hydrogen sulfide sectional pressure of catalyzer is not less than minimum prescribed value. Described supplementary sulphur can be sulfide hydrogen maybe can be converted into hydrogen sulfide to the material of hydroconversion process without undesirable action, such as hydrogen sulfide containing gas or oil product, or after contacting, generate the dithiocarbonic anhydride or Methyl disulfide etc. of hydrogen sulfide with high-temperature hydrogen. When the dilution hydrocarbon of pre-hydrotreating reaction process R1 provides with hydrogen sulfide containing hydrogenation reaction effluent form, if hydrogen sulfide quantity wherein meets the needs of pre-hydrotreating reaction process R1, it is possible to do not re-use sulfur supplementary agent.

The general principle of the high pressure separation process of the hydrogenation reaction effluent of the present invention is below described in detail.

The high pressure separation process of hydrogenation reaction effluent comprises cold high pressure separator usually, when hydrocarbon ils density in hydrogenation reaction effluent big (such as close with water-mass density) or viscosity is big or when being difficult to be separated with emulsifying water, setting operation temperature is also needed to be generally the high pressure hot separator of 150��450 DEG C, now hydrogenation reaction effluent enter high pressure hot separator be separated into one on volume primarily of hydrogen composition hot high score gas gas and one primarily of conventional liq hydrocarbon and may exist solid composition hot high score fluid body, hot high score gas enters the cold high pressure separator that service temperature is generally 20��80 DEG C and is separated into cold high score oil and cold high score gas, owing to a large amount of high boiling component enters in hot high score fluid body, achieve following target: cold high score oil density diminishes or viscosity diminishes or is easy to be separated with water. the high pressure separation process of hydrogenation reaction effluent arranges high pressure hot separator, also possesses the advantage reducing calorific loss, because hot high score fluid body can avoid the process that cools of use air cooler that hot high score gas experiences or water cooler. simultaneously, it is possible to recycled by the hydrogenation process that hot for part high score fluid body returns to upstream, to improve the overall raw material character of the hydrogenation process receiving this turning oil, or this turning oil is carried out circulation hydrogenation.

Before hydrogenation reaction effluent or hot high score gas enter cold anticyclone separate section, usually temperature (being generally and reactive moieties charging heat exchange) is first reduced to about 220��100 DEG C (these temperature should higher than sulphur hydrogenation ammonia Tc in this hydrogenation reaction effluent gas phase), then usually inject washing water wherein and form water filling back end hydrogenation reaction effluent, washing water are used for absorbing ammonia and other impurity that may produce such as hydrogenchloride etc., and the inevitable absorbing hydrogen sulphide of the aqueous solution after absorbing ammonia. In cold anticyclone separate section, described water filling back end hydrogenation reaction effluent is separated into: one on volume primarily of the cold high score gas of hydrogen composition, cold high score oil primarily of conventional liq hydrocarbon and dissolved hydrogen composition, one primarily of water composition and be dissolved with the cold high score water of ammonia, hydrogen sulfide. Described cold high score water, wherein the content of ammonia is generally 0.5��15% (w), is preferably 1��8% (w). An object of note washing water is the ammonia and hydrogen sulfide that absorb in hydrogenation reaction effluent, prevents from forming sulphur hydrogenation ammonia or many sulphur ammonia crystallization blocking heat exchanger channel, increases system pressure drop. The injection rate of described washing water, should determine according to following principle: on the one hand, and washing water are divided into vapour phase water and liquid phase water after injecting hydrogenation reaction effluent, and the liquid phase water yield must be greater than zero, be preferably washing water total amount 30% or more; Another further aspect, the ammonia of washing water for absorbing in hydrogenation reaction effluent, prevents the ammonia density of high score gas too high, reduce catalyst activity, the ammonia volumetric concentration of usual high score gas is more low more good, is generally not more than 200PPm (v), is preferably not more than 50PPm (v). Described cold high pressure separator working pressure is that hydrogenation reaction part pressure subtracts true pressure and falls, and the difference of cold anticyclone separate section working pressure and hydrogenation reaction pressure is unsuitable too low or too high, is generally 0.35��3.2MPa, is generally 0.5��1.5MPa. The hydrogen volume concentration value of described cold high score gas, should not too low (causing device working pressure to rise), generally should be not less than 70% (v), 80% (v) should be not less than, preferably be not less than 85% (v). As previously mentioned at least partially, the cold high score gas that is generally 85��100% return and recycle in hydrogenation reaction part, with the amounts of hydrogen that provides hydrogenation reaction part necessary and hydrogen concentration; In order to improve plant investment efficiency, it is necessary to ensure that recycle hydrogen concentration is not less than aforesaid low limit value, for this reason, according to concrete feedstock property, reaction conditions, product slates, it is possible to get rid of the described cold high score gas of a part to get rid of methane, the ethane of reaction generation. For the cold high score gas of discharge, it is possible to adopt conventional membrane separation process or pressure swing adsorption technique or oil to wash technique and realize hydrogen and non-hydrogen gas Component seperation, and the hydrogen reclaimed is used as new hydrogen.

