CN106190283B

CN106190283B - The hydrocarbon heat from hydrogenation cracking method inferior for adding hydrogen aromatic hydrocarbons either shallow saturated reaction process is set

Info

Publication number: CN106190283B
Application number: CN201610542919.2A
Authority: CN
Inventors: 何巨堂
Original assignee: Individual
Current assignee: Luoyang Rui Hua New Energy Technology Development Co Ltd
Priority date: 2016-07-04
Filing date: 2016-07-04
Publication date: 2018-09-21
Anticipated expiration: 2036-07-04
Also published as: CN106190283A

Abstract

The hydrocarbon heat from hydrogenation cracking method inferior for adding hydrogen aromatic hydrocarbons either shallow saturated reaction process is set, in hydrocarbon HDS such as metals inferior, polycyclic aromatic hydrocarbon, colloid, the high coal tar heavy oil of asphalt content adds hydrogen aromatic hydrocarbons either shallow saturated reaction process R10, super delocalization energy based on aromatic ring pi bond among polycyclic aromatic hydrocarbon is more than the rule of the super delocalization energy of outside aromatic ring pi bond, carried out under conditions of based on the liquid phase reactor polycyclic aromatic hydrocarbon plus hydrogen aromatic hydrocarbons either shallow saturated reaction so that in-between aromatic ring is saturated, HDS produced positioned at the low methylene bridged bond of the dissociation energy in the centre position of multiring structure aromatic hydrocarbons while de- carbon residue reaction, it is provided rich in the hot tearing material for preferably cracking key for heat from hydrogenation cracking reaction process R20, also it is conducive to improve the yield of hexatomic ring hydrocarbon system object；Reaction compartment liquid phase reactor efficiency can be improved in the operation of R10 low hydrogen/gasoline ratios, and heater can be set up between R10 and R20, and R10 combines processing effect more preferably using hydrogen-containing hydrocarbon stream.

Description

The hydrocarbon heat from hydrogenation cracking method inferior for adding hydrogen aromatic hydrocarbons either shallow saturated reaction process is set

Technical field

The present invention relates to setting plus the hydrocarbon heat from hydrogenation cracking methods inferior of hydrogen aromatic hydrocarbons either shallow saturated reaction process, in hydrocarbon inferior The HDS such as high coal tar heavy oils of metal, polycyclic aromatic hydrocarbon, colloid, asphalt content add hydrogen aromatic hydrocarbons either shallow saturated reaction process R10, the super delocalization energy based on aromatic ring pi bond among polycyclic aromatic hydrocarbon is more than the rule of the super delocalization energy of outside aromatic ring pi bond, anti-in liquid phase Polycyclic aromatic hydrocarbon is carried out under conditions of based on answering adds hydrogen aromatic hydrocarbons either shallow saturated reaction that in-between aromatic ring is made to be saturated, and HDS is taken off Carbon residue produces the low methylene bridged bond of the dissociation energy positioned at the centre position of multiring structure aromatic hydrocarbons while reaction, be heat from hydrogenation Cracking reaction process R20 is provided rich in the hot tearing material for preferably cracking key, is also conducive to improve the yield of hexatomic ring hydrocarbon system object；R10 is low Reaction compartment liquid phase reactor efficiency can be improved in hydrogen-oil ratio operation, and heater can be set up between R10 and R20, and R10 uses hydrogen supply hydrocarbon object Flow joint processing effect more preferably.

Background technology

Coal tar heavy oil HDS of the present invention refers to that the normal boiling point from coal tar is higher than 450 DEG C of fraction such as coal Pitch is generally rich in metal, polycyclic aromatic hydrocarbon, resin and asphalt.

Coal tar heavy oil HDS's of the present invention adds hydrogen lighting process, refers to that coal tar heavy oil hydro-conversion produces Normal boiling point is less than the process of 450 DEG C of fractions, which generally comprises heat from hydrogenation cracking reaction, on suitable reactor types are Streaming expanded bed hydrogenation reactor such as floating bed hydrogenation reactor or boiling bed hydrogenation reactor or moving-burden bed reactor.

The target of coal tar heavy oil HDS of the present invention and coal tar suspension bed heat from hydrogenation cracking reaction process R20 are anti- Answer component；R20 locates with the hydrocarbon component BSAA that the ideal solvent oil of reaction is that normal boiling point is 330~450 DEG C in R20 substantially In liquid phase state therefore solvent naphtha or dilution oil ingredient can be served as；R20 is less than 330 DEG C of hydrocarbon group with the normal boiling point of reaction Point, R20 majorities be in gas phase state thus serve as solvent naphtha or dilution oil ingredient efficiency it is too low, have an adverse effect instead as Hydrogen partial pressure is reduced, vapor is generated because oxygen-enriched, high aromatic carbon rate aromatic hydrocarbons, drop are reacted and generated in the thermal cracking gas making that generation is excessive Low liquid product yield increases hydrogen consumption, increases reaction temperature rising.

The present invention relates to the hydrogenation processes of coal tar, more particularly to it is 330~450 DEG C of hydrogen supply to use normal boiling point The heat from hydrogenation cracking process R20 using suspension bed of coal tar heavy fractioning HDS of the normal boiling point of solvent naphtha higher than 450 DEG C.

The molecular structure of different fractions section about middle coalite tar, molecular size, gum asphalt are in aromatic naphtha Solvability, CN104927914A includes to be said using the high aromatics hydrogenation process of the low hydrogen/gasoline ratio pre- hydrogenation process of hydrogen supply hydrocarbon The 10th section to the 14th section of bright book has been described.In fact, colloid, asphalitine component, inherently room temperature in coal tar Under (30~80 DEG C) dispersions be present in solute in other light aromatics solvents, the two collectively forms relatively uniform solution, very Obviously, quantity of solvent is bigger, and the dispersion degree of solute is bigger, and colloid, the warm-up movement collision probability of asphalitine component are lower.

The polycyclic aromatic hydrocarbon being rich in the high coal tar heavy fractioning HDS inferior of density, which belongs in the high ring structure of aromatic carbon rate, to be lacked The gluey pitch shape component being rich in the multiring structure aromatic hydrocarbons KEYC of methylene bridge, the high coal tar heavy fractioning HDS inferior of density Belong in the high ring structure of aromatic carbon rate the complex or associated matter of the multiring structure aromatic hydrocarbons KEYCX for lacking methylene bridge, the present invention Concern is：The heat for being converted into light oil can not be recycled by becoming in the thermal condensation for reducing or not increasing gluey pitch shape component Under condensation product such as liquid phase be burnt or the precondition of the conversion ratio of solid coke, the high virtue of aromatic carbon rate for being difficult to thermal cracking how is improved Thermal cracking lighting conversion of the complex or associated matter of hydrocarbon KEYC, KEYCX in floating bed hydrogenation heat cracking reaction process R20 Rate can be also related to how to improve obtained by the product R20P from R20 certainly into gluey pitch shape in the recycle oil of reaction process R20 The conversion ratio of component.

Key reactions of the coal tar heavy fractioning HDS inferior in floating bed hydrogenation heat cracking reaction process R20 is described below.

In the heat from hydrogenation cracking reaction process R20 using suspension bed of coal tar heavy fractioning HDS, most important target is anti- Should be the heat from hydrogenation cracking reaction of the polycyclic aromatic hydrocarbon of gluey pitch shape component, if full without of the present invention plus hydrogen aromatic hydrocarbons either shallow With reaction process R10, target heat from hydrogenation cracking reaction, that is, positive reaction of heat from hydrogenation cracking reaction process R20 is including at least following Two series connection steps：

1. heat cracking reaction occurs for 1 macromolecular comprising low dissociation energy bridged bond, generate that at least two molecular weight is smaller splits Solve object free radical；The step consumes energy and there is cracking energy threshold, and speed is slower；

The scission of link position of the heat from hydrogenation cracking reaction of the polycyclic aromatic hydrocarbon of desired shape pitch shape component, is in polycyclic aromatic hydrocarbon On intermediate ring, low number of rings structure hydrocarbon product is generated in this way；

2. stabilized hydrogenation reaction quickly occurs for lysate free radical, relatively stable molecule is generated.

If the content of the low dissociation energy bridged bond in goal response object is too low, the target heat from hydrogenation cracking of goal response object Reaction is it is difficult to which the target heat from hydrogenation cracking reaction conversion ratio for carrying out i.e. goal response object is very low, or needs to increase substantially reaction Temperature, the side reaction in such thermal response will quickly increase, and overall side reaction trend is to increase negative reaction：

1. increasing by the first negative reaction -- the non-targeted thermal response of goal response object i.e. depth thermal condensation is reacted, such as aromatic hydrocarbons dehydrogenation Depth thermal condensation is reacted, that is, is increased the yield for being difficult to recycle the thermal condensation object for being converted into light oil such as weight colloid, heavy bitumen matter, increased The thermal condensation object for being converted into light oil such as liquid phase coke or the yield of solid coke can not be recycled by adding；This is by deteriorate drastically thermal cracking The liquid phase of reaction process forms, its viscosity is made to increase considerably, and dissolving hydrogen, transmission hydrogen, hydrogen supply capacity are greatly lowered, thick The collision of cycloaromatics, colloid, asphalitine is condensed probability and increases considerably, and improves the thermal condensation coking reaction speed of liquid phase, increases Wall of reactor, the speed of hot high score device wall coking threaten device long-term operation；On excessively high thermal cracking temperature can aggravate State disastrous effect；

Based on the first negative reaction, since suspension bed heat cracking reaction process is oily usually using a large amount of Liquid product recycle, Long-term circulate operation as a result, condensed-nuclei aromatics, colloid, asphalitine will be caused to be deposited in the accumulation of space reactor naturally, Height deteriorates liquid phase composition and deteriorates liquid-phase reaction condition；

2. increasing by the second negative reaction -- either shallow the thermal condensation reaction such as aromatic hydrocarbons either shallow of non-targeted reactant such as the hydrocarbon component BSAA Thermal condensation is reacted, that is, increases the yield of the either shallow condensation product condensed-nuclei aromatics BSAAD of polycyclic aromatic hydrocarbon, although these either shallow condensation products are thick The most of of cycloaromatics BSAAD remains to be changed into light oil centainly plus under hydrogen and/or cracking conditions, and which increases BSAAD Secondary plus hydrogen and secondary cracking task amount, either return to the cycle heat from hydrogenation cracking of R20 or subsequent plus hydrogen and cracking Step；On the other hand, at least part condensed-nuclei aromatics BSAAD will gradually be converted into colloid, asphalitine, i.e., increase again in reaction process Add and produce fractional goal response component, aggravates the deterioration of the property of liquid phase of suspension bed heat cracking reaction process；

Second negative reaction is that the first negative reaction manufactures raw material, is the accomplice of the first negative reaction；

3. increasing third negative reaction -- the disconnected side chain reaction of the thermal cracking of for example long side chain aromatic hydrocarbons BSLL of non-targeted reactant increases Add gas yield, increase short-side chain density of aromatic hydrocarbon, weakens the space steric effect formed by long-chain between aromatic core group, increase The pyrocondensation reaction probabilities of short-side chain aromatic hydrocarbons；

Third negative reaction is that the second negative reaction manufactures raw material, is the accomplice of the second negative reaction.

In fact, the side reaction in order to avoid thermal response largely occurs, maintenance thermal cracking target product, that is, normal boiling point is The high yield of 60~350 DEG C of thermal cracking hydrocarbon products, operation temperature cannot be excessively high, for example should be less than 495~525 DEG C of coking temperature Certain distance, typically results in that heat soaking operation temperature is relatively low to cause heat cracking reaction speed relatively low in this way；In order to inhibit pyrocondensation Conjunction reaction inhibits second pyrolysis reaction, and heat from hydrogenation cracking reaction process R20, which is operated and used usually under high hydrogen partial pressure, adds hydrogen to urge Agent, lysate free radical add hydrogen saturated reaction to be usually faster than heat cracking reaction speed, therefore, goal response object heat from hydrogenation cracking The rate-determining steps of reaction are typically heat cracking reaction.Due in the heat cracking reaction speed and goal response object of mark reactant HDS The content of low dissociation energy bridged bond is directly proportional, therefore, it can be stated that, the content of low dissociation energy bridged bond is directly strong in goal response object Ground affects heat cracking reaction speed；And improve heat cracking reaction speed, it is meant that the thermal cracking time is reduced, the result is that reducing heat Condensation reaction amount reduces thermal condensation reaction depth, this will directly reduce the content of contained thermal condensation object and pyrocondensation in product R20P The condensed ring degree of object is closed, reduces and turns from obtained by product R20P into the gluey pitch shape component in the recycle oil of reaction process R20 Change load, conversion ratio and recycle ratio.

Coal tar heavy fractioning HDS inferior is described below in floating bed hydrogenation heat cracking reaction process R20, normal boiling point is The key reaction of the adjoint reactive component BSAA of 330~450 DEG C of the hydrocarbon component.

It is most important with anti-in the heat from hydrogenation cracking reaction process R20 using suspension bed of coal tar heavy fractioning HDS Should be with the i.e. positive reaction of target heat from hydrogenation cracking reaction of reactive component BSAA, if being free of pre-hydrotreating reaction of the present invention Process R10, heat from hydrogenation cracking reaction process R20 include at least following two series connection steps：

1. heat cracking reaction occurs for 1 macromolecular comprising low dissociation energy bridged bond, generate that at least two molecular weight is smaller splits Solve object free radical；

2. lysate free radical quickly occurs plus hydrogen saturated reaction, relatively stable molecule is generated.

It is obvious that with the rate-determining steps of reactive component BSAA heat from hydrogenation cracking reactions be goal response object thermal cracking it is anti- It answers, and it is directly proportional to the low content of dissociation energy bridged bond in goal response object with the heat cracking reaction speed of reactive component BSAA, If the content with the low dissociation energy bridged bond in reactive component BSAA is too low, with the target heat from hydrogenation of reactive component BSAA Cracking reaction is difficult to carry out i.e. very low with the heat from hydrogenation cracking reaction conversion ratio of reactive component BSAA, or needs significantly to carry High reaction temperature, the side reaction in such thermal response will quickly increase, and overall side reaction trend is to increase negative reaction：

1. increasing non-targeted thermal condensation reaction such as aromatic hydrocarbons thermal condensation to react, that is, increase production the higher condensation aromatic ring of condensed ring degree, or It is the fragrant charcoal rate for increasing production aromatic hydrocarbons, these groups by the aromatic hydrocarbons that 3 rings of fractional saturation, 4 cycloaromatics dehydrogenations become all fragrant charcoals of ring charcoal The hydrogen content compared with its precursor aromatic hydrocarbons is divided to decline, for its target thermal cracking lighting reaction, pyrocondensation and reaction belong to It is reacted in the thermal cracking lighting of wide backward reaction, thermal condensation object：Step is more, the energy of consumption is more；

2. increasing non-targeted heat cracking reaction such as aromatic side chain cleavage reaction increases gas yield.

Exist simultaneously the hydrogen supply reaction with the hydrogen supply hydrocarbon in reactive component BSAA：In hydrogen-abstracting agent (such as aromatic carbon rate 100% Polycyclic aromatic hydrocarbon) in the presence of, improve aromatic carbon rate after hydrogen supply hydrocarbon in component BSAA release reactive hydrogen.

It is obvious that in floating bed hydrogenation heat cracking reaction process R10, coal tar heavy fractioning HDS inferior and adjoint reaction The reaction condition of component BSAA, either forward reaction, that is, target thermal cracking lighting reaction or backward reaction, that is, thermal condensation The reaction condition of reaction and gas making reaction, all has consistency.Therefore, described herein to have certain for coal tar heavy fractioning HDS The operating condition that kind influences, actually on also having close or similar influence with reactive component BSAA.

Compared with the low density coal tar heavy fractioning rich in methylene bridged bond, for rich in the high shortage methylene of aromatic carbon rate It is inevitable using floating bed hydrogenation thermal cracking process R20 for the coal tar heavy fractioning HDS of the gluey pitch shape component of base bridged bond Generate the reaction selectivity difference of above-mentioned " target heat cracking reaction speed is small, the heat cracking reaction time is long, thermal condensation reaction is more " As a result, such result is for the normally desired result of industrial technology, it may be said that extremely it is undesirable even fail.Its root Source is that polycyclic aromatic hydrocarbon in coal tar heavy fractioning HDS, gluey pitch shape component are the high shortage methylene bridged bonds of aromatic carbon rate The hydrocarbon component.

Based on the above analysis as can be seen that high rich in aromatic carbon rate in view of the high coal tar heavy fractioning HDS inferior of density Lack the polycyclic aromatic hydrocarbon of methylene bridge, the high concentration liquid phase of gluey pitch shape component, the target of goal response object in ring structure Thermal cracking lighting is reacted based on liquid phase reactor, rich reaction heat condensation reaction be also based on liquid phase reactor, positive reaction with Negative reaction shows as the opposite competitive reaction in direction of the same component of same liquid phase, therefore is provided just in the environment of liquid solution The competitiveness of reaction and negative reaction condition, decisive action is played to the Direction of Reaction, is to determine heat from hydrogenation cracking reaction process R20 works Industry device operates the key of success or failure；In heat from hydrogenation cracking reaction process R20, although operation hydrogen pressure, operation temperature, catalyst, hydrogen Oil volume has an impact " competitiveness of positive reaction and negative reaction condition " than, air speed technological parameter, but in contrast, liquid Hydrocarbon liquid phase forms the relativeness of hydrocarbon group component in other words in phase, be pairs of positive reaction and negative reaction competition results influence it is most strong Strong direct factor；Due to polycyclic aromatic hydrocarbon in coal tar heavy fractioning HDS inferior, gluey pitch shape constituent content is too high has become The host component of practical liquid phase, influence each other solvent each other each other, therefore " in order to change positive reaction and negative reaction selectivity React and change liquid phase solvent hydrocarbon composition ", it has been equal in fact and " has changed to change positive reaction and negative reaction selective reaction Become raw material petroleum hydrocarbon composition ", this has not been the task of heat from hydrogenation cracking reaction process R20, it is required that it is anti-to increase a guide Answer process ----plus hydrogen aromatic hydrocarbons either shallow saturated reaction process, task be " HDS first carry out guiding plus hydrogen lighting reaction (or Person says that hydrofinishing adds hydrogen lighting to react), it is produced positioned at the centre of multiring structure aromatic hydrocarbons while de- carbon residue reacts The low methylene bridged bond of the dissociation energy of position, provides for heat from hydrogenation cracking reaction process R20 rich in the thermal cracking for preferably cracking key Material ", finally constitutes following relatively reasonable reaction chain：" multiring aromatic hydrocarbon the hydrocarbon component → guiding plus hydrogen lighting reaction (adds Hydrogen aromatic hydrocarbons either shallow saturated reaction) → heat cracking reaction → lysate free radical stabilized hydrogenation reaction "

It is above-mentioned analysis shows, for rich in aromatic carbon rate it is high shortage methylene bridged bond gluey pitch shape component coal tar For heavy distillat HDS, in floating bed hydrogenation thermal cracking process R20, in order to improve object thermal cracking lighting reaction speed, Inhibit the side reaction in thermal response, preferably before the heat from hydrogenation cracking reaction process R20 based on heat cracking reaction, by coal tar The molecular structure of oily heavy distillat HDS is adjusted, it is necessary to such as be used under conditions of the side reaction in inhibiting thermal response relatively low Reaction temperature plus the stronger catalyst of hydrogen saturation function, more hydrogen supply hydrocarbon, in the polycyclic aromatic hydrocarbon knot of gluey pitch shape component Manufacture is prone to low dissociation energy bridged bond such as methylene bridge of heat cracking reaction etc. in structure, that is to say, that needs to arrange for a condition Suitable plus hydrogen aromatic hydrocarbons either shallow saturated reaction process R10.

Based on above-mentioned analysis, the present invention proposes setting plus the hydrocarbon heat from hydrogenation cracking inferior of hydrogen aromatic hydrocarbons either shallow saturated reaction process Method, basic conception are：In the hydrocarbon HDS inferior such as high coal tar heavy oils of metal, polycyclic aromatic hydrocarbon, colloid, asphalt content Add hydrogen aromatic hydrocarbons either shallow saturated reaction process R10, the super delocalization energy based on aromatic ring pi bond among polycyclic aromatic hydrocarbon is more than outside aromatic ring pi bond Super delocalization energy rule, carried out under conditions of based on the liquid phase reactor polycyclic aromatic hydrocarbon plus hydrogen aromatic hydrocarbons either shallow saturated reaction make it Intermediate aromatic ring is saturated, and HDS carries out producing the dissociation positioned at the centre position of multiring structure aromatic hydrocarbons while de- carbon residue reaction The low methylene bridged bond of energy, provides for heat from hydrogenation cracking reaction process R20 rich in the cracking material for preferably cracking key, is also conducive to improve six The yield of membered ring hydrocarbon system object；Reaction compartment liquid phase reactor efficiency can be improved in the operation of R10 low hydrogen/gasoline ratios, can be set up between R10 and R20 Heater, R10 combine processing effect more preferably using hydrogen-containing hydrocarbon stream.

Setting plus hydrogen aromatic hydrocarbons either shallow saturated reaction process R10 are that hydrocracking reaction process R20 prepares target cracking key more More cracking stock hydrocarbon, this is the technology proposition not referred in existing coal tar suspension bed heat from hydrogenation process, certainly This is required plus hydrogen aromatic hydrocarbons either shallow saturated reaction process R10 operation temperatures are relatively low and/or add adding for hydrogen saturation function using having Hydrogen catalyst and/or a large amount of hydrogen supply hydrocarbon of use and/or the lower hydrogen to oil volume ratio of use, corresponding technological measure or effect are：

1. reducing operation temperature or the diminution of the reaction process temperature difference being made to be easy to implement, it may be necessary to big using product liquid Recycle ratio operation scheme；

2. using the hydrogenation catalyst for adding hydrogen saturation Function fitness strong, such as micron-sized crystallite molybdenite (MoS₂) or it is other Efficient compound catalyst；

It is hydrocarbon easy to implement, being 330~450 DEG C using the normal boiling point in coal tar 3. using a large amount of hydrogen supply hydrocarbon Component BSAA can be prepared；HDS can also use branch to be fed mode；

It is easy to implement 4. using low hydrogen to oil volume ratio, under the premise of ensureing to react hydrogen partial pressure, reduces hydrogen oil Volume ratio can extend the liquid phase residence time in reactor reaction space, increase the removal of ccr by hydrotreating reaction depth of HDS.

About the hydrogenation catalyst for adding hydrogen saturation Function fitness strong, a document for recording this kind of technology is shown in：1. publication Title：《Hydroprocessing technique and engineering》, page 66 to page 68；2. retrieval is encoded with books：ISBN is encoded：7-80164-665-7； Chinese depository library CIP data core words：(2004) No. 128349；3. editing：Li Dadong；4. publishing house：Sinopec goes out Version society.The micron-sized crystallite molybdenite (MoS that the hydrogenation of residual oil suspended bed technology EST of Italian ENI companies exploitation is used₂), It is exactly a kind of very high hydrogenation catalyst of hydrogenation activity of promotion hydrogenation reaction without promoting cracking reaction, hot tearing can be rapidly saturated Change C-C the and C- heteroatom radicals generated, it may have certain aromatic hydrogenation is saturated catalytic capability, can effectively inhibit fragrant cluster The condensation reaction of group inhibits coking reaction.It is demonstrated experimentally that the Hydrogenation of this Mo catalyst relative to transition metal Ni, V, Co, Fe etc. are better.The decompression residuum of a variety of crude oil with poor quality of EST technical finesses and extra-heavy crude oil experiments have shown that, 400 Mild hydrocracking, the crystallite molybdenite catalyst of ＞ 1000PPm contents are carried out under~425 DEG C and 16.0MPa of reaction condition Additive amount can inhibit green coke and promote the hydro-upgradings reactions such as demetalization, de- carbon residue, conversion ratio ＞ 99%, demetallization per ＞ 99%, take off carbon yield ＞ 95%, 1% of asphalitine less than raw material residual oil of discharge.

If the coal tar heavy fractioning HDS that hydrogen content is 6.8~7.5% is directly entered floating bed hydrogenation thermal cracking process R20, total hydrogen-consuming volume are calculated according to 3.0~3.5%, and overall big, the overall temperature rise value of thermal discharge is big, in reaction feed hydrogen oil volume Under conditions of being 1000, total overall reaction heat can cause its net raw material Wen Sheng to reach 120~160 DEG C, due to floating bed hydrogenation Thermal cracking process R20 is in order to form the reaction condition of the hotbeds such as the small myopia of the temperature difference, R20 reaction zones inlet temperature and outlet temperature Difference can not possibly be too such as usually 20~60 DEG C big, relies solely on react total shared by the reaction heat quantity that net product is taken out of in this way The ratio of reaction heat is smaller, and remaining major part reaction heat (can heat net raw material Wen Sheng and reach 100~140 DEG C) can only lean on low temperature State feedstock oil and/or cold state raw hydrogen shift or absorb carrying, although reaction heat energy regenerating may be implemented, one Denier cold state feedstock oil interrupts, and the inlet temperature of the first reactor of floating bed hydrogenation thermal cracking process R20 will rise to ratio moment 25~40 DEG C are such as improved, the superposition of reaction heat in conversion zone will be led to, temperature runaway can be induced, it is very harmful.And it is arranged and adds hydrogen virtue Hydrocarbon either shallow saturated reaction process R10 can then significantly reduce the temperature value TS of the starting reaction of coal tar heavy fractioning HDS, this has Conducive to reduction " preheating terminal temperature=Δ T1 of the temperature value TS- coal tar heavy fractionings HDS of starting reaction " temperature difference, in this way may be used To increase substantially the safety of R10, simultaneously as plus hydrogen aromatic hydrocarbons either shallow saturated reaction process this low-temp reaction section of R10 deposit It gains time for follow-up floating bed hydrogenation thermal cracking process R20 adjustment operating parameters or process accident, it in this way can be significantly Safety or the operability of device are improved, this is that process safety can be improved in second advantage of the present invention.