New hydrogen enters the hydrogen adding hydrogen partial and consuming with supplementary hydrogenation process, and new hydrogen hydrogen concentration is more high more good, generally lower than 95% (v), preferably should not be not less than 99% (v). All new hydrogen can be introduced arbitrary hydrogenation reaction part, preferably introduce pre-hydrotreating reaction process R1.

Major advantage of the present invention is:

1. middle coalite tar production low carbon number list six-ring hydrocarbon is opened and the approach of final production benzene hydrocarbon, it is achieved that " polynuclear plane aromatic hydrocarbons prepares single ring architecture hydrocarbon ";

2. same set of device, by adjustment operation condition, it is possible to takes into account scheme running by maximum fine-quality diesel oil scheme or maximum petroleum naphtha scheme or petroleum naphtha and solar oil, strengthens the adaptive faculty to market.

Embodiment

Embodiment one

Coal-tar middle oil, character is in table 4, table 5, table 6.

Table 4 is for entirely evaporating a point coal-tar middle oil, fraction A (coal-tar middle oil light oil), fraction B (coal-tar middle oil heavy oil) analytical data, what table 5 was coal-tar middle oil evaporates a point C (coal-tar pitch) analytical data, and table 6 is coal-tar middle oil distillation fraction receipts rate table.

As can be seen from Table 5, the feature of fraction B (coal-tar middle oil heavy oil) is content of heteroatoms height, hydrogen richness is low, density is big, aromatic hydrocarbons, gum level are 83.5%, molecular association complex is belonged in a large number and non covalent bond due to the colloid in coal-tar middle oil, the structure of these colloids is very easily disintegrated, and its carbon residue content can not be analyzed by the concept equivalence of black petroleum products.

As can be seen from Table 5, the feature evaporating a point C (coal-tar pitch) is that content of heteroatoms height, hydrogen richness are extremely low, aromatic hydrocarbons, colloid, bituminous matter, insolubles are up to 99.34%, carbon residue 37.8%, the non covalent bond owing to the gum asphalt in coal-tar middle oil belongs to molecular association complex in a large number, the structure of these gum asphalts is very easily disintegrated, and its carbon residue content can not be analyzed by the concept equivalence of black petroleum products, its coking test shows, coking yield is 64��68%.

Table 7 is the first hydrogenation process (heat from hydrogenation cracking process) R10 reaction conditions.

Table 8 is the first hydrogenation process (heat from hydrogenation cracking process) R10 product slates.

" hydrocarbon stream of a kind of self-contained heavy oil is produced the method for lightweight oil " that the CN104498076A adopting the present inventor to propose records, it is filtered, dewaters, the degree of depth distillation, it is about 5% deviate from primarily of the heavy matter coal-tar pitch (accounting for coal-tar middle oil) of conventional boiling point higher than the component composition of 530 DEG C by receipts rate, as solid bitumen product, finally pulverize this solid bitumen and mix mixed in coal burning. Oily lower than the coal tar distillation of the multichannel different boiling ranges of the component composition of 530 DEG C primarily of conventional boiling point, as the base stocks of the present embodiment.