Third advantage of the present invention is can to carry the lighting conversion ratio of gluey pitch shape component, adds hydrogen aromatic hydrocarbons either shallow full With reaction process R10 under conditions of inhibiting heat cracking reaction, generation adds hydrogen saturated reaction gum asphalt can be made to have occurred Apparent removal of ccr by hydrotreating reaction, reduces gum asphalt and is converted into expected lightweight in floating bed hydrogenation thermal cracking process R20 The reaction step of product, therefore the one way heat from hydrogenation cracking light conversion ratio of gum asphalt can be improved.

Fourth advantage of the present invention is can to form clearly " order of reaction or conversion zone " concept, according to reaction process Leading reaction target difference or fluctuation section according to reaction process reaction temperature, be arranged reaction process hierarchical concept or Fractional concept, and then segmentation reaction liquid phase product circulation concept is established, it the advantage is that：

1. flexible modulation or the yield for controlling short residence time (low circulation reaction times) liquid product, determine one way indirectly Conversion ratio prevents unreasonable single-stage response effect, enhances thermodynamics, the hydraulics stability of operating process；

2. it is anti-to enhance Discrete control operating condition such as reaction temperature, hydrogen-oil ratio, recycle oil ratio, liquid phase residence time, cycle The flexible adjustment for answering number etc. increases the selection elasticity of reactor diameter.

Fifth advantage of the present invention is, based on clearly " order of reaction or conversion zone " concept, according to the master of reaction process It leads the difference of reaction target or interstage temperature control measures is reacted in the fluctuation section according to reaction process reaction temperature, setting, from And it is clearly distinguishable from the existing more stream that heater such as heating furnace is not provided between suspended-bed reactor and/or fluidized bed reactor Journey form, the present invention under most conditions, are adding hydrogen aromatic hydrocarbons either shallow saturated reaction process R10 and are being to be hydrocracked thermal process reactor It needs that heater such as heating furnace is arranged between R20, the heating that goes into operation is adjusted flexibly and/or serves as with realize temperature difference between order of reaction Stove.

The method of the invention has not been reported.

A kind of coal tar heavy oil using floating bed hydrogenation reactor adds hydrogen lightening method, is by whole coal tar oil ingredients (including fraction of the normal boiling point less than 370 DEG C and normal boiling point are higher than 370 DEG C of fraction) as the raw material being hydrocracked, uses Suspension bed or bubbling bed hydrocracking reactor carry out hydrocracking reaction process, and normal boiling point is less than 330 DEG C by this method The hydrocarbon component introduces hydrocracking reaction process, and defective workmanship is extremely harmful, is also not provided with and adds hydrogen aromatic hydrocarbons either shallow saturated reaction Process.

Chinese patent ZL201010217358.1 describes a kind of coal tar heavy oil using floating bed hydrogenation reactor and adds Hydrogen lightening method, including coal tar raw material pretreatment and distillation separation, coal tar heavy end floating bed hydrocracking and light Matter distillate routine upgrading process.The process characteristic of ZL201010217358.1 is evaporating more than 370 DEG C in coal tar It is allocated as the raw material to be hydrocracked, hydrocracking reaction process R1 is carried out using suspension bed or bubbling bed hydrocracking reactor, Major part (about 80%) direct circulation freshening recracking of mink cell focus (pitch) of the reaction product more than 370 DEG C, fraction (about 20%) is separated by solid-liquid separation, and recycles freshening recracking after detaching solid catalyst, it is therefore an objective to macromolecular in coal tar Pitch is as much as possible to be cracked into small molecule clean or white, is got rid of outside the catalyst separated, and the purpose got rid of outside is removed in cracking The a small amount of high molecular polymer generated in the process and the catalyst inactivated.The technology is due to returning most heavy bitumen Refining has been cracked into small molecule product, and light oil yield will significantly improve, and highest oil yield is 93% or more.This method, which is not provided with, to be added Hydrogen aromatic hydrocarbons either shallow saturated reaction process.

A kind of Chinese patent ZL201210022921.9 proposes the low hydrogen content heavy oil using hydrogen supply hydrocarbon plus hydrogen lighting Method, for being more than 330 DEG C of whole fractions in coal tar, normal boiling point is directly entered swollen higher than 450 DEG C of coal tar heavy oil Swollen bed (such as suspension bed or ebullated bed) heat from hydrogenation cracking reaction area HPU21, while the coal tar for being 330~450 DEG C by normal boiling point Oily fraction as hydrogen supply dissolvent oil precursor by hydrogenation modification reaction zone HPU1 production mainly by normal boiling point be 330~ The hydrogen-containing hydrocarbon stream SHS of 450 DEG C of the hydrocarbon component composition, then introduces heat from hydrogenation cracking reaction area HPU21, it is evident that can by SHS The ratio KL that SHS flows through in reaction zone " hydrogen supply hydrocarbon weight/fresh feed F10X weight " is significantly improved, therefore is condensed with reducing Coking speed improves coal tar heavy oil hydroconversion process liquid product yield, improves product quality, reduce reaction temperature rising, increase The remarkable result of intensity device smooth operation and safety.This method is not provided with plus hydrogen aromatic hydrocarbons either shallow saturated reaction process.

Chinese patent ZL200810166719.7 describes a kind of Unionfining conversion side of coal tar distillate with different boiling ranges First hydrocarbon fraction of method, the coal tar light fraction containing normal boiling point less than 390 DEG C is partially completed in the first hydrofining reaction Conversion, the second hydrocarbon fraction of the first hydrofining reaction effluent and the coal tar heavy duty fraction containing normal boiling point higher than 370 DEG C It is partially completed conversion in the second hydrofining reaction, the second hydrofining reaction effluent is detached and recycles product.Chinese patent Coal tar distillates different to boiling range ZL200810166719.7 carries out Unionfining conversion, forms hydrofinishing preferably Reaction temperature profile has many advantages, such as to improve product quality, quiet run, extends the operation cycle, particularly suitable for medium and high temperature coal The small-scale classification Unionfining of tar wide fraction converts.This method does not refer explicitly to coal tar heavy oil F10 and enters expansion Bed (such as suspension bed or ebullated bed) heat from hydrogenation cracking reaction process, is also not provided with and adds hydrogen aromatic hydrocarbons either shallow saturated reaction process.

CN105623724A discloses a kind of heat from hydrogenation cracking method of the high aromatic hydrocarbons production hexa-atomic cyclic hydrocarbon of low carbon number list, in can using The hexamethylene methane series hydrocarbon or benzene hydrocarbons of coalite tar economically fecund C6~C10, obtains benzene class after catalytic reforming, Aromatics Extractive Project Hydrocarbon.For coal tar hydrogenating heat cracking reaction process R10, which recycles the first hydrogenation reaction effluent R10P packets Logistics containing the first hydrogenated oil, first of usual normal boiling point higher than 350 DEG C are hydrogenated to petroleum hydrocarbon, return to first and add hydrogen anti- Process R10 is answered to be contacted with the first hydrogenation catalyst R10C, first plus the hydrogen life that at least part normal boiling point is 260~350 DEG C At petroleum hydrocarbon, returns to the first hydrogenation process R10 and contacted with the first hydrogenation catalyst R10C, the first hydrogenation reaction effluent R10P In the extra high easy thermal condensation the hydrocarbon component of normal boiling point do not return again to the first hydrogenation process R10.This method is not also set It sets and adds hydrogen aromatic hydrocarbons either shallow saturated reaction process.

The method of the present invention is suitable for new device, it can also be used to have plant modification.

Therefore, it is an object of the invention to propose that the hydrocarbon heat from hydrogenation inferior of setting plus hydrogen aromatic hydrocarbons either shallow saturated reaction process is split Change method.

Invention content

The hydrocarbon heat from hydrogenation cracking method inferior of present invention setting plus hydrogen aromatic hydrocarbons either shallow saturated reaction process, it is characterised in that packet Containing following steps：

(1) in the first hydrogenation process R10, there are hydrogen, hydrocarbon liquid phase, there may be the materials of solid particle simultaneously Under the conditions of, high aromatic carbon rate poor quality hydrocarbon HDS carry out comprising plus the first hydrogenation reaction R10R of hydrogen aromatic hydrocarbons either shallow saturated reaction obtain the One hydrogenation reaction product BASE-R10P；

Hydrocarbon HDS inferior is the high aromatic carbon hydrocarbon material of the hydrocarbon component HD comprising normal boiling point higher than 450 DEG C；

Hydrocarbon HDS inferior, including conventional liquid hydrocarbon raw material HDSL, may include solid particulate materials HDSS；

First hydrogenation reaction R10R, including at least part liquid hydrocarbon feeds HDSL the hydrocarbon component HD hydrofining reaction R10-HD-HTR, hydrofining reaction R10-HD-HTR include at least the partial hydrogenation saturated reaction R10-HD- of polycyclic aromatic hydrocarbon HDAR may include other unsaturated hydrocarbons plus hydrogen saturated reaction and/or impure hydrocarbon plus hydrogen hydrogenolysis；

The reaction of at least part removal of ccr by hydrotreating, the production of the first hydrogenation reaction occurs in the first hydrogenation process R10, HDS The carbon residue of hydro carbons is less than the carbon residue of hydrocarbon HDS inferior in object BASE-R10P；

First hydrogenation reaction R10R is carried out under conditions of based on the liquid phase reactor, what at least part the hydrocarbon component HD occurred The partial hydrogenation saturated reaction R10-HD-HDAR of polycyclic aromatic hydrocarbon makes the aromatic carbon rate reduction of at least part the hydrocarbon component HD be converted into hydrocarbon Component HDH makes the aromatic ring of at least part polycyclic aromatic hydrocarbon component HDA be saturated to form methylene bridged bond, the production of the first hydrogenation reaction The aromatic carbon rate of hydro carbons is less than the aromatic carbon rate of hydrocarbon HDS inferior in object BASE-R10P；

First hydrogenation reaction R10R may use hydrogenation catalyst R10C using up flow type hydrogenation reactor R10E；First When hydrogenation process R10 uses hydrogenation catalyst R10C, the reaction compartment of the up flow type hydrogenation reactor R10E used is urged Agent enters, catalyst is discharged；

There may be part the first hydrogenation reaction product BASE-R10P to deposit or stop or be circulated in hydrogenation reactor R10E Portion space；

First hydrogenation reaction product BASE-R10P, for solid particle may be contained simultaneously containing hydrogen, conventional liq hydrocarbon Material；

Material based on the first hydrogenation reaction product BASE-R10 is used as the first hydrogenation reaction effluent R10P；

R10P is for being discharged BASE-R10P, for that may contain the object of solid particle simultaneously containing hydrogen, conventional liq hydrocarbon Material；

R10P occurs, the composition and phase phase of different R10PX logistics in the form of 1 tunnel or 2 tunnels or multichannel material R10PX It is same or different；

The logistics R10P-XO-TOR20 containing hydrocarbon ils in R10P based on R10P enters the second hydrogenation process R20；

(2) in the second hydrogenation process R20, there are hydrogen, hydrocarbon liquid phase, there may be the mixed phases of solid particle simultaneously Under the conditions of material, logistics R10P-XO-TOR20 carries out the second hydrogenation reaction R20R comprising heat from hydrogenation cracking reaction and obtains second Hydrogenation reaction product BASE-R20P；

Logistics R10P-XO-TOR20 includes the high aromatic carbon hydrocarbon material of the hydrocarbon component HDH of the normal boiling point higher than 450 DEG C；

Logistics R10P-XO-TOR20, including conventional liquid hydrocarbon raw material R10P-XO-TOR20L, may include that solid particle is former Expect R10P-XO-TOR20S；

Second hydrogenation reaction R20R, including the hydrocarbon component at least part conventional liquid hydrocarbon raw material R10P-XO-TOR20L The heat from hydrogenation cracking reaction of HDH may include the hydrocarbon component HDH at least part conventional liquid hydrocarbon raw material R10P-XO-TOR20L Hydrofining reaction；The hydrofining reaction of second hydrogenation reaction R20R include unsaturated hydrocarbons plus hydrogen saturated reaction and/or contain Impurity hydrocarbon adds hydrogen hydrogenolysis；

Second hydrogenation process R20 may use hydrogenation catalyst R20C using up flow type hydrogenation reactor R20E； When second hydrogenation process R20 uses hydrogenation catalyst R20C, the reaction compartment of the up flow type hydrogenation reactor R20E used There is catalyst to enter, catalyst discharge；

There may be part the second hydrogenation reaction product BASE-R20P to deposit or stop or be circulated in hydrogenation reactor R20E Portion space；

Second hydrogenation reaction product BASE-R20P, it is same to contain hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon Shi Keneng contains the mixed phase material including at least gas phase and liquid phase of solid particle；

Material based on the second hydrogenation reaction product BASE-R20P is used as the second hydrogenation reaction effluent R20P；

Second hydrogenation reaction effluent R20P is for being discharged the second hydrogenation reaction product BASE-R20P, to contain hydrogen, miscellaneous Matter component, conventional gas hydrocarbon, conventional liq hydrocarbon may contain the mixed phase object including at least gas phase and liquid phase of solid particle simultaneously Material；

Second hydrogenation reaction effluent R20P occurs, different R20PX in the form of 1 tunnel or 2 tunnels or multichannel material R20PX The composition and phase of logistics are identical or different；

(3) in removal process SR, what the second hydrogenation reaction effluent R20P of recycling obtained mainly being made of hydrogen in volume Hydrogen rich gas gas SRV and the possibility being mainly made of conventional liquid hydrocarbon contain the liquid stream SRL of solid particle, at least part Hydrogen rich gas gas SRV returns to hydrogenation process and recycles.

The present invention, the first hydrogenation process R10, best first hydrogenation reaction R10R is to add hydrogen aromatic hydrocarbons either shallow saturated reaction Based on, it is characterised in that：

(1) in the first hydrogenation process R10, there are hydrogen, hydrocarbon liquid phase there may be solid particles simultaneously at least Under the conditions of the mixed phase material of gas-liquid two-phase, hydrocarbon HDS inferior carry out with add based on hydrogen aromatic hydrocarbons either shallow saturated reaction first plus Hydrogen reaction R10R obtains the first hydrogenation reaction product BASE-R10P；

First hydrogenation reaction R10R is carried out under conditions of based on the liquid phase reactor, what at least part the hydrocarbon component HD occurred The partial hydrogenation saturated reaction R10-HD-HDAR of polycyclic aromatic hydrocarbon makes the aromatic carbon rate reduction of at least part the hydrocarbon component HD be converted into hydrocarbon Component HDH makes the intermediate aromatic ring of at least part polycyclic aromatic hydrocarbon component HDA be saturated to form methylene bridged bond, and first adds hydrogen anti- The aromatic carbon rate of hydro carbons in product BASE-R10P is answered to be less than the aromatic carbon rate of hydrocarbon HDS inferior；

First hydrogenation reaction product BASE-R10P, it is same to contain hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon Shi Keneng contains the mixed phase material including at least gas phase and liquid phase of solid particle；

R10P is for being discharged BASE-R10P, to contain hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon while can The mixed phase material including at least gas phase and liquid phase of solid particle can be contained；

The poor quality hydrocarbon HDS to add the first hydrogenation reaction R10R based on hydrogen aromatic hydrocarbons either shallow saturated reaction, refer to： It is that the outer hydrogen of remaining deoxidation consumes R10HK that first hydrogenation reaction R10R total hydrogen consumptions R10HT, which subtracts hydrogenation deoxidation reactive hydrogen consumption R10HDO, The outer hydrogen consumption R10HK of deoxidation is to add the hydrogen of hydrogen aromatic hydrocarbons either shallow saturated reaction to consume based on R10HDA, i.e. R10HDA/R10HK ＞ 0.5；

R10P enters the second hydrogenation process R20 as logistics R10P-XO-TOR20.

The present invention, in general, hydrocarbon HDS inferior is selected from one or more of following materials：

1. oil product obtained by coalite tar or its distillate or its hot procedure, hot procedure are coking or urge Change cracking process or catalytic pyrolysis process；

2. oil product obtained by medium temperature coal tar or its distillate or its hot procedure；

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

4. oil product obtained by direct hydrogenation liquefaction of coal liquefaction process, direct hydrogenation liquefaction of coal liquefaction process includes molten using hydrogen supply The direct hydrogenation liquefaction of coal liquefaction process of agent oil, coal refines process to oil altogether, coal faces hydrogen thermosol liquefaction process；

5. oil product obtained by petroleum based heavy fuel oils or its distillate or its hot procedure；

6. oil product obtained by shale oil or its distillate or its hot procedure；

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

8. other colloid weight contents are higher than 15% and/or asphalitine weight content is higher than 5.0% hydrocarbon ils.

The present invention is usually mainly made of normal boiling point higher than 450 DEG C of the hydrocarbon component HD when hydrocarbon HDS inferior comes from coal tar；

Carried out in the first hydrogenation process R10, hydrocarbon HDS inferior with add based on hydrogen aromatic hydrocarbons either shallow saturated reaction first plus Hydrogen reacts R10R, the Unit Weight hydrogen consumption of hydrocarbon HDS inferior：Usually 0.05~3.0%, generally 0.25~2.5%, it is preferably 0.5~1.5%.

The present invention comes from coal tar, the hydrogenation catalyst used in the first hydrogenation process R10, hydrocarbon HDS inferior R10C can be a kind of compound coal tar hydrogenation catalyst, including high-activity component and low activity component；The high activity group It is 1: 10 to 10: 1 that parting, which belongs to the weight ratio of low activity component metals,；The high-activity component is the water soluble salt chemical combination of molybdenum Or mixtures thereof object；The low activity group is divided into ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, catalyst R10C water contents are less than 2wt%；The powdered granule that R10C particle diameters are 1~100 μm.

The present invention comes from coal tar, the hydrogenation catalyst used in the first hydrogenation process R10, hydrocarbon HDS inferior R10C, can include at least Mo elements, and Mo is M in the body of work form of the first hydrogenation process R10₀S₂In, hydrogenation catalyst The powdered granule that agent R10C is 1~100 μm.

The present invention, when hydrocarbon HDS inferior comes from coal tar, the operating condition of the first hydrogenation process R10 is usually：Temperature For 300~480 DEG C, pressure be 6.0~30.0MPa, hydrogen/feedstock oil volume ratio is 0.01: 1~4000: 1, hydrogenation catalyst R10C addition weight is the 0.001~8.0% of HDS weight, volume space velocity is 0.1~10.0hr^-1；Hydrocarbon HDS weight chemistry inferior Hydrogen consumption is 0.05~3.0%.

The present invention, when hydrocarbon HDS inferior comes from coal tar, the operating condition of the first hydrogenation process R10 is generally：Temperature For 350~460 DEG C, pressure be 12.0~22.0MPa, hydrogen/feedstock oil volume ratio is 50: 1~600: 1, hydrogenation catalyst R10C addition weight is the 0.01~5.0% of HDS weight, volume space velocity is 0.2~2.0hr^-1；Hydrocarbon HDS weight chemistry hydrogen inferior Consumption is 0.50~1.5%.

The present invention, in the first hydrogenation process R10, when hydrocarbon HDS inferior comes from coal tar, hydrocarbon HDS inferior is carried out to add The average reaction temperature of the first hydrogenation reaction R10R, the first hydrogenation process R10 based on hydrogen aromatic hydrocarbons either shallow saturated reaction compared with Usually low 15~100 DEG C of the average reaction temperature of second hydrogenation process R20.

The present invention, when hydrocarbon HDS inferior comes from coal tar, its usual gum asphaltic content is 10~90%, carbon residue is 0.01~25%, tenor is 2~2000PPm；

Carried out in the first hydrogenation process R10, hydrocarbon HDS inferior with add based on hydrogen aromatic hydrocarbons either shallow saturated reaction first plus Hydrogen reacts R10R, and gum asphalt hydrogenation and removing rate is more than 3%, carbon residue hydrogenation and removing rate and is more than 3%.

The present invention, when hydrocarbon HDS inferior comes from coal tar, its general gum asphaltic content is 30~80%, carbon residue be 5~ 20%, tenor is 50~700PPm；

Carried out in the first hydrogenation process R10, hydrocarbon HDS inferior with add based on hydrogen aromatic hydrocarbons either shallow saturated reaction first plus Hydrogen reacts R10R, gum asphalt hydrogenation and removing rate：Typically larger than 5%, it is generally higher than 10%, preferably and is more than 15%, carbon residue Hydrogenation and removing rate：Typically larger than 5%, it is generally higher than 10%, preferably and is more than 15%.

The present invention, when hydrocarbon HDS inferior comes from coal tar, hydrogen/feedstock oil volume ratio of the first hydrogenation process R10： Usually less than 400: 1,200: 1 are generally below, 50: 1 can be less than, it can be to the reaction compartment of the first hydrogenation process R10 The method hydrogen make-up added using 2 times or repeatedly.

The present invention, when hydrocarbon HDS inferior comes from coal tar, the liquid phase volume of the reaction compartment of the first hydrogenation process R10 Divide rate：Usually above 0.5, it is generally greater than 0.7, can be 0.90~1.0.

Thermal high separation process R10MP-THPS, feature can be arranged in the first hydrogenation process R10 in the present invention It is：

In the first hydrogenation process R10, the end product of the first hydrogenation process R10 or intermediate product are considered as instead Answer product R10MP, setting thermal high separation process R10MP-THPS；

It is obtained containing dissolving hydrogen, normal boiling point in thermal high separation process R10MP-THPS, separation reaction product R10MP The hot high score liquid R10MP-THPS-L and net product stream R10MP-THPS-PP, R10MP- of conventional liquid hydrocarbon higher than 350 DEG C Solids may be contained in THPS-L；Net product stream R10MP-THPS-PP enters the adjacent hydroconversion reaction zone in downstream；

The logistics R10MP-THPS-LR comprising hydrocarbon liquids based on hot high score liquid R10MP-THPS-L returns to upstream and adds Hydroformylation reaction zone R10Z is used as cycle liquid phase；

Define the upstream of the weight flow rate and upstream hydroconversion reaction zone R10Z and R10Z that may be present of R10MP-THPS-LR The ratio between total weight flow rate of hydrocarbon HDS raw materials inferior of whole hydroconversion reaction zones is recycle ratio KR100, recycle ratio KR100：Usually 0.05~30, it is generally 0.5~10.

The present invention, in the first hydrogenation process R10, when using hydrogenation catalyst R10C, any up flow type using The structure type of hydrogenation reactor R10E can be in following a kind, when the up flow type that the first hydrogenation process R10 is used When hydrogenation reactor R10E is 2 or more, the structure type of up flow type hydrogenation reactor R10E is identical or different：

1. suspension bed；

2. ebullated bed；

3. moving bed.

The present invention, in the first hydrogenation process R10, existing solid particle can be selected from one of the following or 2 kinds Or it is a variety of：

1. semicoke particle obtained by direct hydrogenation liquefaction of coal process；

2. catalyst granules；

3. iron rust particle；

4. particles of inorganic material；

5. coking of coal process generate into the solid particle in coal tar；

6. the product solid particle from hydro carbons thermal condensation process；

7. the solid particle from shale；

8. the solid particle from oil-sand；

9. other particles being present in the first hydrogenation reaction product BASE-R10P.

The present invention, hydrocarbon HDS poor quality hydrocarbon HDS inferior point for two-way or demultiplex raw material when, it is characterised in that：

1. the reaction compartment of the first hydrogenation process R10 is divided into the sub- hydroconversion reaction zone of 2 or multiple serial operations： First sub- hydroconversion reaction zone R101, second sub- hydroconversion reaction zone R102 etc.；

Hydrocarbon HDS inferior points are two-way or demultiplex raw material, and first via poor quality hydrocarbon HDS1 enters the first sub- hydroconversion reaction zone R101, the second tunnel poor quality hydrocarbon HDS2 are directly entered the second sub- hydroconversion reaction zone R102 without R101；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, last The reaction effluent of a sub- hydroconversion reaction zone is used as the first hydrogenation reaction effluent R10P.

The present invention, hydrocarbon HDS poor quality hydrocarbon HDS inferior point for two-way branch raw material when, it is characterised in that：

1. the reaction compartment of the first hydrogenation process R10 is divided into the sub- hydroconversion reaction zone of 2 serial operations：First son Hydroconversion reaction zone R101, the second sub- hydroconversion reaction zone R102；

Hydrocarbon HDS inferior points are two-way, and first via poor quality hydrocarbon HDS1 enters the first sub- hydroconversion reaction zone R101, and the second tunnel is inferior Hydrocarbon HDS2 is directly entered the second sub- hydroconversion reaction zone R102；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, the first son Hydroconversion reaction zone reaction effluent R101P enters the second sub- hydroconversion reaction zone R102, the second sub- hydroconversion reaction zone reaction effluent The reaction effluent of last the i.e. sub- hydroconversion reaction zone R102P is used as the first hydrogenation reaction effluent R10P；

First via poor quality hydrocarbon HDS1 accounts for the ratio of all hydrocarbon HDS inferior：Usually 0.10~0.90, generally 0.30~ 0.70, it is preferably 0.40~0.60.