The fraction section that molecular structure is different, arranges different hydrogenation approach.

It is the fraction section of 350��530 DEG C to conventional boiling point, carries out floating bed hydrogenation thermally splitting process, taking fecund low carbon number list six-ring hydrocarbon as target; Floating bed hydrogenation hot cracking catalyst, for oil-soluble molybdenum nickel bimetal catalyzer (Mo and Ni mass ratio is 3: 2), concrete active ingredient is molybdenum dialkyldithiocarbamacompositions (MoDTC), molybdenum dialkyl-dithiophosphate (MoDDP), organic acid molybdenum, organic acid nickel; Auxiliary agent is Sodium dodecylbenzene sulfonate (SDBS), cetyl trimethylammonium bromide (CTAB), oleic acid (OA).

Embodiment two

Based on embodiment one, it is that the solar oil of 180��260 DEG C is for target product by petroleum naphtha, the conventional boiling range of 50��180 DEG C of conventional boiling range, the conventional boiling range of another output about 5% is the wax slop of 450��540 DEG C, all the other conventional boiling points all enter the first hydrogenation process R10 cycling hot cracking higher than the heat from hydrogenation cracking generation oil of 260 DEG C, reactive moieties operational condition is constant, and the overall operation product yield of the first hydrogenation process R10 is in table 9. Table 9 is the first hydrogenation process R10 product slates of embodiment two.

Embodiment three

Based on embodiment one, taking conventional boiling range as the petroleum naphtha of 50��180 DEG C for target product, the conventional boiling range of another output about 5% is the wax slop of 450��540 DEG C, all the other conventional boiling points all enter the first hydrogenation process R10 cycling hot cracking higher than the heat from hydrogenation cracking generation oil of 180 DEG C, reactive moieties operational condition is constant, and the overall operation product yield of the first hydrogenation process R10 is in table 10. Table 10 is the first hydrogenation process R10 product slates of embodiment three.

In order to obtain petroleum naphtha to greatest extent, it is possible to liquefied gas product is produced petroleum naphtha ZN through aromatization process and is finally used as reformer raw material petroleum naphtha.

Embodiment four

Based on embodiment two, at recycling step, temperature high pressure separation process S20 and hydrogenation upgrading reaction process R30X in thermal high sepn process S10, first is set;

This scheme is suitable for filling the situation of small scale, it is possible to reduce construction investment to greatest extent.

Embodiment five

Based on embodiment two, hydrogenation upgrading reaction process R20, hydrogenation upgrading reaction process R30 are set;

This scheme is suitable for the big situation of dress scale, it is possible to optimize hydrogenation upgrading reaction process R20 operational condition to greatest extent.

Embodiment six

Based on embodiment five, it is arranged in series after hydrogenation upgrading reaction process R30 and selects type hydrocracking reaction process R90, the list six-ring hydrocarbon of production low carbon number to greatest extent.

Table 4 evaporates a point coal-tar middle oil, fraction A, fraction B analytical data entirely

Table 5 coal-tar middle oil evaporate a point C analytical data

Sequence number	Project	Evaporate a point C
			1	Sulphur, %	0.40
2	Nitrogen, %	0.8519
			3	C/H, %	89.1/5.90
4	Carbon residue, %	37.8
			5	Softening temperature (ring and ball method)/DEG C	106
6	Degree of prolonging (25 DEG C)/cm	0
			7	Penetration degree (25 DEG C)/mm	3
8	Four composition, %
			9	Bituminous matter	44.04
10	Fragrance point	7.03
			11	Saturated point	0.66
12	Colloid	14.82
			13	Insolubles	33.45

Table 6 coal-tar middle oil distillation fraction receipts rate table

Sequence number	Fraction section	Evaporate point, DEG C	Receipts rate, %
				1	Water	Water	4.22
2	Fraction A	< 310 DEG C	36.10
				3	Fraction B	310 DEG C��500 DEG C	47.65
4	Evaporate a point C	> 500 DEG C	12.03
				5		Add up to	100.00

Table 7 first hydrogenation process (heat from hydrogenation cracking process) R10 reaction conditions

Project	Data
		The total pressure of reaction, MPa	13.8
Reaction hydrogen partial pressure, MPa	Minimum 10.0
		Average reaction temperature, DEG C	425��430
Hydrogen to oil volume ratio	600��700
		Heat from hydrogenation cracking catalyst	Oil-soluble molybdenum nickel bimetal catalyzer
Heat from hydrogenation cracking catalyst consumption, in metal, to fresh feed weight of oil, PPm	150
		Auxiliary agent	Sodium dodecylbenzene sulfonate
Auxiliary dosage, to fresh feed weight of oil, PPm	180��220
		Vulcanizing agent	Sulphur powder
Vulcanizing agent consumption, to fresh feed weight of oil, PPm	370��430
		Reaction velocity, h^-1	0.9��1.0

Table 8 first hydrogenation process (heat from hydrogenation cracking process) R10 product slates

Sequence number	Material title	% weight, based on raw material R10F

1	Charging side
			1.1	Hydrogen	4.82%
1.2	Raw material R10F	100.00%
			1.3	Add up to	104.82%

			2	Discharging side
2.1	Water	6.40%
			2.2	Gas	2.53%
2.3	Petroleum naphtha	20.02%
			2.4	Diesel oil 1	17.68%
2.5	Diesel oil 2	17.72%
			2.6	Wax oil	31.48%
2.7	Residual oil	7.85%
			2.8	Wall is mutually burnt	0.05%
2.9	Liquid phase is burnt	1.10%
			2.10	Add up to	104.82%

First hydrogenation process R10 product slates of table 9 embodiment two

Sequence number	Material title	% weight, based on raw material R10F
			1	Petroleum naphtha	41.66%
2	Diesel oil 1	41.93%
			3	Diesel oil 2
4	Wax oil
			5	Residual oil	7.85%
6	Wall is mutually burnt	0.05%
			7	Liquid phase is burnt	1.10%

First hydrogenation process R10 product slates of table 10 embodiment three

Claims

1. the heat from hydrogenation cracking method of a high aromatic hydrocarbons product low carbon number list six-ring hydrocarbon, it is characterised in that comprise following step:

2. method according to claim 1, it is characterised in that:

(2) at recycling step, reclaim the first hydrogenation reaction effluent R10P to obtain comprising the logistics that the first hydrogenation generates oil, at least partially conventional boiling point be 180��250 DEG C the first hydrogenation generate oil hydrocarbon, return the first hydrogenation process R10 and contact with the first hydrogenation catalyst R10C.

3. method according to claim 1, it is characterised in that:

(2) at recycling step, reclaim the first hydrogenation reaction effluent R10P, obtain primarily of the distillate LN3 that the hydrocarbon component that conventional boiling point is 170��260 DEG C forms.

4. method according to claim 1, it is characterised in that:

(1) first hydrogenation process R10, it may also be useful at least one heat from hydrogenation cracking reaction district, beds mode of operation is up-flow reactor, be selected from following in a kind or several combinations:

1. suspension bed and slurry bed system;

2. ebullated bed;

3. upflowing moving-bed;

4. upflowing slight expanded-bed.