The present invention, when tri- tunnel branch raw materials of hydrocarbon HDS poor qualities hydrocarbon HDS Fen Wei inferior, it is characterised in that：

1. the reaction compartment of the first hydrogenation process R10 is divided into the sub- hydroconversion reaction zone of 3 serial operations：First son Hydroconversion reaction zone R101, the second sub- hydroconversion reaction zone R102, the sub- hydroconversion reaction zone R103 of third；

Tri- tunnels hydrocarbon HDS Fen Wei inferior, first via poor quality hydrocarbon HDS1 enter the first sub- hydroconversion reaction zone R101, and the second tunnel is inferior Hydrocarbon HDS2 is directly entered the second sub- hydroconversion reaction zone R102, and third road poor quality hydrocarbon HDS3 is directly entered the sub- hydroconversion reaction zone of third R103；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, the first son Hydroconversion reaction zone reaction effluent R101P enters the second sub- hydroconversion reaction zone R102, the second sub- hydroconversion reaction zone reaction effluent R102P enters the sub- hydroconversion reaction zone R103 of third, last i.e. height of the sub- hydroconversion reaction zone reaction effluent R103P of third adds hydrogen The reaction effluent of reaction zone is used as the second hydrogenation reaction effluent R10P；

First via poor quality hydrocarbon HDS1 accounts for the ratio of all hydrocarbon HDS inferior：Usually 0.10~0.75, generally 0.15~ 0.5, it is preferably 0.25~0.45, the second tunnel poor quality hydrocarbon HDS2 accounts for the ratio of all hydrocarbon HDS inferior：Usually 0.10~0.75, one As for 0.15~0.5, be preferably 0.25~0.45.

The present invention, when tetra- tunnel branch raw materials of hydrocarbon HDS poor qualities hydrocarbon HDS Fen Wei inferior, it is characterised in that：

1. the reaction compartment of the first hydrogenation process R10 is divided into the sub- hydroconversion reaction zone of 3 serial operations：First son Hydroconversion reaction zone R101, the second sub- hydroconversion reaction zone R102, the sub- hydroconversion reaction zone R103 of third, the 4th sub- hydroconversion reaction zone R104；

Tetra- tunnels hydrocarbon HDS Fen Wei inferior, first via poor quality hydrocarbon HDS1 enter through the first sub- hydroconversion reaction zone R101, the second tunnel Hydrocarbon HDS2 inferior is directly entered the second sub- hydroconversion reaction zone R102, and third road poor quality hydrocarbon HDS3 is directly entered the sub- hydrogenation reaction of third Area R103, the 4th tunnel poor quality hydrocarbon HDS4 are directly entered the 4th sub- hydroconversion reaction zone R104；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, the first son Hydroconversion reaction zone reaction effluent R101P enters the second sub- hydroconversion reaction zone R102, the second sub- hydroconversion reaction zone reaction effluent R102P enters the sub- hydroconversion reaction zone R103 of third, and the sub- hydroconversion reaction zone reaction effluent R103P of third enters the 4th son plus hydrogen is anti- Area R104, the 4th sub- hydroconversion reaction zone reaction effluent R104P i.e. reaction effluent of last sub- hydroconversion reaction zone is answered to make It is used for the second hydrogenation reaction effluent R10P；

First via poor quality hydrocarbon HDS1 accounts for the ratio of all hydrocarbon HDS inferior：Usually 0.05~0.50, generally 0.15~ 0.40, it is preferably 0.20~0.30, the second tunnel poor quality hydrocarbon HDS2 accounts for the ratio of all hydrocarbon HDS inferior：Usually 0.05~0.50, one As for 0.15~0.40, be preferably 0.20~0.30, third road poor quality hydrocarbon HDS32 accounts for the ratio of all hydrocarbon HDS inferior：Usually 0.05~0.50, it is generally 0.15~0.40, is preferably 0.20~0.30.

The present invention, first with hydrogenation process R10, the reaction compartment of First reactor R101E can be divided into Sub- reaction compartment R101E1, R101E2 of few 2 serial operations；

Hydrocarbon HDS inferior points are two-way or demultiplex raw material HDS1, HDS2 etc., and first via poor quality hydrocarbon HDS1 enters the first son Reaction compartment R101E1, the second tunnel poor quality hydrocarbon HDS2 are directly entered the second sub- reaction compartment R101E2, remaining existing branch is bad Matter hydrocarbon, which is directly entered, subsequently corresponds to sub- hydroconversion reaction zone.

The reaction compartment of the present invention, the first hydrogenation process R10, the First reactor R101E used are divided at least 2 Sub- reaction compartment R101E1, R101E2 of a serial operation；

Hydrocarbon HDS inferior points are two-way or demultiplex raw material HDS1, HDS2 etc., and first via poor quality hydrocarbon HDS1 passes through First The bottom inlet of reactor R101E enters the first sub- reaction compartment R101E1, and the second tunnel poor quality hydrocarbon HDS2 is by being arranged in first Fluid distributor in platform reactor R101E enters the second sub- reaction compartment R101E2, remaining existing branch poor quality hydrocarbon passes through The fluid distributor being arranged in First reactor R101E, which enters, subsequently corresponds to sub- reaction zone space.

The present invention, first with hydrogenation process R10, the hydrogenation reactor R10E used, usually 1~3, general It is 1~2.

The present invention, in the first hydrogenation process R10, the hydrogen-containing hydrocarbon stream SHS-TOR10 containing hydrogen supply hydrocarbon SH can be into Enter the first hydrogenation process R10 to contact with the HD components of hydrocarbon HDS inferior or its hydro-conversion object；

The hydrogen supply hydrocarbon SH refers to double ring arene and/or fractional saturation of the normal boiling point higher than 330 DEG C of fractional saturation Polycyclic aromatic hydrocarbon；The ratio between hydrogen supply hydrocarbon SH weight and conventional liquid the hydrocarbon component total weight in logistics SHS-TOR10 in logistics SHS-TOR10 Value is higher by ratio at least 3 weights of hydrogen supply hydrocarbon SH weight and conventional liquid the hydrocarbon component total weight in hydrocarbon HDS inferior in hydrocarbon HDS inferior Measure %；Conventional liquid the hydrocarbon component protium average weight content is higher by the protium weight of hydrocarbon HDS inferior in logistics SHS-TOR10 Content at least 1.5 weight %.

The present invention, hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component total weight ratio in logistics SHS-TOR10：It is usually above 10 weight %, 15 weight %, preferably higher than 20 weight % are generally greater than；

The weight flow SHS-TOR10W and normal boiling point in hydrocarbon HDS inferior for defining hydrogen-containing hydrocarbon stream SHS-TOR10 are higher than The ratio between 450 DEG C weight flow HDW of the hydrocarbon component HD is KSH, i.e. KSH=SHS-TOR10W/HDW, KSH：Usually 0.1~ 10.0., generally 0.5~5.0, be preferably 1.0~3.0.

The present invention, first with hydrogenation process R10, there are when the sub- hydroconversion reaction zone of 2 or multiple serial operations, supplies Hydrogen hydrocarbon stream SHS-TOR10 can fully enter the first sub- hydroconversion reaction zone R101.

The present invention, first with hydrogenation process R10, there are when the sub- hydroconversion reaction zone of 2 or multiple serial operations, The 30~60% of hydrogen-containing hydrocarbon stream SHS-TOR10 can be used as first via hydrogen-containing hydrocarbon stream SHS-TOR101 to enter the first son plus hydrogen Reaction zone R101, remaining hydrogen-containing hydrocarbon stream SHS-TOR10X enter other sub- hydroconversion reaction zones.

The present invention, hydrogen-containing hydrocarbon stream SHS-TOR10 can come from processing hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF's The hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target is prepared as with hydrogen supply hydrocarbon；Hydrogen supply hydrocarbon in logistics SHS-TOR10 SH weight accounts for conventional liquid the hydrocarbon component total weight ratio and is higher than 6 weight %；KSH=0.1~10.

The present invention can be hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF with coal tar light fraction when processing coal tar heavy oil, It is characterized in that：

Hydrocarbon HDS inferior is the logistics that the hydrocarbon component HD mainly by normal boiling point higher than 450 DEG C from coal tar is formed；

Hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component total weight ratio higher than 10 weights in hydrogen-containing hydrocarbon stream SHS-TOR10 Measure %；

KSH=0.2~5；

Hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF is selected from one or more of following logistics：

1. the logistics for the coalite tar fractional composition for being mainly 350~450 DEG C by normal boiling point；

2. the logistics for the medium temperature coal tar fractional composition for being mainly 350~450 DEG C by normal boiling point；

3. the logistics for the high temperature coal-tar fractional composition for being mainly 230~450 DEG C by normal boiling point；

4. mainly by being 120~350 DEG C of fractions and the low temperature that normal boiling point is 350~450 DEG C of fractions comprising normal boiling point The logistics of coal tar fraction composition；

5. mainly by being 120~350 DEG C of fractions and the medium temperature that normal boiling point is 350~450 DEG C of fractions comprising normal boiling point The logistics of coal tar fraction composition；

6. being mainly 120~350 DEG C of fractions by the normal boiling point after dephenolize and normal boiling point is 350~450 DEG C of fractions The logistics of coalite tar fractional composition；

7. being mainly 120~350 DEG C of fractions by the normal boiling point after dephenolize and normal boiling point is 350~450 DEG C of fractions The logistics of medium temperature coal tar fractional composition.

The present invention processes coal tar heavy oil and using coal tar light fraction MF as hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF When, it is characterised in that：

In the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen supply hydrocarbon, what it is from coal tar is mainly 350 by normal boiling point The logistics MFS of~450 DEG C of hydrocarbon MF compositions carries out hydrogen supply hydrocarbon hydrogenation reaction HPU1R processed, and at least part the hydrocarbon component MF completes to add Hydrogen modified-reaction obtains hydrogenation reaction effluent HPU1P, the hydrogen-containing hydrocarbon stream SHS- obtained based on hydrogenation reaction effluent HPU1P TOR10 is selected from the one or several of following logistics：

1. reaction effluent HPU1P is used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS-TOR10 and logistics HDS Enter the first hydrogenation process R10 after mixing；

2. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and heat Gas separated by high pressure separator HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS-TOR10 enters the first hydrogenation process R10 after being mixed with logistics HDS；

3. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and heat Gas separated by high pressure separator HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS-TOR10 enters hydroconversion reaction zone HPU21, gained liquid after the hot high score oil HPU1-HSO decompressions of at least part, degassing HPU1-HSOA enters the first hydrogenation process R10 after being mixed with logistics HDS；

4. reaction effluent HPU1P, which enters cold anticyclone separation process HPU1-CS, is separated into cold high score oil HPU1-CSO and cold Gas separated by high pressure separator HPU1-CSV, the cold high score oil HPU1-CSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS-TOR10 enters the first hydrogenation process R10 after being mixed with logistics HDS；

5. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；In hydrogenated oil HPU1PO fractionating sections, separation hydrogenated oil HPU1PO obtain the logistics rich in hydrogen supply the hydrocarbon component, are rich in supply at least partially The logistics of hydrogen the hydrocarbon component is used as hydrogen-containing hydrocarbon stream SHS-TOR10, and hydrogen-containing hydrocarbon stream SHS-TOR10 enters after being mixed with logistics HDS First hydrogenation process R10；

6. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；In hydrogenated oil HPU1PO fractionating sections, separation hydrogenated oil HPU1PO obtain the logistics rich in hydrogen supply the hydrocarbon component, at least part mainly by The logistics rich in hydrogen supply the hydrocarbon component composition that normal boiling point is 350~450 DEG C is used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen supply hydrocarbon Logistics SHS-TOR10 enters the first hydrogenation process R10 after being mixed with logistics HDS.

The present invention processes coal tar heavy oil and using coal tar light fraction LMF as hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF When, it is characterised in that：

In the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen supply hydrocarbon, from coal tar containing normal boiling point be 60~ The logistics LMFS of 450 DEG C of hydrocarbon LMF completes deep hydrofinishing reaction HPU1R and is converted into hydrogenation reaction effluent HPU1P, conventional to boil Point is converted into naphtha and diesel component for 60~350 DEG C of hydrocarbon, and normal boiling point is that 350~450 DEG C of hydrocarbon is converted into rich in confession The hydrogenation tail oil of hydrogen hydrocarbon SH is selected from following logistics based on the obtained hydrogen-containing hydrocarbon stream SHS-TOR10 of hydrogenation reaction effluent HPU1P It is one or several：

1. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and heat Gas separated by high pressure separator HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS-TOR10 enters the first hydrogenation process R10 after being mixed with logistics HDS；

2. the intermediate reaction effluent HPU1MP for being prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon enters thermal high Separation process HPU1M-HS is separated into hot high score oil HPU1M-HSO and hot gas separated by high pressure separator HPU1MP-HSV, the hot high score of at least part Oily HPU1M-HSO is used as hydrogen-containing hydrocarbon stream SHS-TOR10, and hydrogen-containing hydrocarbon stream SHS-TOR10 enters hydroconversion reaction zone HPU21, until Into the after gained degassing oil HPU1M-HSOA is mixed with logistics HDS after few a part of hot high score oil HPU1M-HSO decompressions degassing One hydrogenation process R10；

3. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；In hydrogenated oil HPU1PO fractionating sections, separation hydrogenated oil HPU1PO obtain the logistics rich in hydrogen supply the hydrocarbon component, are rich in supply at least partially The logistics of hydrogen the hydrocarbon component is used as hydrogen-containing hydrocarbon stream SHS-TOR10, and hydrogen-containing hydrocarbon stream SHS-TOR10 enters after being mixed with logistics HDS First hydrogenation process R10；

4. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；In hydrogenated oil HPU1PO fractionating sections, separation hydrogenated oil HPU1PO obtain the logistics rich in hydrogen supply the hydrocarbon component, at least part mainly by The logistics rich in hydrogen supply the hydrocarbon component composition that normal boiling point is 350~450 DEG C is used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen supply hydrocarbon Logistics SHS-TOR10 enters the first hydrogenation process R10 after being mixed with logistics HDS.

The present invention, in the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen supply hydrocarbon, to produce hydrogen supply hydrocarbon to greatest extent as mesh Mark.

Hydrogen-containing hydrocarbon stream SHS-TOR10 can be contained often from what the second hydrogenation reaction effluent R20P of separation was obtained Advise the distillate that boiling point is 300~490 DEG C of the hydrocarbon components.

Hydrogen-containing hydrocarbon stream SHS-TOR10 can be contained often from what the second hydrogenation reaction effluent R20P of separation was obtained Advise the distillate that boiling point is 330~450 DEG C of the hydrocarbon components.

Hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF can be obtained from the second hydrogenation reaction effluent R20P of separation Contain normal boiling point be 300~490 DEG C of the hydrocarbon components distillate.

Hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF can be obtained from the second hydrogenation reaction effluent R20P of separation Contain normal boiling point be 330~450 DEG C of the hydrocarbon components distillate.

The present invention, hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF, the coal that can be mainly 350~450 DEG C by normal boiling point Tarry distillate forms；At this point, the operating condition for being prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon is：Temperature be 250~ 460 DEG C, pressure be 6.0~30.0MPa, hydrogen/feedstock oil volume ratio is 300: 1~3000: 1, hydrogenation catalyst HPU3-CAT Volume space velocity is 0.05~5.0hr^-1；Hydrocarbon HDS weight chemistry hydrogen consumption inferior is 0.5~4.5% weight.

The present invention, in the second hydrogenation process R20, the hydrogenation catalyst R20C used can be a kind of composite briquette Hydrogenation of tar catalyst, including high-activity component and low activity component；The high-activity component metal and low activity component metals Weight ratio be 1: 1000 to 1: 10；The high-activity component be molybdenum, nickel, cobalt or tungsten metal water soluble salt compound or its Mixture；The low activity group is divided into ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, urges Agent water content is less than 2wt%, the powdered granule that particle diameter is 1~100 μm.

The present invention, in the second hydrogenation process R20, the second hydrogenation reaction R20R, including at least part liquid hydrocarbon is former Expect HDSL in the hydrocarbon component HD hydrofining reaction, including at least part liquid hydrocarbon feeds HDSL the hydrocarbon component HD heat from hydrogenation Cracking reaction；

Second hydrogenation process R20, the hydrogenation catalyst R10C used can include at least Mo elements, and Mo is second The body of work form of hydrogenation process R20 is M₀S₂。

The present invention, in the second hydrogenation process R20, the second hydrogenation reaction R20R, the hydrogenation catalyst R20C used can To include at least semicoke solid particle.

The present invention can be arranged and add hydrogen upgrading reaction process R60, in hydrogen and plus hydrogen upgrading catalyst R60C existence conditions Under, the logistics SRLX of at least part liquid stream SRL or the removing solid particle based on logistics SRL is carried out plus hydrogen upgrading is anti- R60R is answered to obtain adding hydrogen upgrading reaction product R60P, it is imurity-removal or reduction hydrocarbon ils density to add the effect of hydrogen upgrading reaction R60R Or it reduces hydrocarbon ils boiling point or improves Cetane number；

Deep hydrogenation modification reaction R60R includes the one or more of following reaction：

1. aromatic hydrocarbons deep hydrogenation saturated reaction；

2. hydro carbons deep hydrogenation denitrification reaction；

3. cycloalkane adds hydrogen ring-opening reaction；

4. hydrocarbon hydrocracking reacts；

5. hydrocarbons hydrogenation isomerization reaction.

The present invention, in general, described plus hydrogen upgrading reaction process R60 operating condition is：Temperature is 250~440 DEG C, pressure It is 4.0~30.0MPa, hydrogen upgrading catalyst R60C volume space velocities is added to be 0.02~10.0hr^-1, hydrogen/feedstock oil volume ratio be 300: 1~4000: 1；It is a kind of catalyst or 2 kinds of catalyst combinations uses or multiple catalysts group to add hydrogen upgrading catalyst R60C It closes and uses.

The present invention, when hydrocarbon HDS inferior comes from coal tar, each step operation condition is usually：

(1) hydrocarbon HDS inferior comes from coal tar, and gum asphaltic content is 10~90%, carbon residue is 0.01~25%, gold Category content is 2~2000PPm；

(2) second hydrogenation process R20, organic oxygen hydrogenation and removing rate are more than 40%, gum asphalt hydrogenation and removing rate It is more than 35% more than 40%, carbon residue hydrogenation and removing rate, metal hydrogenation removal efficiency is more than 60%.

The present invention, when hydrocarbon HDS inferior comes from coal tar, each step operation condition is generally：

(2) hydrocarbon HDS inferior comes from coal tar, and gum asphaltic content is 40~80%, carbon residue is 5~20%, metal Content is 50~700PPm；

Second hydrogenation process R20, organic oxygen hydrogenation and removing rate are more than 60%, gum asphalt hydrogenation and removing rate and are more than 60%, carbon residue hydrogenation and removing rate is more than 70%, and metal hydrogenation removal efficiency is more than 80%.

The conversion ratio that is hydrocracked of (2) second hydrogenation process R20, the hydrocarbon component HD are more than 25%.

The conversion ratio that is hydrocracked of second hydrogenation process R20, the hydrocarbon component HD are more than 45%.

The present invention, in the second hydrogenation process R20, by the end product of the second hydrogenation process R20 or intermediate production Object is considered as reaction product R20MP, and thermal high separation process R20MP-THPS can be arranged；

It is obtained containing dissolving hydrogen, conventional boiling in thermal high separation process R20MP-THPS, separation reaction effluent R10MP The hot high score liquid R20MP-THPS-L and net product stream R20MP-THPS-PP of conventional liquid hydrocarbon of the point higher than 350 DEG C, Solids may be contained in R20MP-THPS-L；Net product stream R20MP-THPS-PP enters the adjacent hydroconversion reaction zone in downstream；

The logistics R20MP-THPS-LR return comprising hydrocarbon liquids based on hot high score liquid R20MP-THPS-L belongs to the The upstream hydroconversion reaction zone R20Z of two hydrogenation process R20 is used as cycle liquid phase；

Define the weight flow rate and upstream hydroconversion reaction zone R20Z and the upstreams R20Z whole hydrogenation reaction of R20MP-THPS-LR The ratio between the total weight flow rate of hydrocarbon HDS raw materials inferior in area is recycle ratio KR200, recycle ratio KR200：Usually 0.05~30, one As be 2~10.

The first way of thermal high separation process R20MP-THPS, which is arranged, is：

(2) in the second hydrogenation process R20, in sub- hydroconversion reaction zone setting thermal high separation process R20MP-THPS；

Thermal high separation process RTHPS, is arranged the upper space in hydrogenation reactor, with liquid header, drain pipeline, The system that circulating pump, liquor charging pipeline form makes R20MP-THPS-LR inject in the R20Z of upstream hydrogenation reaction space.

The second way of thermal high separation process R20MP-THPS, which is arranged, is：

Thermal high separation process R20MP-THPS is completed in independent high pressure hot separator R20MP-THPS-E；

In high pressure hot separator R20MP-THPS-E, separation reaction effluent R10MP is obtained containing dissolving hydrogen, routine The hot high score liquid R20MP-THPS-L and net product stream R20MP-THPS-PP of conventional liquid hydrocarbon of the boiling point higher than 350 DEG C, Solids may be contained in R20MP-THPS-L；Net product stream R20MP-THPS-PP enters the adjacent sub- hydrogenation reaction in downstream Area.

The present invention divides SR in removal process, and thermal high separation process THPS can be arranged：

It obtains adding hydrogen containing hydrogen, impurity in thermal high separation process THPS, the second hydrogenation reaction effluent R20P of separation Product, conventional gas hydrocarbon and normal boiling point are less than the hot high score gas THPS-V of 350 DEG C of conventional liquid hydrocarbon and contain dissolved hydrogen It may contain solids in hot high score the liquid THPS-L, THPS-L of the conventional liquid hydrocarbon of gas, normal boiling point higher than 350 DEG C；

The operating condition of thermal high separation process THPS is usually：Temperature is 250~460 DEG C, pressure be 4.0~ 30.0MPa；

The operating condition of thermal high separation process THPS is generally：Temperature is 350~440 DEG C, pressure be 10.0~ 25.0MPa；

Part, the logistics for including hydrocarbon liquids based on hot high score liquid THPS-L are shunted in hot high score liquid R10P-SL THPS-LR returns to the second hydrogenation process R20；Define the weight flow rate that normal boiling point in THPS-LR is more than 450 DEG C of the hydrocarbon components It is recycle ratio K999, recycle ratio K999 with the ratio between weight flow rate of HD components in hydrocarbon raw material HDS inferior：Usually 0.05~10, Generally 0.5~2.

The present invention divides SR in removal process, can be arranged cold anticyclone separation process LHPS, cold low separation process LLPS, Cold low point of oil cycle washing methane process：

In cold anticyclone separation process LHPS, flowing out comprising the second hydrogenation reaction based on the second hydrogenation reaction effluent R20P The logistics R10P-H100 of most of hydrogen component is separated into the hydrogen rich gas gas being mainly made of hydrogen in volume in object R20P The body LHPS-V and liquid stream LHPS-L being mainly made of conventional liquid hydrocarbon；Hydrogen rich gas gas LHPS-V is used as SRV；

Cold low point rich in conventional gas hydrocarbon is separated into after cold low separation process LLPS, liquid stream LHPS-L decompressions The gas LLPS-V and and liquid stream LLPS-L that is mainly made of conventional liquid hydrocarbon；

First part liquid stream LLPS-L is used as absorbing oil LLPS-LA, and based on the second hydrogenation reaction effluent R20P The logistics R10P-H100 mixing comprising most of hydrogen component in the second hydrogenation reaction effluent R20P after into cold anticyclone point From process LHPS；Remainder liquid stream LLPS-L is used as cold low point of oily product LLPS-LP；

In general, the operating condition of cold anticyclone separation process LHPS is：Temperature is 20~70 DEG C, pressure be 6.0~ 30.0MPa；

In general, the operating condition of cold low separation process LLPS is：Temperature is 20~70 DEG C, pressure be 0.01~ 3.0MPa；

Generally, the operating condition of cold anticyclone separation process LHPS is：Temperature is 20~50 DEG C, pressure be 8.0~ 25.0MPa；、

Generally, the operating condition of cold low separation process LLPS is：Temperature is 20~50 DEG C, pressure is 0.2~1.0MPa；

Definition absorbs the ratio between the weight flow rate of oil LLPS-LA and cold low point of oily product LLPS-LP weight flow rates to absorb oil Recycle ratio K300, K300 are usually 0.05~10, generally 0.5~4.

In the second hydrogenation process R20, when using hydrogenation catalyst R20C, the structure of up flow type hydrogenation reactor R20E Form, can be in following a kind or several：

1. suspension bed；

2. ebullated bed；

3. moving bed.

In the second hydrogenation process R20, existing solid particle can be selected from one of the following or several：

2. catalyst granules；

3. iron rust particle；

4. particles of inorganic material；

5. coking of coal process generate into the solid particle in coal tar；

7. the solid particle from shale；

8. the solid particle from oil-sand；

9. other particles being present in the second hydrogenation reaction product BASE-R20P.