5. method according to claim 1 or 2 or 3 or 4, it is characterised in that:

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

3. coal-tar heavy oil or its distillate;

6. ethylene cracking tar;

6. method according to claim 1 or 2 or 3 or 4, it is characterised in that:

Conventional boiling point in hydrocarbon feed R10F is greater than 50% higher than the weight content of the hydrocarbon component of 250 DEG C, simultaneously containing the hydrocarbon component of conventional boiling point higher than 500 DEG C; Hydrocarbon feed R10F is selected from one or more of following materials:

1. coalite tar or its distillate;

2. coal-tar middle oil or its distillate;

7. method according to claim 6, it is characterised in that:

(1) it is 20��65% at the heat from hydrogenation cracking conversion rate KY of the first hydrogenation process R10, hydrocarbon feed R10F;

8. method according to claim 6, it is characterised in that:

(1) at the first hydrogenation process R10, hydrocarbon feed R10F heat from hydrogenation cracking conversion rate KY is 30��45%.

9. method according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, the part by weight that conventional boiling point is the hydrocarbon component R10P-N of 70��180 DEG C is 20��90%.

10. method according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, conventional boiling point be the hydrocarbon component R10P-N of 70��180 DEG C part by weight be 30��80%.

11. methods according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, conventional boiling point be the hydrocarbon component R10P-N of 70��180 DEG C part by weight be 40��70%.

12. methods according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, conventional boiling point be the hydrocarbon component R10P-N of 70��180 DEG C part by weight be not less than 30%.

13. methods according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, conventional boiling point be the hydrocarbon component R10P-N of 70��180 DEG C part by weight be not less than 40%.

14. methods according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, conventional boiling point be the hydrocarbon component R10P-N of 70��180 DEG C part by weight be not less than 50%.

15. methods according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, the part by weight that conventional boiling point is the hydrocarbon component R10P-N of 70��260 DEG C is not less than 60%.

16. methods according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, in the conventional liquid hydrocarbon of the first hydrogenation reaction effluent R10P, the part by weight that conventional boiling point is the hydrocarbon component R10P-N of 70��260 DEG C is not less than 70%.

17. methods according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, in the first hydrogenation reaction effluent R10P in conventional liquid hydrocarbon, the part by weight that conventional boiling point is the hydrocarbon component R10P-N of 70��260 DEG C is not less than 75%.

18. methods according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, adopts floating bed hydrogenation, and operational condition is: temperature of reaction is 320��480 DEG C, reaction pressure 6��25MPa, volume space velocity 0.2��5.0h^-1, hydrogen to oil volume ratio 200��3000.

19. methods according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, adopts floating bed hydrogenation, and operational condition is: temperature of reaction is 360��480 DEG C, reaction pressure 8��18MPa, volume space velocity 0.2��5.0h^-1, hydrogen to oil volume ratio 200��1500.

20. methods according to claim 6, it is characterised in that:

(1) first hydrogenation process R10, adopts boiling bed hydrogenation, and operational condition is: temperature of reaction is 320��480 DEG C, reaction pressure 6��25MPa, volume space velocity 0.2��5.0h^-1, hydrogen to oil volume ratio 200��3000.

21. methods according to claim 6, it is characterised in that:

22. methods according to claim 6, it is characterised in that:

23. methods according to claim 6, it is characterised in that:

24. methods according to claim 6, it is characterised in that:

25. methods according to claim 6, it is characterised in that:

(2) at recycling step, reclaiming the first hydrogenation reaction effluent R10P, obtain primarily of the distillate DO of conventional boiling point higher than the hydrocarbon component composition of 530 DEG C, distillate DO does not return the first hydrogenation process R10.

26. methods according to claim 6, it is characterised in that:

27. method according to claim 6, it is characterised in that:

28. methods according to claim 6, it is characterised in that:

29. methods according to claim 6, it is characterised in that:

(2) at recycling step, unifining process RL10 is set;

30. methods according to claim 6, it is characterised in that:

31. methods according to claim 6, it is characterised in that:

(2) at recycling step, arranging thermal high sepn process S10, its mode of operation is as follows:

32. according to method described in claim 31, it is characterised in that:

33. methods according to claim 6, it is characterised in that:

(2) at recycling step, arranging thermal high sepn process S10 and depressurization step 1DPS, its mode of operation is as follows:

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

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

36. according to method described in claim 33, it is characterised in that:

(2) at recycling step, reclaim the effluent stream of thermal high sepn process S10 and the effluent stream of depressurization step 1DPS, obtain primarily of the distillate VGO2 of conventional boiling point higher than the hydrocarbon component composition of 180 DEG C, distillate VGO2 goes the 3rd unifining process R3X to contact with the 3rd hydrogenation catalyst R3XC at least partially, obtains the 3rd hydrofining reaction effluent R3XP; 3rd hydrofining reaction effluent R3XP enters the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C.

37. according to method described in claim 33, it is characterised in that:

(2) at recycling step, reclaim the effluent stream of thermal high sepn process S10 and the effluent stream of depressurization step 1DPS, obtain primarily of the distillate VGO2 of conventional boiling point higher than the hydrocarbon component composition of 260 DEG C, distillate VGO2 goes the 3rd unifining process R3X to contact with the 3rd hydrogenation catalyst R3XC at least partially, obtains the 3rd hydrofining reaction effluent R3XP; 3rd hydrofining reaction effluent R3XP enters the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C.

38. according to method described in claim 33, it is characterised in that:

(2) at recycling step, reclaim the effluent stream of thermal high sepn process S10 and the effluent stream of depressurization step 1DPS, obtain primarily of the distillate VGO2 of conventional boiling point higher than the hydrocarbon component composition of 300 DEG C, distillate VGO2 goes the 3rd unifining process R3X to contact with the 3rd hydrogenation catalyst R3XC at least partially, obtains the 3rd hydrofining reaction effluent R3XP; 3rd hydrofining reaction effluent R3XP enters the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C.

39. methods according to claim 4, it is characterised in that:

(2) at recycling step, reclaim the effluent stream of thermal high sepn process S10 and the effluent stream of depressurization step 1DPS, obtain primarily of the distillate VGO2 of conventional boiling point higher than the hydrocarbon component composition of 330 DEG C, distillate VGO2 goes the 3rd unifining process R3X to contact with the 3rd hydrogenation catalyst R3XC at least partially, obtains the 3rd hydrofining reaction effluent R3XP; 3rd hydrofining reaction effluent R3XP enters the first hydrogenation process R10 and contacts with the first hydrogenation catalyst R10C.

40. according to method described in claim 33, it is characterised in that:

41. according to method described in claim 40, it is characterised in that:

42. according to method described in claim 40, it is characterised in that:

43. according to method described in claim 42, it is characterised in that:

44. methods according to claim 6, it is characterised in that:

(2) at recycling step, hydrogenation upgrading reaction process R20 is set;

45. according to method described in claim 44, it is characterised in that:

46. according to method described in claim 44, it is characterised in that:

Gas recovery S10-PV, obtains primarily of the distillate LN2 of conventional boiling point lower than the conventional liquid hydrocarbon composition of 180 DEG C, and distillate LN2 enters hydrogenation upgrading reaction process R20 at least partially;

47. according to method described in claim 44, it is characterised in that:

48. methods according to claim 6, it is characterised in that:

(2) at recycling step, hydrogenation upgrading reaction process R30 is set;

49. according to method described in claim 48, it is characterised in that:

50. according to method described in claim 48, it is characterised in that:

Gas recovery S10-PV, obtains primarily of the distillate LN3 that the conventional liquid hydrocarbon that conventional boiling point is 170��260 DEG C forms, and distillate LN3 enters hydrogenation upgrading reaction process R30 at least partially;

51. according to method described in claim 48, it is characterised in that:

(2) at recycling step, hydrogenation upgrading reaction process R30 is set;

52. methods according to claim 6, it is characterised in that:

(2) at recycling step, hydrogenation upgrading reaction process R30X is set;

53. according to method described in claim 52, it is characterised in that:

54. according to method described in claim 52, it is characterised in that:

Gas recovery S10-PV, obtains primarily of the distillate MN3 of conventional boiling point lower than the conventional liquid hydrocarbon composition of 260 DEG C, and distillate MN3 enters hydrogenation upgrading reaction process R30X at least partially;

55. according to method described in claim 52, it is characterised in that:

(2) at recycling step, hydrogenation upgrading reaction process R30X is set;

56. methods according to claim 6, it is characterised in that:

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

Cold high score oil S40L enters hydrogenation upgrading reaction process R20 as distillate LN2.