The present invention, when hydrocarbon HDS inferior comes from coal tar, the operating condition of the second hydrogenation process R20 is：

(1) coal tar is come from the first hydrogenation process R10, hydrocarbon HDS inferior；

(2) in the second hydrogenation process R20, the operating condition of the second hydrogenation process R20 is：Temperature be 300~ 480 DEG C, pressure be 6.0~30.0MPa, hydrogen/feedstock oil volume ratio is 300: 1~4000: 1, hydrogenation catalyst R10C is added Weight is the 0.001~8.0% of HDS weight, volume space velocity is 0.1~10.0hr^-1；Hydrocarbon HDS weight chemistry hydrogen consumption inferior is 0.5~5.0%.

The present invention, the reaction compartment of the second hydrogenation process R20, the son that can be divided into 2 or multiple serial operations add Hydroformylation reaction zone：First sub- hydroconversion reaction zone R201, second sub- hydroconversion reaction zone R202 etc.；

R10P-XO-TOR20 points of logistics is two-way or demultiplex raw material, and first via logistics R10P-XO-TOR201 enters First sub- hydroconversion reaction zone R201, the second tunnel logistics R10P-XO-TOR202 are directly entered the second sub- hydrogenation reaction without R201 Area R202；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, last The reaction effluent of a sub- hydroconversion reaction zone is used as the second hydrogenation reaction effluent R20P.

The present invention can be divided into two tunnels, first via logistics in the second hydrogenation process R20, logistics R10P-XO-TOR20 R10P-XO-TOR201 enters the first sub- hydroconversion reaction zone R201, and the second tunnel logistics R10P-XO-TOR202 is directly entered the second son Hydroconversion reaction zone R202；

The ratio that first via logistics R10P-XO-TOR201 accounts for whole logistics R10P-XO-TOR20 is 0.40~0.60.

The present invention can be divided into three tunnels, first via logistics in the second hydrogenation process R20, logistics R10P-XO-TOR20 R10P-XO-TOR201 enters the first sub- hydroconversion reaction zone R201, and the second tunnel logistics R10P-XO-TOR202 is directly entered the second son Hydroconversion reaction zone R202, third road logistics R10P-XO-TOR203 are directly entered the sub- hydroconversion reaction zone R203 of third；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, the first son Hydroconversion reaction zone reaction effluent R201P enters the second sub- hydroconversion reaction zone R202, the second sub- hydroconversion reaction zone reaction effluent R202P enters the sub- hydroconversion reaction zone R203 of third, last i.e. height of the sub- hydroconversion reaction zone reaction effluent R203P of third adds hydrogen The reaction effluent of reaction zone is used as the second hydrogenation reaction effluent R20P；

First via logistics R10P-XO-TOR201 accounts for the ratio of whole logistics R10P-XO-TOR20：Usually 0.1~ 0.75, it is generally 0.15~0.50, is preferably 0.25~0.45, the second tunnel logistics R10P-XO-TOR202 accounts for whole logistics R10P- The ratio of XO-TOR20：Usually 0.1~0.75, generally 0.15~0.50 it is preferably, 0.25~0.45.

The present invention can be divided into four tunnels, first via logistics in the second hydrogenation process R20, logistics R10P-XO-TOR20 R10P-XO-TOR201 enters the first sub- hydroconversion reaction zone R201, and the second tunnel logistics R10P-XO-TOR202 is directly entered the second son Hydroconversion reaction zone R202, third road logistics R10P-XO-TOR203 are directly entered the sub- hydroconversion reaction zone R203 of third, the 4th road object Stream R10P-XO-TOR204 is directly entered the 4th sub- hydroconversion reaction zone R204；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, the first son Hydroconversion reaction zone reaction effluent R201P enters the second sub- hydroconversion reaction zone R202, the second sub- hydroconversion reaction zone reaction effluent R202P enters the sub- hydroconversion reaction zone R203 of third, and the sub- hydroconversion reaction zone reaction effluent R203P of third enters the 4th son plus hydrogen is anti- Area R204, the 4th sub- hydroconversion reaction zone reaction effluent R204P i.e. reaction effluent of last sub- hydroconversion reaction zone is answered to make It is used for the second hydrogenation reaction effluent R20P；

First via logistics R10P-XO-TOR201 accounts for the ratio of whole logistics R10P-XO-TOR20：Usually 0.05~ 0.5, it is generally 0.15~0.4, is preferably 0.20~0.30, the second tunnel logistics R10P-XO-TOR202 accounts for whole logistics R10P-XO- The ratio of TOR20：Usually 0.05~0.5, generally 0.15~0.4 it is preferably, 0.20~0.30, third road logistics R10P-XO- TOR203 accounts for the ratio of whole logistics R10P-XO-TOR20：Usually 0.05~0.5, generally 0.15~0.4 it is preferably, 0.20 ~0.30.

The present invention, in removal process SR, the H2 volumetric concentrations of hydrogen rich gas gas SRV：Typically larger than 75%, generally higher than 85%.

The present invention, in the second hydrogenation process R20, hydrogen-containing hydrocarbon stream SHS-TOR20, Ke Yijin containing hydrogen supply hydrocarbon SH Enter the second hydrogenation process R20 to contact with R10P-XO-TOR20 or its hydro-conversion object；

The hydrogen supply hydrocarbon SH refers to double ring arene and/or fractional saturation of the normal boiling point higher than 330 DEG C of fractional saturation Polycyclic aromatic hydrocarbon；The ratio between hydrogen supply hydrocarbon SH weight and conventional liquid the hydrocarbon component total weight in logistics SHS-TOR20 in logistics SHS-TOR20 It is worth, hydrogen supply hydrocarbon SH weight and conventional liquid the hydrocarbon component gross weight in logistics R10P-XO-TOR20 in high effluent stream R10P-XO-TOR20 The ratio of amount at least 3 weight %；The high effluent stream of conventional liquid the hydrocarbon component protium average weight content in logistics SHS-TOR20 The protium weight content of the conventional liquid hydrocarbon of R10P-XO-TOR20 at least 1.5 weight %.

The present invention, hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component total weight ratio in logistics SHS-TOR20：It is usually above 10 weight %, 15 weight %, preferably are generally greater than higher than 20 weight %；

It defines conventional in the weight flow SHS-TOR20W and logistics R10P-XO-TOR20 of hydrogen-containing hydrocarbon stream SHS-TOR20 The ratio between the weight flow R10P-XO-TOR20-HDW of the hydrocarbon component HD of boiling point higher than 450 DEG C is KSH200, i.e. KSH200=SHS- TOR20W/R10P-XO-TOR20-HDW, KSH200：Usually 0.1~10.0, generally 0.5~5.0 it is preferably, 1.0~3.0.

The present invention, the second hydrogenation process R20 can be divided into the sub- hydroconversion reaction zone of at least two serial operation, hydrogen supply Hydrocarbon stream SHS-TOR20 fully enters the first sub- hydroconversion reaction zone R201.

The present invention, the second hydrogenation process R20 can be divided into the sub- hydroconversion reaction zone of at least two serial operation, hydrogen supply The 30~60% of hydrocarbon stream SHS-TOR20 enter the first sub- hydroconversion reaction zone as first via hydrogen-containing hydrocarbon stream SHS-TOR201 R201, remaining hydrogen-containing hydrocarbon stream SHS-TOR20X enter other sub- hydroconversion reaction zones.

The present invention, hydrogen-containing hydrocarbon stream SHS-TOR20 can come from processing hydrogen supply hydrocarbon precursor logistics SHS-TOR20BF's The hydrogenation reaction effluent HPU1P of the hydroconversion reaction zone HPU1 of target is prepared as with hydrogen supply hydrocarbon；In hydrogen-containing hydrocarbon stream SHS-TOR20 Hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component total weight ratio and is higher than 6 weight %；KSH200=0.1~10.

The present invention, process coal tar heavy oil when can using coal tar light fraction as hydrogen supply hydrocarbon precursor logistics SHS-TOR20BF, It is characterized in that：

Hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component total weight ratio higher than 10 weights in hydrogen-containing hydrocarbon stream SHS-TOR20 Measure %；

K=0.2~5；

Hydrogen supply hydrocarbon precursor logistics SHS-TOR20BF is selected from one or more of following logistics：

The present invention processes coal tar heavy oil and using coal tar light fraction MF as hydrogen supply hydrocarbon precursor logistics SHS-TOR20BF When, it is characterised in that：

In the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen supply hydrocarbon, what it is from coal tar is mainly 350 by normal boiling point The logistics MFS of~450 DEG C of hydrocarbon MF compositions carries out hydrogen supply hydrocarbon hydrogenation reaction HPU1R processed, and at least part the hydrocarbon component MF completes to add Hydrogen modified-reaction obtains hydrogenation reaction effluent HPU1P, the hydrogen-containing hydrocarbon stream SHS- obtained based on hydrogenation reaction effluent HPU1P TOR20 is selected from the one or several of following logistics：

1. reaction effluent HPU1P is used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS-TOR20 and logistics HDS Enter the second hydrogenation process R20 after mixing；

2. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and heat Gas separated by high pressure separator HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS-TOR20 enters the second hydrogenation process R20 after being mixed with logistics HDS；

3. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and heat Gas separated by high pressure separator HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS-TOR20 enters the second hydrogenation process R20, gained liquid after the hot high score oil HPU1-HSO decompressions of at least part, degassing Body HPU1-HSOA enters the second hydrogenation process R20 after being mixed with logistics HDS；

4. reaction effluent HPU1P, which enters cold anticyclone separation process HPU1-CS, is separated into cold high score oil HPU1-CSO and cold Gas separated by high pressure separator HPU1-CSV, the cold high score oil HPU1-CSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS-TOR20 enters the second hydrogenation process R20 after being mixed with logistics HDS；

5. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；In hydrogenated oil HPU1PO fractionating sections, separation hydrogenated oil HPU1PO obtain the logistics rich in hydrogen supply the hydrocarbon component, are rich in supply at least partially The logistics of hydrogen the hydrocarbon component is used as hydrogen-containing hydrocarbon stream SHS-TOR20, and hydrogen-containing hydrocarbon stream SHS-TOR20 enters after being mixed with logistics HDS Second hydrogenation process R20；

6. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；In hydrogenated oil HPU1PO fractionating sections, separation hydrogenated oil HPU1PO obtain the logistics rich in hydrogen supply the hydrocarbon component, at least part mainly by The logistics rich in hydrogen supply the hydrocarbon component composition that normal boiling point is 350~450 DEG C is used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen supply hydrocarbon Logistics SHS-TOR20 enters the second hydrogenation process R20 after being mixed with logistics HDS.

The present invention processes coal tar heavy oil and using coal tar light fraction LMF as hydrogen supply hydrocarbon precursor logistics SHS-TOR20BF When, it is characterised in that：

In the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen supply hydrocarbon, from coal tar containing normal boiling point be 60~ The logistics LMFS of 450 DEG C of hydrocarbon LMF completes deep hydrofinishing reaction HPU1R and is converted into hydrogenation reaction effluent HPU1P, conventional to boil Point is converted into naphtha and diesel component for 60~350 DEG C of hydrocarbon, and normal boiling point is that 350~450 DEG C of hydrocarbon is converted into rich in confession The hydrogenation tail oil of hydrogen hydrocarbon SH is selected from following logistics based on the obtained hydrogen-containing hydrocarbon stream SHS-TOR20 of hydrogenation reaction effluent HPU1P It is one or several：

1. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and heat Gas separated by high pressure separator HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS-TOR20 enters the second hydrogenation process R20 after being mixed with logistics HDS；

2. the intermediate reaction effluent HPU1MP for being prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon enters thermal high Separation process HPU1M-HS is separated into hot high score oil HPU1M-HSO and hot gas separated by high pressure separator HPU1MP-HSV, the hot high score of at least part Oily HPU1M-HSO is used as hydrogen-containing hydrocarbon stream SHS-TOR20, and hydrogen-containing hydrocarbon stream SHS-TOR10 enters hydroconversion reaction zone HPU21, until Into the after gained degassing oil HPU1M-HSOA is mixed with logistics HDS after few a part of hot high score oil HPU1M-HSO decompressions degassing Two hydrogenation process R20；

3. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；In hydrogenated oil HPU1PO fractionating sections, separation hydrogenated oil HPU1PO obtain the logistics rich in hydrogen supply the hydrocarbon component, are rich in supply at least partially The logistics of hydrogen the hydrocarbon component is used as hydrogen-containing hydrocarbon stream SHS-TOR20, and hydrogen-containing hydrocarbon stream SHS-TOR20 enters after being mixed with logistics HDS Second hydrogenation process R20；

4. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；In hydrogenated oil HPU1PO fractionating sections, separation hydrogenated oil HPU1PO obtain the logistics rich in hydrogen supply the hydrocarbon component, at least part mainly by The logistics rich in hydrogen supply the hydrocarbon component composition that normal boiling point is 350~450 DEG C is used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen supply hydrocarbon Logistics SHS-TOR20 enters the second hydrogenation process R20 after being mixed with logistics HDS.

The present invention, in the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen-containing hydrocarbon stream SHS-TOR20, to make to greatest extent It is target to take hydrogen supply hydrocarbon.

The present invention, hydrogen-containing hydrocarbon stream SHS-TOR20 can be obtained from the second hydrogenation reaction effluent R20P of separation Contain the distillate that normal boiling point is 300~490 DEG C of the hydrocarbon components.

The present invention, hydrogen-containing hydrocarbon stream SHS-TOR20 can be obtained from the second hydrogenation reaction effluent R20P of separation Contain the distillate that normal boiling point is 330~450 DEG C of the hydrocarbon components.

The present invention, hydrogen supply hydrocarbon precursor logistics SHS-TOR20BF can be from the second hydrogenation reaction effluent of separation The distillate containing normal boiling point for 300~490 DEG C of the hydrocarbon components that R20P is obtained.

The present invention, hydrogen supply hydrocarbon precursor logistics SHS-TOR20BF can be from the second hydrogenation reaction effluent of separation The distillate containing normal boiling point for 330~450 DEG C of the hydrocarbon components that R20P is obtained.

The present invention can be divided into the roads N branch feed stream in the second hydrogenation process R20, logistics R10P-XO-TOR20 R10P-XO-TOR201, logistics R10P-XO-TOR202 ..., logistics R10P-XO-TOR20N, wherein N >=2；

It is M, M >=N+1 in the number of units of the second hydrogenation process R20, the up-flow reactor R20E used；

Branch poor quality hydrocarbon R10P-XO-TOR20X enters X platform up-flow reactor R20XE；

The logistics R20NE-SL being mainly made of liquid phase is obtained from the inner space of N platform up-flow reactors R20NE, until Few a part of logistics R20NE-SL is recycled back into the reaction compartment of the arbitrary reactor within the scope of R201E to R20NE；

The logistics R20ME-SL being mainly made of liquid phase is obtained from the inner space of M platform up-flow reactors R1ME, until Few a part of logistics R20ME-SL is recycled back to the reaction compartment of any one reactor after reactor R20NE.

The present invention, in the first hydrogenation process R10, when hydrocarbon HDS inferior comes from coal tar, the second hydrogenation process The operating condition of R20 is usually：Temperature is 300~500 DEG C, pressure is 6.0~30.0MPa, hydrogen/feedstock oil volume ratio is 300: 1~4000: 1, hydrogenation catalyst R20C be added weight be the 0.001~8.0% of HDS weight, volume space velocity be 0.1~ 10.0hr^-1；

The operating condition of second hydrogenation process R20 is generally：Temperature is 350~460 DEG C, pressure be 10.0~ 25.0MPa, hydrogen/feedstock oil volume ratio are 300: 1~2000: 1, hydrogenation catalyst R10C addition weight is HDS weight 0.01~5.0%, volume space velocity is 0.2~5.0hr^-1；

The operating condition of second hydrogenation process R20 is preferably：Temperature is 380~460 DEG C, pressure be 17.0~ 23.0MPa, hydrogen/feedstock oil volume ratio are 500: 1~1200: 1, hydrogenation catalyst R10C addition weight is the 0.3 of HDS weight ~3.0%, volume space velocity is 0.3~2.0hr^-1。

The present invention, when hydrocarbon HDS inferior comes from coal tar, operating target in detail is usually：

Carried out in the first hydrogenation process R10, hydrocarbon HDS inferior with add based on hydrogen aromatic hydrocarbons either shallow saturated reaction first plus Hydrogen reacts R10R, and gum asphalt hydrogenation and removing rate is more than 3%, carbon residue hydrogenation and removing rate and is more than 3%；

(2) in the second hydrogenation process R20, the second hydrogenation reaction effluent R20P conventional liquid hydrocarbon protium weight It measures content and is higher than 9.0%；

In the second hydrogenation process R20, hydrocarbon HDS weight chemistry hydrogen consumption inferior is higher than 1.5%；

It is more than 50% in the de- carbon yield of the second hydrogenation process R20, hydrocarbon HDS inferior；

It is more than 25% in the conversion ratio that is hydrocracked of the second hydrogenation process R20, hydrocarbon HDS inferior.

The present invention when hydrocarbon HDS inferior comes from coal tar, operates target and is generally in detail：

(1) hydrocarbon HDS inferior comes from coal tar, and gum asphaltic content is 40~80%, carbon residue is 5~20%, metal Content is 50~700PPm；

Carried out in the first hydrogenation process R10, hydrocarbon HDS inferior with add based on hydrogen aromatic hydrocarbons either shallow saturated reaction first plus Hydrogen reacts R10R, and gum asphalt hydrogenation and removing rate is more than 5%, carbon residue hydrogenation and removing rate and is more than 5%；

(2) in the second hydrogenation process R20, hydrocarbon HDS inferior in coal tar, the second hydrogenation reaction effluent R20P The protium weight content of conventional liquid hydrocarbon is higher than 10.0%；

In the second hydrogenation process R20, hydrocarbon HDS weight chemistry hydrogen consumption inferior is higher than 2.5%；

It is more than 70% in the de- carbon yield of the second hydrogenation process R20, hydrocarbon HDS inferior；

It is more than 40% in the conversion ratio that is hydrocracked of the second hydrogenation process R20, hydrocarbon HDS inferior.

The present invention, the hydrogenation reactor R20X that the second hydrogenation process R20 is used：Usually 1~5, generally 2~ 4.

The present invention, the coal tar that hydrogen supply hydrocarbon precursor logistics SHS-TOR20-BF is mainly 350~450 DEG C by normal boiling point When fractional composition, the operating condition that the hydroconversion reaction zone HPU1 of target is prepared as with hydrogen supply hydrocarbon is：Temperature is 250~460 DEG C, presses Power is 6.0~30.0MPa, hydrogen/feedstock oil volume ratio is 300: 1~3000: 1, hydrogenation catalyst HPU3-CAT volume space velocities For 0.05~5.0hr^-1；Hydrocarbon HDS weight chemistry hydrogen consumption inferior is 0.5~4.5% weight.

The present invention can make at least part hydrogen rich gas gas SRV as hydrogen SRV-C to be purified in recovery section SR It is separated into purifying hydrogen of hydrogen SRV-CH and purification tail gas SRV-CC, at least part purifying hydrogen of hydrogen into hydrogen purification unit GH100 SRV-CH returns to hydrogenation process and recycles.

The present invention, hydrocarbon HDS inferior whens containing organic oxygen, can recycle the second hydrogenation reaction effluent in removal process SR R20P obtains the hydrogen rich gas gas SRV being mainly made of hydrogen in volume and the liquid stream being mainly made of conventional liquid hydrocarbon SRL, at least first part's hydrogen rich gas gas SRV return to the second hydrogenation process R20 as reaction process circulating hydrogen SRV-TO-R10 is recycled, at least second part hydrogen rich gas gas SRV and containing based on the second hydrogenation reaction effluent R20P Being used as after the logistics R10P-HH mixing for having most of hydrogen in the second hydrogenation reaction effluent R20P, most of vapor reduces The circulating hydrogen SRV-200 of steam partial pressure is recycled；

Circulating hydrogen SRV-TO-R1 is finally recycled into hydrogen rich gas gas SRV；

Circulating hydrogen SRV-R200 is finally recycled into hydrogen rich gas gas SRV.

Based on the present invention, the 1st kind of detailed process of the first principle processing scheme of coal tar FOO is：

(1) hydrocarbon HDS inferior comes from coal tar FOO；

The hydrocarbon for being mainly 60~360 DEG C by normal boiling point is separated into coal tar FOO separate section FRAC, coal tar FOO The hydrocarbon HD for being higher than 450 DEG C comprising normal boiling point that the light fraction FOL of composition and the mainly hydrocarbon by normal boiling point more than 360 DEG C form Heavy distillat FOMH, at least part heavy distillat FOMH is used as hydrocarbon HDS inferior；At least part light fraction FOL enters pre-add hydrogen Process RFOL is converted into hydrogenation reaction effluent RFOL-P, hydrogenation reaction effluent RFOL-P or its generation oil or it generates oil and evaporates Divide oil, into the first hydrogenation process R10 or the second hydrogenation process R20.

Based on the present invention, the 2nd kind of detailed process of the first principle processing scheme of coal tar FOO is：

(1) hydrocarbon HDS inferior comes from coal tar FOO；

The hydrocarbon for being mainly 60~360 DEG C by normal boiling point is separated into coal tar FOO separate section FRAC, coal tar FOO The hydrocarbon HD for being higher than 450 DEG C comprising normal boiling point that the light fraction FOL of composition and the mainly hydrocarbon by normal boiling point more than 360 DEG C form Heavy distillat FOMH, at least part heavy distillat FOMH is used as hydrocarbon HDS inferior；

At least part light fraction FOL is converted into hydrogenation reaction effluent RFOL-P into pre- hydrogenation process RFOL；

Hydrogenation reaction effluent RFOL-P enters thermal high separation process RFOL-P-THPS and is separated into hot gas separated by high pressure separator RFOL- P-THPS-V and hot high score oil RFOL-P-THPS-L；

Based on the logistics RFOL-P-THPS-LX of hot high score oil RFOL-P-THPS-L, into the first hydrogenation process R10 Or the second hydrogenation process R20；

(3) in removal process SR, what the second hydrogenation reaction effluent R20P of recycling obtained mainly being made of hydrogen in volume The hydrogen rich gas gas SRV and liquid stream SRL being mainly made of conventional liquid hydrocarbon, at least part hydrogen rich gas gas SRV are returned Hydrogenation process recycles；

The removal process of hot gas separated by high pressure separator RFOL-P-THPS-V is flowed out with the second hydrogenation reaction of at least part at least partially The removal process SR of object R20P is shared.

Based on the present invention, the 3rd kind of detailed process of the first principle processing scheme of coal tar FOO is：

(1) hydrocarbon HDS inferior comes from coal tar FOO；

(4) adding hydrogen upgrading reaction process R60, in hydrogen and under adding hydrogen upgrading catalyst R60C existence conditions, at least one Partially liq logistics SRL is carried out plus hydrogen upgrading reaction R60R is obtained plus hydrogen upgrading reaction product R60P, and hydrogen upgrading is added to react R60R Effect be imurity-removal or reduce hydrocarbon ils density or reduce hydrocarbon ils boiling point；

The hydro-upgrading reaction process of hot gas separated by high pressure separator RFOL-P-THPS-V and at least part plus hydrogen upgrading at least partially Reaction process R60 is shared.

Based on the present invention, the 1st kind of detailed process of second of principle processing scheme of coal tar FOO is：

(1) hydrocarbon HDS inferior comes from coal tar FOO；

The hydrocarbon for being mainly 60~450 DEG C by normal boiling point is separated into coal tar FOO separate section FRAC, coal tar FOO The light fraction FOLM of the composition and heavy distillat FOD that mainly hydrocarbon by normal boiling point more than 450 DEG C forms, at least part heavy distillat FOD is used as hydrocarbon HDS inferior；At least part light fraction FOLM is converted into hydrogenation reaction effluent into pre- hydrogenation process RFOLM RFOLM-P, hydrogenation reaction effluent RFOLM-P or its generation oil or its generation oil distillate oil, into the first hydrogenation process R10 or the second hydrogenation process R20.

Based on the present invention, the 2nd kind of detailed process of second of principle processing scheme of coal tar FOO is：

(1) hydrocarbon HDS inferior comes from coal tar FOO；

The hydrocarbon for being mainly 60~450 DEG C by normal boiling point is separated into coal tar FOO separate section FRAC, coal tar FOO The light fraction FOLM of the composition and heavy distillat FOD that mainly hydrocarbon by normal boiling point more than 450 DEG C forms, at least part heavy distillat FOD is used as hydrocarbon HDS inferior；

At least part light fraction FOLM is converted into hydrogenation reaction effluent RFOLM-P into pre- hydrogenation process RFOLM；

Hydrogenation reaction effluent RFOLM-P enters thermal high separation process RFOLM-P-THPS and is separated into hot gas separated by high pressure separator RFOLM-P-THPS-V and hot high score oil RFOLM-P-THPS-L；

Based on the logistics RFOLM-P-THPS-LX of hot high score oil RFOLM-P-THPS-L, into the first hydrogenation process R10 or the second hydrogenation process R20；

The removal process of hot gas separated by high pressure separator RFOLM-P-THPS-V and the second hydrogenation reaction stream of at least part at least partially The removal process SR for going out object R20P is shared.

Based on the present invention, the 3rd kind of detailed process of second of principle processing scheme of coal tar FOO is：

(1) hydrocarbon HDS inferior comes from coal tar FOO；

The hydro-upgrading reaction process of hot gas separated by high pressure separator RFOLM-P-THPS-V is carried at least part plus hydrogen at least partially Qualitative response process R60 is shared.

Based on the present invention, the 1st kind of detailed process of the third principle processing scheme of coal tar FOO is：

(1) hydrocarbon HDS inferior comes from coal tar FOO；

The hydrocarbon for being mainly 60~360 DEG C by normal boiling point is separated into coal tar FOO separate section FRAC, coal tar FOO Fraction FOM and master in the middle coalite tar that the light fraction FOL of composition, the hydrocarbon for being mainly 360~450 DEG C by normal boiling point form To be more than the heavy distillat FOD that 450 DEG C of hydrocarbon forms by normal boiling point, at least part heavy distillat FOD is used as hydrocarbon HDS inferior；Extremely Fraction FOM is converted into hydrogenation reaction effluent RFOM-P, hydrogenation reaction effluent into pre- hydrogenation process RFOM in a few part RFOM-P or its generation oil or its generation oil distillate oil, into the first hydrogenation process R10 or the second hydrogenation process R20。

Based on the present invention, the 2nd kind of detailed process of the third principle processing scheme of coal tar FOO is：

(1) hydrocarbon HDS inferior comes from coal tar FOO；

The hydrocarbon for being mainly 60~360 DEG C by normal boiling point is separated into coal tar FOO separate section FRAC, coal tar FOO Fraction FOM and master in the middle coalite tar that the light fraction FOL of composition, the hydrocarbon for being mainly 360~450 DEG C by normal boiling point form To be more than the heavy distillat FOD that 450 DEG C of hydrocarbon forms by normal boiling point, at least part heavy distillat FOD is used as hydrocarbon HDS inferior；

Fraction FOM is converted into hydrogenation reaction effluent RFOM-P into pre- hydrogenation process RFOM at least part；

Hydrogenation reaction effluent RFOM-P enters thermal high separation process RFOM-P-THPS and is separated into hot gas separated by high pressure separator RFOM- P-THPS-V and hot high score oil RFOM-P-THPS-L；

Based on the logistics RFOM-P-THPS-LX of hot high score oil RFOM-P-THPS-L, into the first hydrogenation process R10 Or the second hydrogenation process R20；

The removal process of hot gas separated by high pressure separator RFOM-P-THPS-V is flowed out with the second hydrogenation reaction of at least part at least partially The removal process SR of object R20P is shared.

Based on the present invention, the 3rd kind of detailed process of the third principle processing scheme of coal tar FOO is：

(1) hydrocarbon HDS inferior comes from coal tar FOO；

The hydro-upgrading reaction process of hot gas separated by high pressure separator RFOM-P-THPS-V and at least part plus hydrogen upgrading at least partially Reaction process R60 is shared.

The present invention, establishing the 1st kind of method of the first hydrogenation process R10 recycle oils is：

(3) in removal process SR, what the second hydrogenation reaction effluent R20P of recycling obtained mainly being made of hydrogen in volume Hydrogen rich gas gas SRV and the possibility being mainly made of conventional liquid hydrocarbon contain the liquid stream SRL of solid particle；

Separation liquid stream SRL obtains the thermal cracking heavy oil streams R20P- of the hydrocarbon component containing normal boiling point more than 350 DEG C HO, at least part thermal cracking heavy oil streams R20P-HO remove the first hydrogenation process as recycle oil R20P-HO-TOR10 R10。

The present invention, establishing the 2nd kind of method of the first hydrogenation process R10 recycle oils is：

The thermal cracking heavy oil object that the hydrocarbon component that it is mainly 350~530 DEG C by normal boiling point that separation liquid stream, which obtains, forms R20P-HO is flowed, at least part thermal cracking heavy oil streams R20P-HO goes first to add hydrogen anti-as recycle oil R20P-HO-TOR10 Answer process R10.

The present invention, establishing the 3rd kind of method of the first hydrogenation process R10 recycle oils is：

The thermal cracking heavy oil object that the hydrocarbon component that it is mainly 350~530 DEG C by normal boiling point that separation liquid stream, which obtains, forms Stream R20P-HO and the thermal cracking residue that mainly the hydrocarbon component by normal boiling point more than 530 DEG C forms, at least part thermal cracking weight Oily logistics R20P-HO removes the first hydrogenation process R10 as recycle oil R20P-HO-TOR10.

The present invention, establishing the 1st kind of method of the second hydrogenation process R20 recycle oils is：

Separation liquid stream obtains the thermal cracking heavy oil streams R20P-HO of the hydrocarbon component containing normal boiling point more than 350 DEG C, At least part thermal cracking heavy oil streams R20P-HO removes the second hydrogenation process R20 as recycle oil R20P-HO-TOR20.

The present invention, establishing the 2nd kind of method of the second hydrogenation process R20 recycle oils is：

Separation liquid stream obtains the thermal cracking heavy oil streams that the hydrocarbon component mainly by normal boiling point more than 350 DEG C forms R20P-HO, at least part thermal cracking heavy oil streams R20P-HO go the second hydrogenation reaction as recycle oil R20P-HO-TOR20 Process R20.

The present invention, establishing the 3rd kind of method of the second hydrogenation process R20 recycle oils is：

The thermal cracking heavy oil object that the hydrocarbon component that it is mainly 350~530 DEG C by normal boiling point that separation liquid stream, which obtains, forms Stream R20P-HO and the thermal cracking residue that mainly the hydrocarbon component by normal boiling point more than 530 DEG C forms, at least part thermal cracking weight Oily logistics R20P-HO removes the second hydrogenation process R20 as recycle oil R20P-HO-TOR20.

The present invention, in the first hydrogenation process R10, when using floating bed hydrogenation reactor, the hydrogenation catalyst that uses R10C usually enters the first hydrogenation process R10 with the first hydrogenation process R10 chargings.

The present invention, in the first hydrogenation process R10, using floating bed hydrogenation reactor, the hydrogenation catalyst that uses R10C usually enters the first hydrogenation process R10 with the first hydrogenation process R10 chargings；

In the second hydrogenation process R20, can no longer add new catalyst, at this time hydrogenation catalyst R20C be from The hydrogenation catalyst R10C of first hydrogenation process R10.

In the second hydrogenation process R20, using floating bed hydrogenation reactor, the hydrogenation catalyst R20C used can be with Addition includes to add different from the heat from hydrogenation cracking reaction catalyst R20C-2 of hydrogenation catalyst R10C, at this time hydrogenation catalyst R20C Hydrogen heat cracking reaction catalyst R20C-2 and hydrogenation catalyst R10C from the first hydrogenation process R10.

The present invention, in the first hydrogenation process R10, using floating bed hydrogenation reactor, the hydrogenation catalyst that uses R10C usually enters the first hydrogenation process R10, the first hydrogenation reaction mistake with the first hydrogenation process R10 chargings The heat from hydrogenation cracking reaction catalyst R20C-2 that the second hydrogenation process R20 is used can be not present in journey R10；

The present invention, in the first hydrogenation process R10, using floating bed hydrogenation reactor, the hydrogenation catalyst that uses R10C usually enters the first hydrogenation process R10 with the first hydrogenation process R10 chargings；First hydrogenation reaction mistake The heat from hydrogenation cracking reaction catalyst R20C-2 that second hydrogenation process R20 existing for journey R10 is used, can be with separation Hydrocarbon ils recycle stream obtained by second hydrogenation reaction effluent R20P is into the first hydrogenation process R10's；

The present invention, in the first hydrogenation process R10, the hydrogen gas stream used is preferably new hydrogen logistics.

The present invention, in the first hydrogenation process R10, the logistics R10P-XO- containing hydrocarbon ils in R10P based on R10P TOR20 can enter the second hydrogenation process R20 after heating furnace heats up.

Specific implementation mode

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

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

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

High aromatic hydrocarbons of the present invention refers to for example middle low temperature of the high oil product of the density of aromatic hydrocarbon containing tricyclic and/or polycyclic aromatic hydrocarbon Coal tar.

Tricyclic structure aromatic hydrocarbons of the present invention refers to the ring structure containing there are three and wherein at least one ring belongs to aromatic ring Hydro carbons, as fluorenes, dibenzofuran, thia fluorenes, carbazole, dibenzopyridine, anthracene, phenanthrene and its with side chain component or part thereof add hydrogen saturation production Object.

Multiring structure aromatic hydrocarbons of the present invention refers to belonging to containing four or more ring structure and wherein at least one ring The hydro carbons of aromatic ring.

Polycyclic aromatic hydrocarbon of the present invention refers to the hydro carbons containing four or more adjacent aromatic rings building stone, in thermal cracking The logical tendency for often occurring thermal condensation of reaction process.

Impurity element of the present invention refers to non-hydrogen in feedstock oil, non-carbon, nonmetalloid such as oxygen, sulphur, nitrogen, chlorine Deng.

Impurity hydrogenation products of the present invention refer to non-hydrogen in feedstock oil, non-carbon element hydrogenation products, including water, Hydrogen sulfide, ammonia, hydrogen chloride etc..

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

The composition or concentration or content value of component of the present invention are unless stated otherwise weight datum value, weight Percentage is expressed as weight %.

The chemical hydrogen consumption amount of hydrocarbon stream of the present invention or the hydrocarbon component is unless stated otherwise weight chemical hydrogen consumption Amount and hydrocarbon stream or the ratio of the weight of the hydrocarbon component, i.e. weight datum value chemical hydrogen consumption amount.

It can also be benzene hydrocarbons that the hexa-atomic cyclic hydrocarbon of list of the present invention, which can be hexamethylene methane series hydrocarbon, usually C₆~C₁₀Hydrocarbon.

Naphtha Cut of the present invention refers to that normal boiling point is generally 60~180 DEG C, usually 60~165 DEG C of hydrocarbon Class.

Fraction of diesel oil of the present invention refers to that normal boiling point is generally 160~370 DEG C, usually 180~360 DEG C of hydrocarbon Class.

Light diesel fuel fraction of the present invention refers to that normal boiling point is generally 155~280 DEG C, is usually 165~270 DEG C Hydro carbons.

Heavy diesel fuel fraction of the present invention refers to that normal boiling point is generally 250~370 DEG C, is usually 260~360 DEG C Hydro carbons.

Coal tar and its hydro-upgrading process described in detail below.

Coal tar of the present invention refers to the processes such as the pyrolysis step from pyrolysis of coal or the dry distillation of coal or coal generating gas process Coal tar or its fraction, can be the by-product coalite tar or its fraction of coal generating gas, can also be coal coking pyrolysis of coal Process (including semicoke, medium temperature coking, high-temperature coking process) by-product coal tar or its fraction, can be above-mentioned coal tar Miscella, can be above-mentioned coal tar extract obtained extract oil such as depitching coal tar through light hydrocarbon solvent or it is evaporated Divide oil.

High-temperature coking belongs to coal high temperature pyrolysis process, and the final temperature of pyrolytic process is generally higher than 900 DEG C, usually 1000 Between~1400 DEG C.The high temperature coal-tar refers to that coal high temperature pyrolysis produces the pair of coke and/or the production of town gas process Product crude tar oil.High temperature coal-tar usually produces following product in primary distillation process：Light oil (topping tar), carbolic oil, naphthalene The products such as oil, lightweight washing oil, heavy wash oil, lightweight carbolineum, heavy carbolineum, pitch, carbolic oil can be further separated into crude phenols and take off Carbolic oil, naphtalene oil can be further separated into thick naphthalene and de- naphtalene oil.High temperature coal-tar light fraction of the present invention refers to：Carbolineum is washed Oil, naphtalene oil, de- naphtalene oil, carbolic oil, dephenolize oil, light oil and its miscella.

Since raw coal property and coking or gas-making process condition change in a certain range, the property of coal tar is also one Determine variation in range.The process conditions and product requirement of coal tar primary distillation process also change in a certain range, therefore coal tar The property of oily light fraction also changes in a certain range.The property of coal tar light fraction, proportion are usually 0.92~1.25, conventional It is usually 120~460 DEG C that boiling point, which is generally 60~500 DEG C, usual tenor is 5~80PPm, sulfur content be 0.4~ 0.8%, nitrogen content is 0.6~1.4%, oxygen content is 0.4~9.0%, and usual water content is 0.2~5.0%, and carbon residue content is logical It is often 0.5~13%.

Middle coalite tar of the present invention refers to producing from pyrolysis of coal or coal generating gas or the coal tar of other processes Product can be the medium temperature of coalite tar or medium temperature process of coking from semicoke process (pyrolysis temperature is less than 700 DEG C) Coal tar (pyrolysis temperature is between 700~950 DEG C) or their miscella, usually contain coal tar heavy duty oil ingredient.Due to raw coal Property and coking or gas-making process condition change in a certain range, and the property of middle coalite tar also becomes in a certain range Change.The property proportion of middle coalite tar of the present invention is usually 0.89~1.15, usual tenor be 5~200PPm, Sulfur content is 0.1~0.7%, nitrogen content is 0.6~1.6%.Middle coalite tar of the present invention, sometimes inorganic water content be 0.2~5.0%, organic oxygen content is usually 2.5~18%, in particular 3.5~10%, more particularly 5~10% sometimes.

Table 1 is different boiling ranges fraction aromatic ring number distribution statistics table in typical medium temperature coal tar.

It is that 120~450 DEG C of the hydrocarbon components and normal boiling point are high that medium temperature coal tar of the present invention, which typically includes conventional boiling range, In the mixture of 450 DEG C of the hydrocarbon components, the light fraction FD1 that the conventional boiling range for generally comprising 10~20% is 120~260 DEG C is (containing double Cyclophane hydrocarbon-fraction), generally comprise 30~40% conventional boiling range be 260~370 DEG C middle fraction FD2 (contain bicyclic, thrcylic aromatic hydrocarbon Fraction), the heavy distillat FD3 (containing bicyclic to Fourth Ring aromatic fraction) and 8 that is 370~450 DEG C comprising 20~35% conventional boiling range ~20% conventional boiling range is higher than 450 DEG C of residue oil fraction FD4 (i.e. coal tar pitch fraction).

Middle coalite tar light fraction oil of the present invention, refers to that normal boiling point is generally 60~480 DEG C, is usually 60~450 DEG C of coal tar distillate oil, usually may be used fixed bed hydrogenation technology and carries out hydro-upgrading.

Middle coalite tar heavy fraction of oil of the present invention refers to that normal boiling point is usually above 370 DEG C, is generally greater than 400 DEG C of middle coalite tar fraction, their heat from hydrogenation cracking process refer to that at least part hydrocracking reaction occurs The process that molecular weight is less than cracked stock molecular weight is produced, which generally comprises parallel hydrodemetallization, hydrofinishing, adds Hydrogen heat cracking reaction, suitable reactor types are up flow type expanded bed such as suspended-bed reactors or fluidized bed reactor.

Different boiling ranges fraction aromatic ring number distribution statistics table in the typical medium temperature coal tar of table 1

Residue oil fraction FD4 is generally difficult to realize long period using conventional bed technology, adds hydrogen lighting in high yield therefore adopt With up flow type expanded bed such as suspension bed or boiling bed hydrogenation technical transform it, in order to prevent gum asphalt reunite cause it is unnecessary Coking reaction, it is often necessary to form glue using thering is the solvent hydro carbons of good ability of dissolving each other to dissolve dispersion to it with cinder oil distillate The weak solution of matter asphalitine, solvent hydro carbons can be the heavy distillat FD3 that conventional boiling range is 370~450 DEG C, can also be heavy distillat The conversion product for adding hydrogen aromatic moiety saturation of FD3 and residue oil fraction FD4 can also be that middle fraction FD2's plus hydrogen aromatic moiety are full The conversion product of sum.The conversion product for adding hydrogen aromatic moiety saturation of middle fraction FD2 belongs to excellent hydrogen supply dissolvent, is rich in hydrogen supply hydrocarbon.

High aromatic carbon rate poor quality hydrocarbon HDS of the present invention, can be a kind of high aromatic hydrocarbons of long distillate, can also be 2 kinds or it is a variety of not With the high aromatic hydrocarbons of boiling range；The hydrogenation process that first hydrogenation process R10 of the present invention is carried out, can process a kind it is bad Matter hydrocarbon HDS can also process the hydrocarbon HDS inferior of 2 kinds or a variety of different boiling ranges；First hydrogenation process R10 of the present invention Can be 2 tunnels or multiple feed, the catalyst that the raw material that do not go the same way flows through when the high aromatic hydrocarbons of 2 kinds of processing or a variety of different boiling ranges Bed or reaction compartment can be identical or different, can be in parallel plus hydrogen relationships, can also be to respectively enter multi-reaction-area one after another Serial hydrogenation process relationship, naturally it is also possible to be Unionfining again after first in parallel front-end hydrogenation and then front-end hydrogenation product converge Relationship, can also be other more complicated syntagmatics.

According to the present invention, before the coal tar carries out hydrotreating or before being fractionated, generally went through and filtered out admittedly The process of body particle.

Middle coalite tar of the present invention, usually contains phenolic compound, before entering hydrogenation process, can extract The such as rudimentary phenol of phenolic compound therein.

The technological process range of hydrocarbon raw material HDS hydro-upgrading processes UHP, normally start from hydrocarbon raw material HDS adds hydrogen aromatic hydrocarbons Either shallow saturated reaction process, heat from hydrogenation cracking reaction process end to obtain hydro-upgrading naphtha and/or light diesel product Flow range, typical hydro-upgrading process UHP include the first hydrogenation process R10, the second hydrogenation process R20, The separation process of second hydrogenation reaction effluent R20P plus hydrogen upgrading reaction process R60 plus hydrogen upgrading generate the fractionation of oil Journey, the cycle cracking process of heat from hydrogenation cracking tail oil plus the cycle cracking process of hydrogen upgrading tail oil.

Cycle cracking tail oil of the present invention is commonly referred to as generating oil for the heat from hydrogenation cracking of specific feedstock oil, add Hydrogen upgrading generates the high boiling hydrocarbon for being not suitable as naphtha or light diesel component in oil, usually mainly by normal boiling point height It is formed in 300 DEG C or 330 DEG C or 360 DEG C of the hydrocarbon components.

The olefin(e) centent height of fraction of the coalite tar light fraction such as normal boiling point less than 350 DEG C, phenol content in usually High, gum level height simultaneously contains the more component easily reacted under the conditions of mitigation, therefore, the pre-add of the coal tar light fraction Hydrogen process, usually using hydrogenation protecting agent, olefins hydrogenation agent, hydrogenation deoxidation agent, removal of ccr by hydrotreating agent, hydrogen desulfurization agent etc. Single dose or the tandem compound or mixed loading combination of double agent or multi-agent, usually using down-flow fixed bed hydrogenation reactor.

The deep hydrogenation upgrading processes of coal tar light fraction, or logistics obtained by the second hydrogenation reaction effluent of separation R20P SRLX, progress add hydrogen upgrading reaction R60R to obtain adding hydrogen upgrading reaction product R60P, are taken off usually using hydrogen desulfurization agent plus hydrogen Nitrogen agent, aromatic hydrogenation saturator and cycloalkane add hydrogen ring opening catalyst, hydroisomerisation catalysts, hydrocracking catalyst etc. Single dose or the tandem compound or mixed loading combination of double agent or multi-agent, usually using down-flow fixed bed hydrogenation reactor.

The characteristic of the present invention described in detail below.

R10P enters the second hydrogenation process R20 as logistics R10P-XO-TOR20.

6. oil product obtained by shale oil or its distillate or its hot procedure；

1. suspension bed；

2. ebullated bed；

3. moving bed.

2. catalyst granules；

3. iron rust particle；

4. particles of inorganic material；

5. coking of coal process generate into the solid particle in coal tar；

7. the solid particle from shale；

8. the solid particle from oil-sand；

KSH=0.2~5；

1. aromatic hydrocarbons deep hydrogenation saturated reaction；

2. hydro carbons deep hydrogenation denitrification reaction；

3. cycloalkane adds hydrogen ring-opening reaction；

4. hydrocarbon hydrocracking reacts；

5. hydrocarbons hydrogenation isomerization reaction.

1. suspension bed；

2. ebullated bed；

3. moving bed.

2. catalyst granules；

3. iron rust particle；

4. particles of inorganic material；

5. coking of coal process generate into the solid particle in coal tar；

7. the solid particle from shale；

8. the solid particle from oil-sand；

K=0.2~5；

(1) hydrocarbon HDS inferior comes from coal tar FOO；

As needed, pre- hydrogenation process R1 and/or deep hydrogenation upgrading processes R2 can be added in any supplement sulphur, with Ensure reaction process necessary minimum concentration of hydrogen sulfide such as 500PPm (v) or 1000PPm (v), to ensure that catalyst is necessary Hydrogen sulfide sectional pressure is not less than minimum must value.The supplement sulphur can be sulfide hydrogen or pair that can be converted into hydrogen sulfide Material of the hydroconversion process without ill-effect, such as hydrogen sulfide containing gas or oil product, or generated after being contacted with high-temperature hydrogen The carbon disulfide or dimethyl disulfide of hydrogen sulfide or sulphur etc..When the flux oil of pre- hydrogenation process R1 is anti-with hydrogen sulfide containing plus hydrogen When effluent form being answered to provide, if hydrogen sulfide quantity therein meets the needs of pre- hydrogenation process R1, benefit can not used Sulphur agent.

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

The high pressure separation process of hydrogenation reaction effluent generally comprises cold high pressure separator, when hydrocarbon in hydrogenation reaction effluent Oil density big (such as close with water density) or viscosity are big or when being difficult to detach with water emulsification, it is also necessary to it is usual that operation temperature be arranged For 150~450 DEG C of high pressure hot separator, hydrogenation reaction effluent enters high pressure hot separator and is separated into one in volume at this time On the hot gas separated by high pressure separator gas that is mainly made of hydrogen and one be mainly made of conventional liq hydrocarbon and solid that may be present Hot high score fluid body, hot gas separated by high pressure separator enter the cold high pressure separator that operation temperature is usually 20~80 DEG C be separated into cold high score oil and Cold gas separated by high pressure separator realizes following target since a large amount of high boiling components enter in hot high score fluid body：Cold high score oil density becomes smaller Or viscosity becomes smaller or is easily isolated with water.High pressure hot separator is arranged in the high pressure separation process of hydrogenation reaction effluent, is also equipped with The advantages of reducing thermal loss because hot high score fluid body can be undergone to avoid hot gas separated by high pressure separator using air cooler or water cooler Cool process.Meanwhile the hydrogenation process that the hot high score fluid body in part can be returned to upstream recycles, to improve The overall raw material property of the hydrogenation process of the recycle oil is received, or cycle plus hydrogen are carried out to the recycle oil.Hydrogenation reaction stream Go out object or hot gas separated by high pressure separator enters before cold anticyclone separate section, usually first reduces temperature (being usually to feed to exchange heat with reactive moieties) To about 220~100 DEG C (temperature should be higher than that in the hydrogenation reaction effluent gas phase sulphur hydrogenation ammonia crystallization temperature), then usually to Wherein injection washings form water filling back end hydrogenation reaction effluent, and washings are used for absorbing ammonia and issuable other impurity such as Hydrogen chloride etc., and the aqueous solution after absorbing ammonia necessarily absorbs hydrogen sulfide.In cold anticyclone separate section, the water filling back end hydrogenation reaction Effluent is separated into：One cold gas separated by high pressure separator being mainly made of hydrogen in volume, one mainly by conventional liq hydrocarbon and dissolving The cold high score oil of hydrogen composition, a cold high score water be mainly made of water and dissolved with ammonia, hydrogen sulfide.The cold high score water, The content of wherein ammonia is generally 0.5~15% (w), preferably 1~8% (w).One purpose of note washings is to absorb to add hydrogen anti- The ammonia and hydrogen sulfide in effluent are answered, prevents from forming sulphur hydrogenation ammonia or more sulphur ammonia Crystallization Plugging heat exchanger channels, increases system pressure Power drops.The injection rate of the washings should be determined according to following principles：On the one hand, after washings injection hydrogenation reaction effluent It is divided into vapour phase water and liquid phase water, liquid phase water has to be larger than zero, preferably washs 30% or more of water inventory；In another aspect, Washings are used to absorb the ammonia in hydrogenation reaction effluent, prevent the ammonia density of gas separated by high pressure separator too high, reduce catalyst activity, usually The lower the ammonia volumetric concentration of gas separated by high pressure separator the better, generally no greater than 200PPm (v), desirably no more than 50PPm (v).The cold height Pressure separator operation pressure is that hydrogenation reaction partial pressure subtracts actual pressure drop, cold anticyclone separate section operating pressure and plus hydrogen The difference of reaction pressure, it is unsuitable too low or excessively high, it is usually generally 0.35~3.2MPa, 0.5~1.5MPa.The cold height The hydrogen volume concentration value of point gas, it is unsuitable too low (device operating pressure is caused to rise), should generally be not less than 70% (v), it is suitable not Less than 80% (v), preferably not below 85% (v).As previously described at least part, be usually 85~100% cold gas separated by high pressure separator return It returns and is recycled in hydrogenation reaction part, to provide the necessary amounts of hydrogen in hydrogenation reaction part and hydrogen concentration；In order to improve device Efficiency of investment, it is necessary to assure cycle hydrogen concentration is not less than lower limit value above-mentioned, for this purpose, according to specific feedstock property, reaction item Part, product distribution can exclude a part of cold gas separated by high pressure separator to exclude methane, the ethane that reaction generates.For the cold of discharge Gas separated by high pressure separator, may be used conventional membrane separation process or pressure swing adsorption technique or oil wash technique realizes hydrogen and non-hydrogen gas component Separation, and the hydrogen of recycling is used as new hydrogen.

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

Be not provided with plus the hydrocarbon inferior of i.e. the first hydrogenation process R10 of hydrogen aromatic hydrocarbons either shallow saturated reaction process R10 adds hydrogen Method for thermal cracking is compared, the advantage of the invention is that：

1. setting plus hydrogen aromatic hydrocarbons either shallow saturated reaction process R10, the super delocalization energy based on aromatic ring pi bond among polycyclic aromatic hydrocarbon is big In the rule of the super delocalization energy of outside aromatic ring pi bond, carried out under conditions of based on the liquid phase reactor polycyclic aromatic hydrocarbon plus hydrogen aromatic hydrocarbons it is shallow Degree saturated reaction makes in-between aromatic ring be saturated, and HDS produced positioned at multiring structure aromatic hydrocarbons while de- carbon residue reaction The low methylene bridged bond of the dissociation energy in centre position, provides for heat from hydrogenation cracking reaction process R20 rich in the cracking for preferably cracking key Material can be improved object thermal cracking lighting reaction speed, shorten the thermal cracking time, inhibits the side reaction in thermal response, be conducive to Improve the yield of hexatomic ring hydrocarbon system object；

Add hydrogen aromatic hydrocarbons either shallow saturated reaction process R10 2. being arranged, adds hydrogen saturation Function fitness is strong to add conducive to giving full play to For example micron-sized crystallite molybdenite (MoS of hydrogen catalyst₂) or other efficient compound catalyst hydrogenating function；Add hydrogen aromatic hydrocarbons shallow The type of catalyst R10C and liquid concentration existing for degree saturated reaction process can be different from heat from hydrogenation cracking reaction process and deposit Catalyst R20C type and liquid concentration；

3. setting plus hydrogen aromatic hydrocarbons either shallow saturated reaction process R10 are conducive to reduce " the temperature value TS- coal tar of starting reaction The preheating terminal temperature of heavy distillat HDS=Δ T1 " temperature differences is conducive to improve process safety；

4. setting plus hydrogen aromatic hydrocarbons either shallow saturated reaction process R10, can be improved feedstock oil and recycle oil studies on asphaltene lighting Conversion ratio reduces feedstock oil and recycle oil studies on asphaltene thermal condensation conversion ratio；R10 reactors, R20 reactors can be significantly reduced Inner wall wall surface coking amount, can significantly reduce the coking amount of the wall surface of the high pressure hot separator of R20P, can significantly reduce R10 reactions The concentration and aromatic hydrocarbon fused rings degree of gluey asphaltic substances in device, R20 inside reactor liquid phases, can dramatically increase R10 reactors, The uniformity of R20 inside reactor liquid phases composition, can significantly reduce R10 reactors, R20 inside reactor liquid phase viscosities, can show It writes and improves R10 reactors, the molten hydrogen rate of R20 inside reactor liquid phases, transmission hydrogen rate and hydrogen supply speed；

5. setting plus hydrogen aromatic hydrocarbons either shallow saturated reaction process R10, can form clearly " order of reaction or conversion zone " concept " add hydrogen saturated reaction section, heat from hydrogenation cracking zone ", according to the difference of the leading reaction target of reaction process or according to reacting The fluctuation section of journey reaction temperature, and then establish segmentation reaction liquid phase product circulation concept；

6. setting plus hydrogen aromatic hydrocarbons either shallow saturated reaction process R10 are based on clearly " order of reaction or conversion zone " concept, according to The difference of the leading reaction target of reaction process or fluctuation section according to reaction process reaction temperature, setting reaction interstage temperature Control measures are not provided with heater such as to be clearly distinguishable from existing more between suspended-bed reactor and/or fluidized bed reactor The Process flow of heating furnace, the present invention under most conditions, are adding hydrogen aromatic hydrocarbons either shallow saturated reaction process R10 and are being to be hydrocracked It needs that heater such as heating furnace is arranged between thermal process reactor R20, to realize being adjusted flexibly and/or filling for temperature difference between order of reaction When the heating furnace that goes into operation；

7. setting plus hydrogen aromatic hydrocarbons either shallow saturated reaction process, based on clearly " order of reaction or conversion zone " concept, according to anti- The difference of the leading reaction target of process or the difference according to reaction process hydrogen consumption speed are answered, is ensureing to react hydrogen partial pressure Under the conditions of, Discrete control or light oil volume ratio or reaction compartment liquid phase fraction are reconciled, adds hydrogen aromatic hydrocarbons either shallow saturated reaction process R10 Lower hydrogen to oil volume ratio or higher liquid air volume ratio may be used, improve space reactor efficiency, increase adding for feedstock oil The hydrogen aromatic hydrocarbons either shallow saturated reaction liquid phase reactor time；Simultaneously for heat from hydrogenation cracking reaction process leave more hydrogen (quantity and Initial temperature) it is used to adjust the reaction temperature of R20；

8. plus hydrogen aromatic hydrocarbons either shallow saturated reaction process R10, HDS can effectively reduce reaction process R10 with branch feeding manner Total hydrogenation reaction severity；

9. using a large amount of hydrogen supply hydrocarbon, make full use of the hydrocarbon component BSAA's that the normal boiling point in coal tar is 330~450 DEG C Hydro-upgrading generates oil, effectively improves the KSH ratios of R10, can be effectively increased the dispersion degree of the hydrocarbon component HD, obtain reactive hydrogen speed Degree reduces the hydrocarbon component HD condensation coking speed, is conducive to improve asphalitine lighting conversion ratio；

10. the first hydrogenation process R10 can process coal tar heavy oil or coal tar more inferior；It is bad to produce The coal carbonization technology of matter, for example high tar yield of coal conversion process of heavy coal tar, opens effective coal tar processing road, It can be combined into coal processing fundamental technology with production poor quality, the coal conversion process such as coal carbonization technology of heavy coal tar；

(11) new device or existing plant modification be can be applied to.

Reference examples one

Use a kind of hydrogenation method for coal tar suspension bed of heterogeneous catalysis of Chinese patent ZL201010217358.1 for The property of reference examples one of the present invention, the coal tar raw material of selection is shown in Table 2, and the true boiling-point (TBP) cutting result of coal tar raw material is shown in Table 3.

The coal tar is separated into IBP~355 after conventional method dehydration, except mechanical admixture pretreatment through distillation process DEG C fraction FOL, 355~435 DEG C of fraction FOM and be more than 435 DEG C of heavy distillat FOD, more than 355 DEG C " comprising fraction FOM and The mixed fraction FOMD of fraction FOD ", the feedstock oil as floating bed hydrogenation reactor carry out being hydrocracked lighting reaction.

Used catalyst is a kind of compound suspension bed hydrogenation catalyst of molybdenum-iron, and used catalyst includes high activity metal group Divide molybdenum and low activity metal component iron, the weight ratio of wherein high-activity component metal molybdenum and low activity component metals iron is 1: 500, Catalyst water content is less than 0.5wt%, and particle diameter is 1~100 μm of powdered granule.It is 58wt% that the catalyst, which is by iron content, Bloodstone (main ingredient Fe2O3) is ground into the powdered granule less than 100 μm, then that 10% ammonium molybdate aqueous solution is uniform Ground sprays on particle, and spray flux is about molybdenum: iron weight ratio is equal to 1: 500, through being dried 1 hour at 100 DEG C, obtains water content Powdered granule catalyst less than 0.5wt%.

Table 4 is one heat from hydrogenation cracking reaction process condition of reference examples.

The suspension bed hydrogenation process process of this example is：The recycle oil for being stripped of catalyst and/or coal tar are more than first Powdered granule molybdenum-iron compound floating bed hydrogenation of the sub-fraction of 355 DEG C of heavy distillates with catalyst grain size less than 100 μm is urged Agent (and metal molybdenum: iron weight ratio is 1: 500) and vulcanizing agent dimethyl disulfide together under 80 DEG C of stirring condition fully It is uniformly mixed obtained oil-catalyst slurry, controls the solid concentration of oil-catalyst slurry in 25wt% or so.Then oil-catalyst slurry with Remaining most of coal tar is more than 355 DEG C of heavy distillate raw materials and floating bed hydrogenation reaction product containing after atmospheric tower is fractionated There is the recycle oil (i.e. about 4/5ths normal bottom heavy oil) of catalyst to mix, enters after the boosting of raw material pump, mixed hydrogen heating and suspend Bed hydroprocessing reactor carries out hydrocracking reaction, and process conditions are as shown in table 4, and the addition of catalyst is to control active component Metal is 0.9: 100 with coal tar raw material weight ratio, and suspended-bed reactor reaction effluent is by high-temperature separator, low temperature point Divide oil mixture stream and hydrogen-rich gas two parts from liquid-solid phase height is obtained after device.Hydrogen-rich gas is used as recycle hydrogen.Liquid-solid phase is high After low point of oil mixture flows through atmospheric tower fractionation, tower top obtains being less than 355 DEG C of light distillates, and bottom of tower is obtained containing the normal of catalyst Bottom heavy oil, often bottom heavy oil is recycled directly to as recycle oil in floating bed hydrogenation reactor wherein most (about 4/5ths) It further carries out plus hydrogen lighting is reacted；The normal bottom heavy oil of remaining fraction (about 1/5th) is carried out using the method for filtering It is separated by solid-liquid separation, catalyst residue and floating bed hydrogenation heavy distillate is obtained after separation, this part heavy distillate or directly and outstanding The reaction raw materials of floating bed are mixed or as partial solvent prepared by oil-catalyst slurry, are recycled into floating bed hydrogenation reactor It further carries out plus hydrogen lighting reaction, the catalyst of abjection gets rid of or regenerate outside.

Table 5 is portion of product yield distribution obtained by one heat from hydrogenation cracking reaction process of reference examples.

The method for handling coal tar using this example suspension bed hydrogenation process can make light oil (the conventional boiling that coal tar is extracted The heat from hydrogenation cracking of light fraction of the point less than 355 DEG C and normal boiling point less than 355 DEG C generates oil) yield reaches 91.1wt%.Examination The light oil tested can be used existing processing technology and carry out upgrading processing fuel oil and industrial chemicals.

The property of 2 reference examples of table, one coal tar raw material

The true boiling-point (TBP) cutting result of 3 reference examples of table, one coal tar raw material

Component	Weight yield, % is to aqueous tar
		Water	3.07
Fraction FOL, 170 DEG C~355 DEG C fractions	41.30
		Fraction FOM, 355 DEG C~435 DEG C fractions	23.72
435 DEG C of fractions of fraction FOD, ＞	31.91
		It amounts to	100

4 reference examples of table, one heat from hydrogenation cracking reaction process condition

Project	Data
		Reaction temperature, DEG C	450
React hydrogen partial pressure, MPa	17~18
		Air speed, h^-1	1.0
Hydrogen-oil ratio, v/v	900
		Catalyst (including regenerated catalyst) addition (iron+molybdenum)/feedstock oil weight ratio	0.9/100
Normal bottom heavy oil direct circulation amount/go the de- solid amount of vacuum tower	4/1
		Vulcanizing agent dimethyl sulfide/feedstock oil	2/100

Portion of product yield distribution obtained by 5 reference examples of table, one heat from hydrogenation cracking reaction process

Based on above-mentioned data, build coal tar processing amount be 50 tons/when coal tar hydrogenating reforming unit, setting 2 etc. The air speed of volume suspended-bed reactor R201E, R202E, every reactor are 2.0h^-1, total air speed is 1.0h^-1。

The average operating temperature of reactor R201E is 445 DEG C, the average operating temperature of R202E is 455 DEG C

Embodiment one

Based on reference examples one, increases poor quality hydrocarbon HDS and add i.e. the first hydrogenation process of hydrogen aromatic hydrocarbons either shallow saturated reaction process R10。

According to the present invention, used mixed fraction FOMD as poor quality hydrocarbon HDS, it is anti-that hydrocarbon HDS inferior enters heat from hydrogenation cracking Before answering process i.e. the second hydrogenation process R20, is completed first by the first hydrogenation process R10 plus hydrogen aromatic hydrocarbons either shallow is full And reaction, reinforcing hydrogenation reaction function based on liquid phase reactor under conditions of carries out polycyclic aromatic hydrocarbon plus hydrogen aromatic hydrocarbons either shallow saturation R10R is reacted, the intermediate aromatic ring of part polycyclic aromatic hydrocarbon is made to be saturated, HDS produced positioned at polycyclic while de- carbon residue reaction The low methylene bridged bond of the dissociation energy in the centre position of structure aromatic hydrocarbons；Table 6 is the first hydrogenation process R10's of embodiment one Operating condition and operating result, wherein the increase of metal molybdenum is by using the second catalyst crystallite molybdenite (MoS₂) miberal powder What form was realized, crystallite molybdenite (MoS₂) miberal powder is 15~75 μm of powdered granule.

Based on reference examples one, embodiment one increases the first hydrogenation process R10, and the first hydrogenation process R10 makes With the pre- hydrocracking reactor R101E of 1 suspension bed, it is 2.0h that the air speed of reactor R101E, which is to hydrocarbon HDS1 inferior,^-1, such 3 Total air speed of floating bed hydrogenation reactor R101E, R201E, R203E of platform serial operation is：Total poor quality hydrocarbon HDS is 0.667h^-1。

The the first hydrogenation process R10 operating conditions and operating result of 6 embodiment one of table

Project	Data
		Reactor R10E	1, suspension bed
Average reaction temperature, DEG C	410~420
		React hydrogen partial pressure, MPa	17.3~18.3
Air speed, h^-1	2.0
		Hydrogen-oil ratio, v/v	300
First catalyst (including regenerated catalyst) addition (iron+molybdenum)/feedstock oil weight ratio	0.9/100
		Metal molybdenum in first catalyst: iron weight ratio is	1∶500
First catalyst particle size range, micron	1~100
		Second catalyst (including regenerated catalyst) addition, catalyst/feed weight of oil ratio	0.2/100
Second catalyst particle size range, micron	15~75
		Normal bottom heavy oil direct circulation amount/go the de- solid amount of vacuum tower	4/1
Vulcanizing agent dimethyl sulfide/feedstock oil	2/100
		Hydrocarbon HDS weight chemistry hydrogen consumption inferior, weight %	0.55~0.65
Gum asphalt hydrogenation and removing rate, weight %	8~10
		Carbon residue hydrogenation and removing rate, weight %	9~12

As can be seen that the hydrogen-oil ratio of the first hydrogenation process R10 is the 1/3 of the second hydrogenation process R20, it is evident that Divide rate conducive to the liquid phase volume for improving R10 reaction compartments, is conducive to extend the liquid phase reactor operating time；

As can be seen that the reaction temperature of the first hydrogenation process R10 reduce 30 compared with the second hydrogenation process R20~ 40 DEG C, it is evident that be conducive to reduce the thermal condensation reaction of polycyclic aromatic hydrocarbon；

As can be seen that comparing reference examples one, second is increased in the catalyst of the first hydrogenation process of the present embodiment R10 Catalyst crystallite molybdenite (MoS₂) miberal powder, and its size distribution is also beneficial to improve it and be retained in the balance of space reactor Amount or inflow-rate of water turbine hold solid amount, to enhance the catalyst hydrogenation ability of the first hydrogenation process R10；

Table 7 is the process conditions of the heat from hydrogenation cracking reaction process R20 of embodiment one, it can be seen that：

1. average reaction temperature reduces 3~5 DEG C, it is conducive to reduce thermal condensation reaction and gas making reaction；

2. because the catalyst that the first hydrogenation process R10 is used, has used the second hydrogenation catalyst.

Table 8 is portion of product yield distribution obtained by the heat from hydrogenation cracking reaction process R20 of embodiment one；

It can be seen that：

1. the general reaction of the first hydrogenation process R10, heat from hydrogenation cracking reaction process R20 are as a result, lightweight oily yield Increase 0.25~0.35wt%；

2. heat from hydrogenation cracking reaction generates and gets rid of residual oil outside oily fractional distillation process, reduce 0.35~0.40wt%.

The process conditions of the heat from hydrogenation cracking reaction process R20 of 7 embodiment one of table

Project	Data
		Average reaction temperature, DEG C	445~447
React hydrogen partial pressure, MPa	17~18
		Air speed, h^-1	1.0
Hydrogen-oil ratio, v/v	900
		First catalyst (including regenerated catalyst) addition (iron+molybdenum)/feedstock oil weight ratio	0.9/100
Metal molybdenum in first catalyst: iron weight ratio is	1∶500
		First catalyst particle size range, micron	1~100
Second catalyst (including regenerated catalyst) addition, catalyst/feed weight of oil ratio	0.2/100
		Second catalyst particle size range, micron	15~75
Normal bottom heavy oil direct circulation amount/go the de- solid amount of vacuum tower	4/1
		Vulcanizing agent dimethyl sulfide/feedstock oil	2/100

Portion of product yield distribution obtained by the heat from hydrogenation cracking reaction process R20 of 8 embodiment one of table

Embodiment two

Hydrogen lighting is added using a kind of low hydrogen content heavy oil using hydrogen supply hydrocarbon of Chinese patent ZL201210022921.9 Method is improved embodiment one.

The hydrocarbon for being mainly 60~355 DEG C by normal boiling point is separated into coal tar FOO separate section FRAC, coal tar FOO Fraction FOM and master in the middle coalite tar that the light fraction FOL of composition, the hydrocarbon for being mainly 355~435 DEG C by normal boiling point form To be more than the heavy distillat FOD that 435 DEG C of hydrocarbon forms by normal boiling point, heavy distillat FOD is used as hydrocarbon HDS inferior；Light fraction FOL is in Fraction FOM is converted into hydrogenation reaction effluent RFOLM-P into pre- hydrogenation process RFOLM, hydrogenation reaction effluent RFOLM-P into Enter thermal high separation process RFOLM-P-THPS and is separated into hot gas separated by high pressure separator RFOLM-P-THPS-V and RFOLM-P-THPS-L heat height It is 0.74 times of heavy distillat FOD weight flows to divide oil, hot high score oil RFOLM-P-THPS-L weight flows

The operating condition of pre- hydrogenation process RFOLM is：Temperature is 270~410 DEG C, pressure 18.0MPa, hydrogen/raw material Oil volume ratio is 800: 1~2000: 1, Hydrobon catalyst HPU3-CAT volume space velocities are 0.55~0.70hr^-1；Chemistry is pure Hydrogen consumption is 2.65~3.15%, makes bicyclic, thrcylic aromatic hydrocarbon in middle fraction FOM that partial hydrogenation saturated reaction occur.

Compared with embodiment one, the specification of equipment and structure of 3 floating bed hydrogenation reactors R101E, R201E, R202E are not Become, the overall hydrogenation process that the first hydrogenation process R10, the second hydrogenation process R20 are constituted, to " heavy distillat FOD+ heat Total air speed of high score oil RFOLM-P-THPS-L " is 0.667h^-1。

The present embodiment, compared with embodiment one, in the middle coalite tar for the hydrocarbon composition that normal boiling point is 355~435 DEG C Fraction FOM is not directly entered the first hydrogenation process R10 instead of, by using the pre-add of fixed bed hydrogenation finishing reactor Hydrogen process RFOLM, which is converted into hydrogenation reaction effluent RFOLM-P and is separated into after hot high score oil RFOLM-P-THPS-L, enters the One hydrogenation process R10；

Table 9 is the first hydrogenation process R10 operating conditions and operating result of embodiment two；

Table 10 is the process conditions of the heat from hydrogenation cracking reaction process R20 of embodiment two；

Table 11 is portion of product yield distribution obtained by the heat from hydrogenation cracking reaction process R20 of embodiment two.

As can be seen that the effect of the present embodiment is：

1. the quantity of the fresh tar stock of the first, second slurry-bed hydrocracking device reduces about 42.6%, i.e., Fraction FOM adds hydrogen by its pre- hydrogenation process RFOLM in the middle coalite tar that the hydrocarbon that normal boiling point is 355~435 DEG C forms The hydrogenated oil that the hydrogen-containing hydrocarbon stream SHS that product is served as includes is replaced, the total hydrogen consumption of 3 suspended-bed reactors and total anti- Answer thermal discharge that can reduce at least 30%；

2. the overall temperature rise and reduction average reaction temperature, raising smooth operation of 3 suspended-bed reactors can be significantly reduced, Conducive to reduction thermal cracking gas making reaction, reduce thermal condensation coking reaction；

First hydrogenation process R10, under conditions of hydrocarbon HDS weight chemistry hydrogen consumption inferior is basically unchanged, hydrocarbon inferior HDS gum asphalt hydrogenation and removing rates improve 2.5~3.0%, and hydrocarbon HDS carbon residues hydrogenation and removing rate inferior improves 3.0~ 3.5%；

3. compared with implementing one, partial suspended bed hydroprocessing reaction task is fixed bed hydroprocessing reaction process and is replaced, and solid Fixed bed hydrogenation process is located at the upstream of the first hydrogenation process R10 using floating bed hydrogenation reactor, is conducive to first The preheating of hydrogenation process R10, it is convenient to realize that substep improves the start-up process of hydrocarbon HDS inventorys inferior, it is convenient to Realize that substep reduces the shut-down process of hydrocarbon HDS inventorys inferior；

4. compared with implementing one, forms fixed bed hydrogenation reaction product and add as solvent washing heavy distillat FOD suspension beds The on-line uninterruption cleaning process of hydrogen heat cracking reaction process thermal condensation object is conducive to extend heavy distillat FOD floating bed hydrogenation hot tearings Change reaction process cycle of oparation.

5. compared with implementing one, the hydrogen-oil ratio of the first hydrogenation process R10 reduces 33% and is reduced to 200, very bright The aobvious liquid phase volume point rate for being conducive to further increase R10 reaction compartments, is conducive to extend the liquid phase reactor operating time；

6. compared with implementing one, the reaction temperature of the second hydrogenation process R20 reduces 9~10 DEG C, it is evident that is conducive to Reduce the thermal condensation reaction of polycyclic aromatic hydrocarbon；

7. compared with implementing one, the hydrogen-oil ratio of the second hydrogenation process R20 reduces 16.67% and is reduced to 750, very The apparent liquid phase volume point rate for being conducive to further increase R20 reaction compartments, is conducive to extend the liquid phase reactor operating time；

8. with implement one compared with, the first hydrogenation process R10, heat from hydrogenation cracking reaction process R20 general reaction knot Fruit, lightweight oily yield further increase, and show as " pre- the first hydrogenation processes of hydrogenation process RFOLM+ R10+ heat from hydrogenation crackings The conventional gas Auditory steady-state responses that reaction process R20 " is amounted to reduce 1.1~1.35wt%；

9. compared with implementing one, heat from hydrogenation cracking reaction generates and gets rid of residual oil outside oily fractional distillation process, reduce 0.40~ 0.45wt%.

What is more important significantly improves the operating characteristics of heat from hydrogenation cracking reaction process R20, is mainly reflected in：

1. considerably reducing heat cracking reaction temperature, considerably reducing heat cracking reaction overall temperature rise, increase substantially The suitable handling, stationarity of device operation, safety；

2. drastically reducing the thermal condensation coking reaction of colloid, asphalitine, getting rid of yield of bottoms outside reduces about 15%, phase The coking probability of the high pressure hot separator bottom of heat from hydrogenation cracking reaction effluent R20P should be reduced, is conducive to extend the company of device The continuous cycle of operation；

3. drastically reducing the thermal condensation coking reaction of colloid, asphalitine, heat from hydrogenation cracking reaction is significantly reduced Colloid, the concentration of asphalitine in the Liquid product recycle oil of journey R20 and condensed ring degree, reduce heat from hydrogenation cracking reaction effluent The coking probability of R20P wall of reactor is conducive to steady production and extends the continuous operation period of device.

The the first hydrogenation process R10 operating conditions and operating result of 9 embodiment two of table

Project	Data
		Reactor R10E	1, suspension bed
Average reaction temperature, DEG C	410~420
		React hydrogen partial pressure, MPa	17.3~18.3
Air speed, h^-1	2.0
		Hydrogen-oil ratio, v/v	200
First catalyst (including regenerated catalyst) addition (iron+molybdenum)/feedstock oil weight ratio	0.9/100
		Metal molybdenum in first catalyst: iron weight ratio is	1∶500
First catalyst particle size range, micron	1~100
		Second catalyst (including regenerated catalyst) addition, catalyst/feed weight of oil ratio	0.2/100
Second catalyst particle size range, micron	15~75
		Normal bottom heavy oil direct circulation amount/go the de- solid amount of vacuum tower	4/1
Vulcanizing agent dimethyl sulfide/feedstock oil	2/100
		Hydrocarbon HDS weight chemistry hydrogen consumption inferior, weight %	0.55~0.65
Hydrocarbon HDS gum asphalts hydrogenation and removing rate inferior, %	11.0~12.5
		Hydrocarbon HDS carbon residues hydrogenation and removing rate inferior, %	12.5~15.0

The process conditions of the heat from hydrogenation cracking reaction process R20 of 10 embodiment two of table

Project	Data
		Average reaction temperature, DEG C	435~438
React hydrogen partial pressure, MPa	17~18
		Air speed, h^-1	1.0
Hydrogen-oil ratio, v/v	750
		First catalyst (including regenerated catalyst) addition (iron+molybdenum)/feedstock oil weight ratio	0.9/100
Metal molybdenum in first catalyst: iron weight ratio is	1∶500
		First catalyst particle size range, micron	1~100
Second catalyst (including regenerated catalyst) addition, catalyst/feed weight of oil ratio	0.2/100
		Second catalyst particle size range, micron	15~75
Normal bottom heavy oil direct circulation amount/go the de- solid amount of vacuum tower	4/1
		Vulcanizing agent dimethyl sulfide/feedstock oil	2/100

Portion of product yield distribution obtained by the heat from hydrogenation cracking reaction process R20 of 11 embodiment two of table

Embodiment three

Based on embodiment two, a kind of high aromatic hydrocarbons production low carbon number disclosed in combination application Chinese patent application CN105623724A The heat from hydrogenation cracking method of single hexa-atomic cyclic hydrocarbon forms second of products scheme to embodiment two.Compared with embodiment two, by second The hydrocarbon component that normal boiling point in hydrogenation reaction effluent R20P is 290~355 DEG C returns to first plus hydrogen as cracked cycle oil Not as adding hydrogen upgrading reaction process R60 raw materials to use, effect is reaction process R10：

1. to the first hydrogenation process R10, hydrogen supply hydrocarbon total amount is increased, can further improve " hydrogen supply hydrocarbon weight/coal tar Oily heavy oil HDS weight " ratio K SH；

2. using " the selective cracking function " of heat from hydrogenation cracking reaction process, voluminous carbon number is 6~10 to greatest extent Hexamethylene methane series hydrocarbon or benzene hydrocarbons.

Claims

1. the hydrocarbon heat from hydrogenation cracking method inferior for adding hydrogen aromatic hydrocarbons either shallow saturated reaction process is arranged, it is characterised in that include following step Suddenly：

(1) in the first hydrogenation process R10, there are hydrogen, hydrocarbon liquid phase, there may be the material conditions of solid particle simultaneously Under, high aromatic carbon rate poor quality hydrocarbon HDS carries out including plus the first hydrogenation reaction R10R of hydrogen aromatic hydrocarbons either shallow saturated reaction obtains first and adds Hydroformylation reaction product BASE-R10P；

First hydrogenation reaction R10R, including at least part liquid hydrocarbon feeds HDSL the hydrocarbon component HD hydrofining reaction R10- HD-HTR, hydrofining reaction R10-HD-HTR include at least the partial hydrogenation saturated reaction R10-HD-HDAR of polycyclic aromatic hydrocarbon, can Can comprising other unsaturated hydrocarbons plus hydrogen saturated reaction and/or impure hydrocarbon plus hydrogen hydrogenolysis；

The reaction of at least part removal of ccr by hydrotreating, the first hydrogenation reaction product occurs in the first hydrogenation process R10, HDS The carbon residue of hydro carbons is less than the carbon residue of hydrocarbon HDS inferior in BASE-R10P；

First hydrogenation reaction R10R is carried out under conditions of based on the liquid phase reactor, and at least part the hydrocarbon component HD occurs polycyclic The partial hydrogenation saturated reaction R10-HD-HDAR of aromatic hydrocarbons makes the aromatic carbon rate reduction of at least part the hydrocarbon component HD be converted into the hydrocarbon component HDH makes the aromatic ring of at least part polycyclic aromatic hydrocarbon component HDA be saturated to form methylene bridged bond, the first hydrogenation reaction product The aromatic carbon rate of hydro carbons is less than the aromatic carbon rate of hydrocarbon HDS inferior in BASE-R10P；

First hydrogenation reaction R10R may use hydrogenation catalyst R10C using up flow type hydrogenation reactor R10E；First adds hydrogen When reaction process R10 uses hydrogenation catalyst R10C, the reaction compartment of the up flow type hydrogenation reactor R10E used has catalyst Into the discharge of, catalyst；

There may be part the first hydrogenation reaction product BASE-R10P to deposit or stop or be circulated in and is empty inside hydrogenation reactor R10E Between；

First hydrogenation reaction product BASE-R10P, for the object of solid particle may be contained simultaneously containing hydrogen, conventional liq hydrocarbon Material；

R10P is for being discharged BASE-R10P, for that may contain the material of solid particle simultaneously containing hydrogen, conventional liq hydrocarbon；

R10P, in the form of 1 tunnel or 2 tunnels or multichannel material R10PX occur, the composition of different R10PX logistics it is identical with phase or It is different；

(2) in the second hydrogenation process R20, there are hydrogen, hydrocarbon liquid phase, there may be the mixed phase materials of solid particle simultaneously Under the conditions of, logistics R10P-XO-TOR20 carries out the second hydrogenation reaction R20R comprising heat from hydrogenation cracking reaction and obtains second plus hydrogen Reaction product BASE-R20P；

Logistics R10P-XO-TOR20, including conventional liquid hydrocarbon raw material R10P-XO-TOR20L, may include solid particulate materials R10P-XO-TOR20S；

Second hydrogenation reaction R20R, including the hydrocarbon component HDH at least part conventional liquid hydrocarbon raw material R10P-XO-TOR20L Heat from hydrogenation cracking reaction, may include at least part conventional liquid hydrocarbon raw material R10P-XO-TOR20L in the hydrocarbon component HDH plus Hydrogen refining reaction；The hydrofining reaction of second hydrogenation reaction R20R include unsaturated hydrocarbons plus hydrogen saturated reaction and/or impure Hydrocarbon adds hydrogen hydrogenolysis；

Second hydrogenation process R20 may use hydrogenation catalyst R20C using up flow type hydrogenation reactor R20E；Second When hydrogenation process R20 uses hydrogenation catalyst R20C, the reaction compartment of the up flow type hydrogenation reactor R20E used is urged Agent enters, catalyst is discharged；

There may be part the second hydrogenation reaction product BASE-R20P to deposit or stop or be circulated in and is empty inside hydrogenation reactor R20E Between；

Second hydrogenation reaction product BASE-R20P, to contain hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon while can The mixed phase material including at least gas phase and liquid phase of solid particle can be contained；

Second hydrogenation reaction effluent R20P is for being discharged the second hydrogenation reaction product BASE-R20P, to contain hydrogen, impurity group Divide, conventional gas hydrocarbon, conventional liq hydrocarbon may contain the mixed phase material including at least gas phase and liquid phase of solid particle simultaneously；

Second hydrogenation reaction effluent R20P occurs, different R20PX logistics in the form of 1 tunnel or 2 tunnels or multichannel material R20PX Composition and phase it is identical or different；

(3) hydrogen-rich being mainly made of hydrogen in volume is obtained in removal process SR, the second hydrogenation reaction effluent R20P of recycling Gas gas SRV and the possibility being mainly made of conventional liquid hydrocarbon contain the liquid stream SRL of solid particle, at least part hydrogen-rich Gas gas SRV returns to hydrogenation process and recycles.

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

(1) in the first hydrogenation process R10, there are hydrogen, hydrocarbon liquid phase at least existing there may be solid particle simultaneously Under the conditions of the mixed phase material of gas-liquid two-phase, hydrocarbon HDS inferior is carried out to add first plus hydrogen based on hydrogen aromatic hydrocarbons either shallow saturated reaction anti- R10R is answered to obtain the first hydrogenation reaction product BASE-R10P；

First hydrogenation reaction R10R is carried out under conditions of based on the liquid phase reactor, and at least part the hydrocarbon component HD occurs polycyclic The partial hydrogenation saturated reaction R10-HD-HDAR of aromatic hydrocarbons makes the aromatic carbon rate reduction of at least part the hydrocarbon component HD be converted into the hydrocarbon component HDH makes the intermediate aromatic ring of at least part polycyclic aromatic hydrocarbon component HDA be saturated to form methylene bridged bond, the production of the first hydrogenation reaction The aromatic carbon rate of hydro carbons is less than the aromatic carbon rate of hydrocarbon HDS inferior in object BASE-R10P；

First hydrogenation reaction product BASE-R10P, to contain hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon while can The mixed phase material including at least gas phase and liquid phase of solid particle can be contained；

R10P is for being discharged BASE-R10P, to contain hydrogen, impurity composition, conventional gas hydrocarbon, conventional liq hydrocarbon while may contain There is the mixed phase material including at least gas phase and liquid phase of solid particle；

The poor quality hydrocarbon HDS to add the first hydrogenation reaction R10R based on hydrogen aromatic hydrocarbons either shallow saturated reaction, refer to：First It is that the outer hydrogen of remaining deoxidation consumes R10HK, deoxidation that hydrogenation reaction R10R total hydrogen consumptions R10HT, which subtracts hydrogenation deoxidation reactive hydrogen consumption R10HDO, Outer hydrogen consumption R10HK is to add the hydrogen of hydrogen aromatic hydrocarbons either shallow saturated reaction to consume based on R10HDA, i.e. R10HDA/R10HK ＞ 0.5；

R10P enters the second hydrogenation process R20 as logistics R10P-XO-TOR20.

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

(1) one or more of following materials are selected from the first hydrogenation process R10, hydrocarbon HDS inferior：

1. oil product obtained by coalite tar or its distillate or its hot procedure, hot procedure is that coking or catalysis are split Change process or catalytic pyrolysis process；

4. oil product obtained by direct hydrogenation liquefaction of coal liquefaction process, direct hydrogenation liquefaction of coal liquefaction process includes using hydrogen supply dissolvent oil Direct hydrogenation liquefaction of coal liquefaction process, oil coal refines process altogether, coal faces hydrogen thermosol liquefaction process；

6. oil product obtained by shale oil or its distillate or its hot procedure；

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

(1) hydrocarbon HDS inferior comes from coal tar, is mainly made of higher than 450 DEG C of the hydrocarbon component HD normal boiling point；

It is carried out in the first hydrogenation process R10, hydrocarbon HDS inferior to add first plus hydrogen based on hydrogen aromatic hydrocarbons either shallow saturated reaction anti- R10R is answered, the Unit Weight hydrogen consumption of hydrocarbon HDS inferior is 0.05~3.0%.

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

(1) it is 0.25~2.5% in the Unit Weight hydrogen consumption of the first hydrogenation process R10, hydrocarbon HDS inferior.

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

(1) it is 0.5~1.5% in the Unit Weight hydrogen consumption of the first hydrogenation process R10, hydrocarbon HDS inferior.

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

(1) coal tar is come from the first hydrogenation process R10, hydrocarbon HDS inferior, the hydrogenation catalyst R10C used is a kind of Compound coal tar hydrogenation catalyst, including high-activity component and low activity component；The high-activity component metal and low activity The weight ratio of component metals is 1: 10 to 10: 1；The high-activity component is or mixtures thereof the water soluble salt compound of molybdenum； The low activity group is divided into ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, catalyst R10C water contents are less than 2wt%；The powdered granule that R10C particle diameters are 1~100 μm.

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

(1) coal tar is come from the first hydrogenation process R10, hydrocarbon HDS inferior, the hydrogenation catalyst R10C used is at least wrapped Element containing Mo, Mo are M in the body of work form of the first hydrogenation process R10₀S₂In, hydrogenation catalyst R10C is 1~100 μ The powdered granule of m.

9. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) hydrocarbon HDS inferior comes from coal tar, and the operating condition of the first hydrogenation process R10 is：Temperature be 300~480 DEG C, Pressure is 6.0~30.0MPa, hydrogen/feedstock oil volume ratio is 0.01: 1~4000: 1, hydrogenation catalyst R10C is added weight and is HDS weight 0.001~8.0%, volume space velocity be 0.1~10.0hr^-1；Hydrocarbon HDS weight chemistry hydrogen consumption inferior be 0.05~ 3.0%.

10. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) hydrocarbon HDS inferior comes from coal tar, and the operating condition of the first hydrogenation process R10 is：Temperature be 350~460 DEG C, Pressure is 12.0~22.0MPa, hydrogen/feedstock oil volume ratio is 50: 1~600: 1, hydrogenation catalyst R10C is added weight and is HDS weight 0.01~5.0%, volume space velocity be 0.2~2.0hr^-1；Hydrocarbon HDS weight chemistry hydrogen consumption inferior be 0.50~ 1.5%.

11. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) coal tar is come from the first hydrogenation process R10, hydrocarbon HDS inferior, hydrocarbon HDS inferior is carried out to add hydrogen aromatic hydrocarbons either shallow The average reaction temperature of the first hydrogenation reaction R10R, the first hydrogenation process R10 based on saturated reaction is compared with second plus hydrogen is anti- Answer the average reaction temperature of process R20 15~100 DEG C low.

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

(1) hydrocarbon HDS inferior comes from coal tar, and gum asphaltic content is 10~90%, carbon residue is 0.01~25%, metal contains Amount is 2~2000PPm；

It is carried out in the first hydrogenation process R10, hydrocarbon HDS inferior to add first plus hydrogen based on hydrogen aromatic hydrocarbons either shallow saturated reaction anti- R10R, gum asphalt hydrogenation and removing rate is answered to be more than 3%, carbon residue hydrogenation and removing rate and be more than 3%.

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

(1) hydrocarbon HDS inferior comes from coal tar, and gum asphaltic content is 30~80%, carbon residue is 5~20%, tenor For 50~700PPm；

It is carried out in the first hydrogenation process R10, hydrocarbon HDS inferior to add first plus hydrogen based on hydrogen aromatic hydrocarbons either shallow saturated reaction anti- R10R, gum asphalt hydrogenation and removing rate is answered to be more than 5%, carbon residue hydrogenation and removing rate and be more than 5%.

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

It is carried out in the first hydrogenation process R10, hydrocarbon HDS inferior to add first plus hydrogen based on hydrogen aromatic hydrocarbons either shallow saturated reaction anti- R10R, gum asphalt hydrogenation and removing rate is answered to be more than 10%, carbon residue hydrogenation and removing rate and be more than 10%.

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

It is carried out in the first hydrogenation process R10, hydrocarbon HDS inferior to add first plus hydrogen based on hydrogen aromatic hydrocarbons either shallow saturated reaction anti- R10R, gum asphalt hydrogenation and removing rate is answered to be more than 15%, carbon residue hydrogenation and removing rate and be more than 15%.

16. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) hydrocarbon HDS inferior comes from coal tar, and hydrogen/feedstock oil volume ratio of the first hydrogenation process R10 is less than 400: 1.

17. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) hydrocarbon HDS inferior comes from coal tar, and hydrogen/feedstock oil volume ratio of the first hydrogenation process R10 is less than 200: 1.

18. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) hydrocarbon HDS inferior comes from coal tar, and hydrogen/feedstock oil volume ratio of the first hydrogenation process R10 is less than 50: 1.

19. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) hydrocarbon HDS inferior comes from coal tar, adds using 2 times or repeatedly to the reaction compartment of the first hydrogenation process R10 Method hydrogen make-up.

20. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) hydrocarbon HDS inferior comes from coal tar, and the liquid phase volume point rate of the reaction compartment of the first hydrogenation process R10 is higher than 0.5。

21. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) hydrocarbon HDS inferior comes from coal tar, and the liquid phase volume point rate of the reaction compartment of the first hydrogenation process R10 is higher than 0.7。

22. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) hydrocarbon HDS inferior comes from coal tar, and the liquid phase volume of the reaction compartment of the first hydrogenation process R10 divides rate to be 0.90 ~1.0.

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

(1) in the first hydrogenation process R10, the end product of the first hydrogenation process R10 or intermediate product are considered as instead Answer product R10MP, setting thermal high separation process R10MP-THPS；

It obtains being higher than containing dissolving hydrogen, normal boiling point in thermal high separation process R10MP-THPS, separation reaction product R10MP The hot high score liquid R10MP-THPS-L and net product stream R10MP-THPS-PP, R10MP- of 350 DEG C of conventional liquid hydrocarbon Solids may be contained in THPS-L；Net product stream R10MP-THPS-PP enters the adjacent hydroconversion reaction zone in downstream；

The logistics R10MP-THPS-LR comprising hydrocarbon liquids based on hot high score liquid R10MP-THPS-L returns to upstream and adds hydrogen anti- Area R10Z is answered to be used as cycle liquid phase；

The weight flow rate for defining R10MP-THPS-LR and the upstream of upstream hydroconversion reaction zone R10Z and R10Z that may be present are whole The ratio between total weight flow rate of hydrocarbon HDS raw materials inferior of hydroconversion reaction zone is recycle ratio KR100, and recycle ratio KR100 is 0.05~30.

24. according to claim 23 the method, it is characterised in that：

(1) it is 0.5~10 in the first hydrogenation process R10, recycle ratio KR100.

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

(1) in the first hydrogenation process R10, when using hydrogenation catalyst R10C, any up flow type hydrogenation reaction using 1 kind in following of the structure type of device R10E, when the up flow type hydrogenation reactor that the first hydrogenation process R10 is used When R10E is 2 or more, the structure type of up flow type hydrogenation reactor R10E is identical or different：

1. suspension bed；

2. ebullated bed；

3. moving bed.

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

(1) in the first hydrogenation process R10, existing solid particle is selected from one of the following or 2 kinds or a variety of：

2. catalyst granules；

3. iron rust particle；

4. particles of inorganic material；

5. coking of coal process generate into the solid particle in coal tar；

7. the solid particle from shale；

8. the solid particle from oil-sand；

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

The reaction compartment of (1) first hydrogenation process R10 is divided into the sub- hydroconversion reaction zone of 2 or multiple serial operations；

Hydrocarbon HDS inferior points are two-way or demultiplex raw material, and first via poor quality hydrocarbon HDS1 enters the first sub- hydroconversion reaction zone R101, Second tunnel poor quality hydrocarbon HDS2 is directly entered the second sub- hydroconversion reaction zone R102 without R101；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, last height The reaction effluent of hydroconversion reaction zone is used as the first hydrogenation reaction effluent R10P.

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

The reaction compartment of (1) first hydrogenation process R10 is divided into the sub- hydroconversion reaction zone of 2 serial operations：First son plus hydrogen Reaction zone R101, the second sub- hydroconversion reaction zone R102；

Hydrocarbon HDS inferior points are two-way, and first via poor quality hydrocarbon HDS1 enters the first sub- hydroconversion reaction zone R101, the second tunnel poor quality hydrocarbon HDS2 is directly entered the second sub- hydroconversion reaction zone R102；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, the first son plus hydrogen Reaction zone reaction effluent R101P enters the second sub- hydroconversion reaction zone R102, the second sub- hydroconversion reaction zone reaction effluent R102P That is the reaction effluent of last sub- hydroconversion reaction zone is used as the first hydrogenation reaction effluent R10P；

The ratio that first via poor quality hydrocarbon HDS1 accounts for all hydrocarbon HDS inferior is 0.10~0.90.

29. according to the method for claim 28, it is characterised in that：

(1) ratio that all hydrocarbon HDS inferior are accounted in the first hydrogenation process R10, first via poor quality hydrocarbon HDS1 is 0.30~ 0.70。

30. according to the method for claim 28, it is characterised in that：

(1) ratio that all hydrocarbon HDS inferior are accounted in the first hydrogenation process R10, first via poor quality hydrocarbon HDS1 is 0.40~ 0.60。

31. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

The reaction compartment of (1) first hydrogenation process R10 is divided into the sub- hydroconversion reaction zone of 3 serial operations：First son plus hydrogen Reaction zone R101, the second sub- hydroconversion reaction zone R102, the sub- hydroconversion reaction zone R103 of third；

Tri- tunnels hydrocarbon HDS Fen Wei inferior, first via poor quality hydrocarbon HDS1 enter the first sub- hydroconversion reaction zone R101, the second tunnel poor quality hydrocarbon HDS2 is directly entered the second sub- hydroconversion reaction zone R102, and third road poor quality hydrocarbon HDS3 is directly entered the sub- hydroconversion reaction zone of third R103；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, the first son plus hydrogen Reaction zone reaction effluent R101P enters the second sub- hydroconversion reaction zone R102, the second sub- hydroconversion reaction zone reaction effluent R102P Into the sub- hydroconversion reaction zone R103 of third, the sub- hydroconversion reaction zone reaction effluent R103P of third i.e. last sub- hydrogenation reaction The reaction effluent in area is used as the second hydrogenation reaction effluent R10P；

The ratio that first via poor quality hydrocarbon HDS1 accounts for all hydrocarbon HDS inferior is 0.10~0.75, and the second tunnel poor quality hydrocarbon HDS2 accounts for whole The ratio of hydrocarbon HDS inferior is 0.10~0.75.

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

(1) ratio that all hydrocarbon HDS inferior are accounted in the first hydrogenation process R10, first via poor quality hydrocarbon HDS1 is 0.15~ The ratio that 0.5, the second tunnel poor quality hydrocarbon HDS2 account for all hydrocarbon HDS inferior is 0.15~0.5.

33. according to the method for claim 31, it is characterised in that：

(1) ratio that all hydrocarbon F1 inferior are accounted in the first hydrogenation process R10, first via poor quality hydrocarbon HDS1 is 0.25~ The ratio that 0.45, the second tunnel poor quality hydrocarbon HDS2 account for all hydrocarbon F1 inferior is 0.25~0.45.

34. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(1) in the first hydrogenation process R10, the reaction compartment of the first hydrogenation process R10 is divided into 3 serial operations Sub- hydroconversion reaction zone：First sub- hydroconversion reaction zone R101, the second sub- hydroconversion reaction zone R102, the sub- hydroconversion reaction zone R103 of third, 4th sub- hydroconversion reaction zone R104；

Tetra- tunnels hydrocarbon HDS Fen Wei inferior, first via poor quality hydrocarbon HDS1 enter through the first sub- hydroconversion reaction zone R101, and the second tunnel is inferior Hydrocarbon HDS2 is directly entered the second sub- hydroconversion reaction zone R102, and third road poor quality hydrocarbon HDS3 is directly entered the sub- hydroconversion reaction zone of third R103, the 4th tunnel poor quality hydrocarbon HDS4 are directly entered the 4th sub- hydroconversion reaction zone R104；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, the first son plus hydrogen Reaction zone reaction effluent R101P enters the second sub- hydroconversion reaction zone R102, the second sub- hydroconversion reaction zone reaction effluent R102P Enter the 4th sub- hydroconversion reaction zone into the sub- hydroconversion reaction zone R103 of third, the sub- hydroconversion reaction zone reaction effluent R103P of third R104, the 4th sub- hydroconversion reaction zone reaction effluent the R104P i.e. reaction effluent of last sub- hydroconversion reaction zone are as the Two hydrogenation reaction effluent R10P are used；

The ratio that first via poor quality hydrocarbon HDS1 accounts for all hydrocarbon HDS inferior is 0.05~0.50, and the second tunnel poor quality hydrocarbon HDS2 accounts for whole The ratio of hydrocarbon HDS inferior is 0.05~0.50, the ratio that third road poor quality hydrocarbon HDS32 accounts for all hydrocarbon HDS inferior is 0.05~ 0.50。

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

(1) ratio that all hydrocarbon HDS inferior are accounted in the first hydrogenation process R10, first via poor quality hydrocarbon HDS1 is 0.15~ The ratio that 0.40, the second tunnel poor quality hydrocarbon HDS2 account for all hydrocarbon HDS inferior is 0.15~0.40, and third road poor quality hydrocarbon HDS3 accounts for whole The ratio of hydrocarbon HDS inferior is 0.15~0.40.

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

(1) ratio that all hydrocarbon HDS inferior are accounted in the first hydrogenation process R10, first via poor quality hydrocarbon HDS1 is 0.20~ The ratio that 0.30, the second tunnel poor quality hydrocarbon HDS2 account for all hydrocarbon HDS inferior is 0.20~0.30, and third road poor quality hydrocarbon HDS3 accounts for whole The ratio of hydrocarbon HDS inferior is 0.20~0.30.

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

(1) in the first hydrogenation process R10, the reaction compartment of First reactor R101E is divided at least two serial operation Sub- reaction compartment R101E1, R101E2；

Hydrocarbon HDS inferior points are two-way or demultiplex raw material HDS1, HDS2 etc., and first via poor quality hydrocarbon HDS1 enters the first son and reacts Space R101E1, the second tunnel poor quality hydrocarbon HDS2 are directly entered the second sub- reaction compartment R101E2, remaining existing branch poor quality hydrocarbon It is directly entered and subsequently corresponds to sub- hydroconversion reaction zone.

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

(1) in the first hydrogenation process R10, the reaction compartment of the First reactor R101E used is divided at least two series connection The sub- reaction compartment of operation；

Hydrocarbon HDS inferior points are two-way or demultiplex raw material HDS1, HDS2 etc., and first via poor quality hydrocarbon HDS1 is reacted by First The bottom inlet of device R101E enters the first sub- reaction compartment R101E1, and the second tunnel poor quality hydrocarbon HDS2 is anti-by being arranged in First The fluid distributor in device R101E is answered to enter the second sub- reaction compartment R101E2, remaining existing branch poor quality hydrocarbon passes through arrangement Fluid distributor in First reactor R101E, which enters, subsequently corresponds to sub- reaction zone space.

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

(1) in the first hydrogenation process R10, the hydrogenation reactor R10E used is 1~3.

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

(1) in the first hydrogenation process R10, the hydrogenation reactor R10E used is 1~2.

41. according to any one of Claims 1-4 0 the method, it is characterised in that：

(1) entering first in the first hydrogenation process R10, the hydrogen-containing hydrocarbon stream SHS-TOR10 containing hydrogen supply hydrocarbon SH adds hydrogen anti- Process R10 is answered to be contacted with the HD components of hydrocarbon HDS inferior or its hydro-conversion object；

The hydrogen supply hydrocarbon SH refers to that normal boiling point is polycyclic higher than the double ring arene of 330 DEG C of fractional saturation and/or fractional saturation Aromatic hydrocarbons；The ratio of hydrogen supply hydrocarbon SH weight and conventional liquid the hydrocarbon component total weight in logistics SHS-TOR10 in logistics SHS-TOR10, It is higher by ratio at least 3 weights of hydrogen supply hydrocarbon SH weight and conventional liquid the hydrocarbon component total weight in hydrocarbon HDS inferior in hydrocarbon HDS inferior Measure %；Conventional liquid the hydrocarbon component protium average weight content is higher by the protium weight of hydrocarbon HDS inferior in logistics SHS-TOR10 Content at least 1.5 weight %.

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

(1) hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component gross weight in the first hydrogenation process R10, logistics SHS-TOR10 Amount ratio is higher than 10 weight %；

The weight flow SHS-TOR10W and normal boiling point in hydrocarbon HDS inferior for defining hydrogen-containing hydrocarbon stream SHS-TOR10 are higher than 450 DEG C The ratio between the weight flow HDW of the hydrocarbon component HD be KSH, i.e. KSH=SHS-TOR10W/HDW, KSH are 0.1~10.0.

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

(1) hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component gross weight in the first hydrogenation process R10, logistics SHS-TOR10 Amount ratio is higher than 15 weight %；

KSH is 0.5~5.0.

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

(1) hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component gross weight in the first hydrogenation process R10, logistics SHS-TOR10 Amount ratio is higher than 20 weight %；

KSH is 1.0~3.0.

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

(1) in the first hydrogenation process R10, there are when the sub- hydroconversion reaction zone of 2 or multiple serial operations, hydrogen-containing hydrocarbon stream SHS-TOR10 fully enters the first sub- hydroconversion reaction zone R101.

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

(1) in the first hydrogenation process R10, there are when the sub- hydroconversion reaction zone of 2 or multiple serial operations, hydrogen-containing hydrocarbon stream The 30~60% of SHS-TOR10 enter the first sub- hydroconversion reaction zone R101 as first via hydrogen-containing hydrocarbon stream SHS-TOR101, remain Remaining hydrogen-containing hydrocarbon stream SHS-TOR10X enters other sub- hydroconversion reaction zones.

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

Hydrogen-containing hydrocarbon stream SHS-TOR10 is prepared as mesh from processing hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF's with hydrogen supply hydrocarbon The hydrogenation reaction effluent HPU1P of target hydroconversion reaction zone HPU1；Hydrogen supply hydrocarbon SH weight accounts for conventional liquid in logistics SHS-TOR10 The hydrocarbon component total weight ratio is higher than 6 weight %；

The weight flow SHS-TOR10W and normal boiling point in hydrocarbon HDS inferior for defining hydrogen-containing hydrocarbon stream SHS-TOR10 are higher than 450 DEG C The ratio between the weight flow HDW of the hydrocarbon component HD be KSH, i.e. KSH=SHS-TOR10W/HDW, KSH=0.1~10.

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

Hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component total weight ratio higher than 10 weight % in hydrogen-containing hydrocarbon stream SHS-TOR10；

KSH=0.2~5；

4. mainly by being 120~350 DEG C of fractions comprising normal boiling point and low temperature coal tar that normal boiling point is 350~450 DEG C of fractions The logistics of oil distillate composition；

5. mainly by being 120~350 DEG C of fractions comprising normal boiling point and medium temperature coal tar that normal boiling point is 350~450 DEG C of fractions The logistics of oil distillate composition；

6. being mainly 120~350 DEG C of fractions and the low temperature that normal boiling point is 350~450 DEG C of fractions by the normal boiling point after dephenolize The logistics of coal tar fraction composition；

7. being mainly 120~350 DEG C of fractions and the medium temperature that normal boiling point is 350~450 DEG C of fractions by the normal boiling point after dephenolize The logistics of coal tar fraction composition.

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

In the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen supply hydrocarbon, what it is from coal tar is mainly 350~450 by normal boiling point DEG C the logistics MFS of hydrocarbon MF composition carry out hydrogen supply hydrocarbon hydrogenation reaction HPU1R processed, at least part the hydrocarbon component MF completes hydrogenation modification Hydrogenation reaction effluent HPU1P is obtained by the reaction, the hydrogen-containing hydrocarbon stream SHS-TOR10 obtained based on hydrogenation reaction effluent HPU1P Selected from the one or several of following logistics：

1. reaction effluent HPU1P is used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS-TOR10 is mixed with logistics HDS Enter the first hydrogenation process R10 afterwards；

2. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and hot high score Gas HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS- TOR10 enters the first hydrogenation process R10 after being mixed with logistics HDS；

3. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and hot high score Gas HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS- TOR10 enters hydroconversion reaction zone HPU21, gained liquid HPU1- after the hot high score oil HPU1-HSO decompressions of at least part, degassing HSOA enters the first hydrogenation process R10 after being mixed with logistics HDS；

4. reaction effluent HPU1P, which enters cold anticyclone separation process HPU1-CS, is separated into cold high score oil HPU1-CSO and cold high score Gas HPU1-CSV, the cold high score oil HPU1-CSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS- TOR10 enters the first hydrogenation process R10 after being mixed with logistics HDS；

5. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；At hydrogenated oil HPU1PO points Part is evaporated, separation hydrogenated oil HPU1PO obtains the logistics rich in hydrogen supply the hydrocarbon component, is rich in hydrogen supply the hydrocarbon component at least partially Logistics be used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS-TOR10 mix with logistics HDS after into first add hydrogen Reaction process R10；

6. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；At hydrogenated oil HPU1PO points Part is evaporated, separation hydrogenated oil HPU1PO obtains the logistics rich in hydrogen supply the hydrocarbon component, and at least part is mainly by normal boiling point It is used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS- for 350~450 DEG C of the logistics rich in hydrogen supply the hydrocarbon component composition TOR10 enters the first hydrogenation process R10 after being mixed with logistics HDS.

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

In the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen supply hydrocarbon, from coal tar is 60~450 DEG C containing normal boiling point The logistics LMFS of hydrocarbon LMF completes deep hydrofinishing reaction HPU1R and is converted into hydrogenation reaction effluent HPU1P, and normal boiling point is 60~350 DEG C of hydrocarbon is converted into naphtha and diesel component, and normal boiling point is that 350~450 DEG C of hydrocarbon is converted into rich in hydrogen supply hydrocarbon The hydrogenation tail oil of SH is selected from the one of following logistics based on the obtained hydrogen-containing hydrocarbon stream SHS-TOR10 of hydrogenation reaction effluent HPU1P It is a or several：

1. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and hot high score Gas HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS- TOR10 enters the first hydrogenation process R10 after being mixed with logistics HDS；

2. the intermediate reaction effluent HPU1MP for being prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon enters thermal high separation Process HPU1M-HS is separated into hot high score oil HPU1M-HSO and hot gas separated by high pressure separator HPU1MP-HSV, the hot high score oil of at least part HPU1M-HSO is used as hydrogen-containing hydrocarbon stream SHS-TOR10, and hydrogen-containing hydrocarbon stream SHS-TOR10 enters hydroconversion reaction zone HPU21, at least Gained degassing oil HPU1M-HSOA enters first after being mixed with logistics HDS after a part of hot high score oil HPU1M-HSO decompressions degassing Hydrogenation process R10；

3. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；At hydrogenated oil HPU1PO points Part is evaporated, separation hydrogenated oil HPU1PO obtains the logistics rich in hydrogen supply the hydrocarbon component, is rich in hydrogen supply the hydrocarbon component at least partially Logistics be used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS-TOR10 mix with logistics HDS after into first add hydrogen Reaction process R10；

4. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；At hydrogenated oil HPU1PO points Part is evaporated, separation hydrogenated oil HPU1PO obtains the logistics rich in hydrogen supply the hydrocarbon component, and at least part is mainly by normal boiling point It is used as hydrogen-containing hydrocarbon stream SHS-TOR10, hydrogen-containing hydrocarbon stream SHS- for 350~450 DEG C of the logistics rich in hydrogen supply the hydrocarbon component composition TOR10 enters the first hydrogenation process R10 after being mixed with logistics HDS.

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

In the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen supply hydrocarbon, to produce hydrogen supply hydrocarbon to greatest extent as target.

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

Hydrogen-containing hydrocarbon stream SHS-TOR10 is to be containing normal boiling point from what the second hydrogenation reaction effluent R20P of separation was obtained The distillate of 300~490 DEG C of the hydrocarbon components.

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

Hydrogen-containing hydrocarbon stream SHS-TOR10 is to be containing normal boiling point from what the second hydrogenation reaction effluent R20P of separation was obtained The distillate of 330~450 DEG C of the hydrocarbon components.

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

Hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF is contained often from what the second hydrogenation reaction effluent R20P of separation was obtained Advise the distillate that boiling point is 300~490 DEG C of the hydrocarbon components.

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

Hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF is contained often from what the second hydrogenation reaction effluent R20P of separation was obtained Advise the distillate that boiling point is 330~450 DEG C of the hydrocarbon components.

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

The coal tar fraction that hydrogen supply hydrocarbon precursor logistics SHS-TOR10BF is mainly 350~450 DEG C by normal boiling point forms；

The operating condition that the hydroconversion reaction zone HPU1 of target is prepared as with hydrogen supply hydrocarbon is：Temperature is 250~460 DEG C, pressure 6.0 ~30.0MPa, hydrogen/feedstock oil volume ratio are 300: 1~3000: 1, hydrogenation catalyst HPU3-CAT volume space velocities be 0.05~ 5.0hr^-1；Hydrocarbon HDS weight chemistry hydrogen consumption inferior is 0.5~4.5% weight.

57. according to any one of claim 1 to 6 the method, it is characterised in that：

(2) in the second hydrogenation process R20, the hydrogenation catalyst R20C used is a kind of compound coal tar hydrogenation catalysis Agent, including high-activity component and low activity component；The high-activity component metal and the weight ratio of low activity component metals are 1: 1000 to 1: 10；The high-activity component is or mixtures thereof the water soluble salt compound of molybdenum, nickel, cobalt or tungsten metal；It is described Low activity group is divided into ferric oxide ore or iron sulfide ore, and wherein iron in ore content is not less than 40wt%, catalyst water content Less than 2wt%, the powdered granule that particle diameter is 1~100 μm.

58. according to any one of claim 1 to 6 the method, it is characterised in that：

(2) in the second hydrogenation process R20, the second hydrogenation reaction R20R, including at least part liquid hydrocarbon feeds HDSL The hydrofining reaction of the hydrocarbon component HD, including the heat from hydrogenation cracking of the hydrocarbon component HD is anti-in at least part liquid hydrocarbon feeds HDSL It answers；

Second hydrogenation process R20, the hydrogenation catalyst R10C used include at least Mo elements, and Mo is in the second hydrogenation reaction mistake The body of work form of journey R20 is M₀S₂。

59. according to any one of claim 1 to 6 the method, it is characterised in that：

(2) half is included at least in the second hydrogenation process R20, the second hydrogenation reaction R20R, the hydrogenation catalyst R20C used Burnt solid particle.

60. according to any one of claim 1 to 6 the method, it is characterised in that：

(4) adding hydrogen upgrading reaction process R60, in hydrogen and under adding hydrogen upgrading catalyst R60C existence conditions, at least part The logistics SRLX of liquid stream SRL or removing solid particle based on logistics SRL, carry out plus hydrogen upgrading reaction R60R are obtained plus hydrogen Upgrading reaction product R60P adds the effect of hydrogen upgrading reaction R60R to be imurity-removal or reduce hydrocarbon ils density or reduce hydrocarbon ils boiling point Or improve Cetane number；

1. aromatic hydrocarbons deep hydrogenation saturated reaction；

2. hydro carbons deep hydrogenation denitrification reaction；

3. cycloalkane adds hydrogen ring-opening reaction；

4. hydrocarbon hydrocracking reacts；

5. hydrocarbons hydrogenation isomerization reaction.

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

(4) plus the operating condition of hydrogen upgrading reaction process R60 is：Temperature is 250~440 DEG C, pressure is 4.0~30.0MPa, adds Hydrogen upgrading catalyst R60C volume space velocities are 0.02~10.0hr^-1, hydrogen/feedstock oil volume ratio be 300: 1~4000: 1；Add hydrogen Upgrading catalyst R60C is a kind of catalyst or 2 kinds of catalyst combinations use or multiple catalysts are applied in combination.

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

(2) second hydrogenation process R20, organic oxygen hydrogenation and removing rate are more than 40%, gum asphalt hydrogenation and removing rate and are more than 40%, carbon residue hydrogenation and removing rate is more than 35%, and metal hydrogenation removal efficiency is more than 60%.

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

(1) hydrocarbon HDS inferior comes from coal tar, and gum asphaltic content is 40~80%, carbon residue is 5~20%, tenor For 50~700PPm；

(2) second hydrogenation process R20, organic oxygen hydrogenation and removing rate are more than 60%, gum asphalt hydrogenation and removing rate and are more than 60%, carbon residue hydrogenation and removing rate is more than 70%, and metal hydrogenation removal efficiency is more than 80%.

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

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

(1) (2) hydrocarbon HDS inferior comes from coal tar, and gum asphaltic content is 40~80%, carbon residue is 5~20%, metal contains Amount is 50~700PPm；

The conversion ratio that is hydrocracked of (2) second hydrogenation process R20, the hydrocarbon component HD are more than 45%.

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

(2) in the second hydrogenation process R20, the end product of the second hydrogenation process R20 or intermediate product are considered as instead Answer product R20MP, setting thermal high separation process R20MP-THPS；

Obtain high containing dissolving hydrogen, normal boiling point in thermal high separation process R20MP-THPS, separation reaction effluent R10MP Hot high score liquid R20MP-THPS-L in 350 DEG C of conventional liquid hydrocarbon and net product stream R20MP-THPS-PP, R20MP- Solids may be contained in THPS-L；Net product stream R20MP-THPS-PP enters the adjacent hydroconversion reaction zone in downstream；

The logistics R20MP-THPS-LR returns comprising hydrocarbon liquids based on hot high score liquid R20MP-THPS-L belong to second and add The upstream hydroconversion reaction zone R20Z of hydrogen reaction process R20 is used as cycle liquid phase；

Define weight flow rate and upstream hydroconversion reaction zone R20Z and the upstreams the R20Z whole hydroconversion reaction zone of R20MP-THPS-LR The ratio between total weight flow rate of hydrocarbon HDS raw materials inferior is recycle ratio KR200, and recycle ratio KR200 is 0.05~30.

67. according to claim 66 the method, it is characterised in that：

(2) in the second hydrogenation process R20, in sub- hydroconversion reaction zone setting thermal high separation process R20MP-THPS；Cycle It is 2~10 than KR200.

68. according to claim 66 the method, it is characterised in that：

Thermal high separation process RTHPS, is arranged the upper space in hydrogenation reactor, with liquid header, drain pipeline, cycle The system that pump, liquor charging pipeline form makes R20MP-THPS-LR inject in the R20Z of upstream hydrogenation reaction space.

69. according to claim 66 the method, it is characterised in that：

In high pressure hot separator R20MP-THPS-E, separation reaction effluent R10MP is obtained containing dissolving hydrogen, normal boiling point The hot high score liquid R20MP-THPS-L and net product stream R20MP-THPS-PP, R20MP- of conventional liquid hydrocarbon higher than 350 DEG C Solids may be contained in THPS-L；Net product stream R20MP-THPS-PP enters the adjacent sub- hydroconversion reaction zone in downstream.

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

(3) divide SR, setting thermal high separation process THPS in removal process；

In thermal high separation process THPS, the second hydrogenation reaction effluent R20P of separation obtain containing hydrogen, impurity hydrogenation products, The hot high score gas THPS-V of the conventional liquid hydrocarbon of conventional gas hydrocarbon and normal boiling point less than 350 DEG C and containing dissolving hydrogen, often It may contain solids in hot high score the liquid THPS-L, THPS-L of conventional liquid hydrocarbon of the rule boiling point higher than 350 DEG C.

71. according to claim 70 the method, it is characterised in that：

The operating condition of thermal high separation process THPS is：Temperature is 250~460 DEG C, pressure is 4.0~30.0MPa.

72. according to claim 70 the method, it is characterised in that：

The operating condition of thermal high separation process THPS is：Temperature is 350~440 DEG C, pressure is 10.0~25.0MPa.

73. according to claim 70 the method, it is characterised in that：

Part, the logistics THPS- comprising hydrocarbon liquids based on hot high score liquid THPS-L are shunted in hot high score liquid R10P-SL LR returns to the second hydrogenation process R20；Define THPS-LR in normal boiling point be more than 450 DEG C of the hydrocarbon components weight flow rate with it is bad The ratio between weight flow rate of HD components is recycle ratio K999 in matter hydrocarbon raw material HDS, and recycle ratio K999 is 0.05~10.

74. according to claim 73 the method, it is characterised in that：

(3) SR, recycle ratio K999 is divided to be 0.5~2 in removal process.

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

(3) divide SR, setting cold anticyclone separation process LHPS, cold low separation process LLPS, cold low point of oil cycle in removal process Wash methane process；

In cold anticyclone separation process LHPS, what it is based on the second hydrogenation reaction effluent R20P includes the second hydrogenation reaction effluent The logistics R10P-H100 of most of hydrogen component is separated into the hydrogen rich gas gas being mainly made of hydrogen in volume in R20P The LHPS-V and liquid stream LHPS-L being mainly made of conventional liquid hydrocarbon；Hydrogen rich gas gas LHPS-V is used as SRV；

It is separated into the cold low point of gas rich in conventional gas hydrocarbon after cold low separation process LLPS, liquid stream LHPS-L decompressions The LLPS-V and and liquid stream LLPS-L that is mainly made of conventional liquid hydrocarbon；

First part liquid stream LLPS-L is used as absorbing oil LLPS-LA, with the packet based on the second hydrogenation reaction effluent R20P It was detached into cold anticyclone after logistics R10P-H100 mixing containing most of hydrogen component in the second hydrogenation reaction effluent R20P Journey LHPS；Remainder liquid stream LLPS-L is used as cold low point of oily product LLPS-LP.

76. according to claim 75 the method, it is characterised in that：

The operating condition of cold anticyclone separation process LHPS is：Temperature is 20~70 DEG C, pressure is 6.0~30.0MPa；

The operating condition of cold low separation process LLPS is：Temperature is 20~70 DEG C, pressure is 0.01~3.0MPa；

Definition absorbs the ratio between the weight flow rate of oil LLPS-LA and cold low point of oily product LLPS-LP weight flow rates to absorb oil cycle It is 0.05~10 than K300, K300.

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

The operating condition of cold anticyclone separation process LHPS is：Temperature is 20~50 DEG C, pressure is 8.0~25.0MPa；、

The operating condition of cold low separation process LLPS is：Temperature is 20~50 DEG C, pressure is 0.2~1.0MPa；

K300 is 0.5~4.

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

(2) in the second hydrogenation process R20, when using hydrogenation catalyst R20C, the structure of up flow type hydrogenation reactor R20E 1 kind or several in following of form：

1. suspension bed；

2. ebullated bed；

3. moving bed.

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

(2) in the second hydrogenation process R20, existing solid particle is selected from one of the following or several：

2. catalyst granules；

3. iron rust particle；

4. particles of inorganic material；

5. coking of coal process generate into the solid particle in coal tar；

7. the solid particle from shale；

8. the solid particle from oil-sand；

80. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(2) in the second hydrogenation process R20, the operating condition of the second hydrogenation process R20 is：Temperature is 300~480 DEG C, pressure be 6.0~30.0MPa, hydrogen/feedstock oil volume ratio is 300: 1~4000: 1, weight is added in hydrogenation catalyst R10C For HDS weight 0.001~8.0%, volume space velocity be 0.1~10.0hr^-1；Hydrocarbon HDS weight chemistry hydrogen consumption inferior be 0.5~ 5.0%.

81. according to the method described in claim 1, it is characterized in that：

The reaction compartment of (2) second hydrogenation process R20 is divided into the sub- hydroconversion reaction zone of 2 or multiple serial operations；

R10P-XO-TOR20 points of logistics is two-way or demultiplex raw material, and first via logistics R10P-XO-TOR201 enters first Sub- hydroconversion reaction zone R201, the second tunnel logistics R10P-XO-TOR202 are directly entered the second sub- hydroconversion reaction zone without R201 R202；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, last height The reaction effluent of hydroconversion reaction zone is used as the second hydrogenation reaction effluent R20P.

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

(2) in the second hydrogenation process R20, bis- tunnels logistics R10P-XO-TOR20 Fen Wei, first via logistics R10P-XO- TOR201 enters the first sub- hydroconversion reaction zone R201, and the second tunnel logistics R10P-XO-TOR202 is directly entered the second sub- hydrogenation reaction Area R202；

83. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(2) in the second hydrogenation process R20, tri- tunnels logistics R10P-XO-TOR20 Fen Wei, first via logistics R10P-XO- TOR201 enters the first sub- hydroconversion reaction zone R201, and the second tunnel logistics R10P-XO-TOR202 is directly entered the second sub- hydrogenation reaction Area R202, third road logistics R10P-XO-TOR203 are directly entered the sub- hydroconversion reaction zone R203 of third；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, the first son plus hydrogen Reaction zone reaction effluent R201P enters the second sub- hydroconversion reaction zone R202, the second sub- hydroconversion reaction zone reaction effluent R202P Into the sub- hydroconversion reaction zone R203 of third, the sub- hydroconversion reaction zone reaction effluent R203P of third i.e. last sub- hydrogenation reaction The reaction effluent in area is used as the second hydrogenation reaction effluent R20P；

The ratio that first via logistics R10P-XO-TOR201 accounts for whole logistics R10P-XO-TOR20 is 0.1~0.75, the second road object The ratio that stream R10P-XO-TOR202 accounts for whole logistics R10P-XO-TOR20 is 0.1~0.75.

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

1. in the second hydrogenation process R20, first via logistics R10P-XO-TOR201 accounts for whole logistics R10P-XO-TOR20 Ratio be 0.15~0.50, the ratio that the second tunnel logistics R10P-XO-TOR202 accounts for whole logistics R10P-XO-TOR20 is 0.15~0.50.

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

1. in the second hydrogenation process R20, first via logistics R10P-XO-TOR201 accounts for whole logistics R10P-XO-TOR20 Ratio be 0.25~0.45, the ratio that the second tunnel logistics R10P-XO-TOR202 accounts for whole logistics R10P-XO-TOR20 is 0.25~0.45.

86. according to the method described in claim 1, it is characterized in that the operating condition of each step is：

(2) in the second hydrogenation process R20, tetra- tunnels logistics R10P-XO-TOR20 Fen Wei, first via logistics R10P-XO- TOR201 enters the first sub- hydroconversion reaction zone R201, and the second tunnel logistics R10P-XO-TOR202 is directly entered the second sub- hydrogenation reaction Area R202, third road logistics R10P-XO-TOR203 are directly entered third sub- hydroconversion reaction zone R203, the 4th tunnel logistics R10P- XO-TOR204 is directly entered the 4th sub- hydroconversion reaction zone R204；

The reaction effluent of the upper alien hydroconversion reaction zone of arranged in series enters the adjacent sub- hydroconversion reaction zone in downstream, the first son plus hydrogen Reaction zone reaction effluent R201P enters the second sub- hydroconversion reaction zone R202, the second sub- hydroconversion reaction zone reaction effluent R202P Enter the 4th sub- hydroconversion reaction zone into the sub- hydroconversion reaction zone R203 of third, the sub- hydroconversion reaction zone reaction effluent R203P of third R204, the 4th sub- hydroconversion reaction zone reaction effluent the R204P i.e. reaction effluent of last sub- hydroconversion reaction zone are as the Two hydrogenation reaction effluent R20P are used；

The ratio that first via logistics R10P-XO-TOR201 accounts for whole logistics R10P-XO-TOR20 is 0.05~0.5, the second road object The ratio that stream R10P-XO-TOR202 accounts for whole logistics R10P-XO-TOR20 is 0.05~0.5, third road logistics R10P-XO- The ratio that TOR203 accounts for whole logistics R10P-XO-TOR20 is 0.05~0.5.

87. according to the method described in claim 86, it is characterised in that：

(2) whole logistics R10P-XO-TOR20 are accounted in the second hydrogenation process R20, first via logistics R10P-XO-TOR201 Ratio be 0.15~0.4, the second tunnel logistics R10P-XO-TOR202 account for whole logistics R10P-XO-TOR20 ratio be 0.15 The ratio that~0.4, third road logistics R10P-XO-TOR203 account for whole logistics R10P-XO-TOR20 is 0.15~0.4.

88. according to the method described in claim 86, it is characterised in that：

(2) whole logistics R10P-XO-TOR20 are accounted in the second hydrogenation process R20, first via logistics R10P-XO-TOR201 Ratio be 0.20~0.30, the ratio that the second tunnel logistics R10P-XO-TOR202 accounts for whole logistics R10P-XO-TOR20 is The ratio that 0.20~0.30, third road logistics R10P-XO-TOR203 account for whole logistics R10P-XO-TOR20 is 0.20~0.30.

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

(3) in removal process SR, the H of hydrogen rich gas gas SRV₂Volumetric concentration is more than 75%.

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

(3) in removal process SR, the H of hydrogen rich gas gas SRV₂Volumetric concentration is more than 85%.

91. according to any one of claim 1 to 6 the method, it is characterised in that：

(2) entering second in the second hydrogenation process R20, the hydrogen-containing hydrocarbon stream SHS-TOR20 containing hydrogen supply hydrocarbon SH adds hydrogen anti- Process R20 is answered to be contacted