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

Cold high score oil S40L takes off except conventional boiling point is lower than the cold high score oil S40L-DG of the de-light constituent of gained after the component of 40 DEG C, enters hydrogenation upgrading reaction process R20 as distillate LN2.

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

In 2nd, temperature high score oil S3L enters hydrogenation upgrading reaction process R20 as distillate LN2.

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

(2) at recycling step, from hydrogenation upgrading reaction effluent R20P generation oil, from hydrogenation upgrading reaction effluent R30P generation oil, be separated in the lump after mixing.

61. methods according to claim 6, it is characterised in that:

(2) at recycling step, hydrogenation upgrading reaction process R20 and hydrogenation upgrading reaction process R30 is set;

62. according to method described in claim 44, it is characterised in that:

(2) at recycling step, in hydrogenation upgrading reaction effluent R20P, the nitrogen content of whole hydrocarbon-fraction is lower than 2PPm, and sulphur content is lower than 2PPm.

63. according to method described in claim 44, it is characterised in that:

(2) at recycling step, in hydrogenation upgrading reaction effluent R20P, the nitrogen content of whole hydrocarbon-fraction is lower than 1PPm, and sulphur content is lower than 1PPm.

64. according to method described in claim 48, it is characterised in that:

(2) at recycling step, the nitrogen content of the whole hydrocarbon-fractions in hydrogenation upgrading reaction effluent R30P lower than 10PPm, sulphur content lower than the cetane value of 10PPm, diesel component higher than 33.

65. according to method described in claim 48, it is characterised in that:

(2) at recycling step, the nitrogen content of the whole hydrocarbon-fractions in hydrogenation upgrading reaction effluent R30P lower than 5PPm, sulphur content lower than the cetane value of 5PPm, diesel component higher than 38.

66. according to method described in claim 29, it is characterised in that:

67. according to method described in claim 29, it is characterised in that:

68. according to method described in claim 29, it is characterised in that:

69. methods according to claim 6, it is characterised in that:

70. methods according to claim 6, it is characterised in that:

(2) at recycling step, thermal high sepn process S10 is set, in a separation gas stripper S10-TE, carries out the flash vaporization process S1F and air lift process 1HBM of the first hydrogenation reaction effluent R10P;

Separation gas stripper overhead gas S10-TE-V, as gas S10-PV.

71. methods according to claim 6, it is characterised in that:

(2) at recycling step, thermal high sepn process S10 is set;

72. methods according to claim 6, it is characterised in that:

(2) at recycling step, thermal high sepn process S10 is set;

73. according to method described in claim 72, it is characterised in that:

(2) at recycling step, thermal high sepn process S10 is set;

74. according to method described in claim 72, it is characterised in that:

75. according to method described in claim 74, it is characterised in that:

76. methods according to claim 6, it is characterised in that:

77. according to method described in claim 76, it is characterised in that:

78. according to method described in claim 76, it is characterised in that:

79. methods according to claim 6, it is characterised in that:

80. according to method described in claim 79, it is characterised in that:

81. according to method described in claim 79, it is characterised in that:

82. according to method described in claim 79, it is characterised in that:

(2) at recycling step, the disconnected side chain reaction process RTC30 of hydrogenation is set;

At the disconnected side chain reaction process RTC30 of hydrogenation, select the disconnected side chain hydrocracking catalyst TCR30C of shape use ZSM-5 molecular sieve, its can be about 0.53nm �� 0.56nm that is 0.53 nanometer �� 0.56 nanometer by a few pore size.

83. according to method described in claim 33, it is characterised in that: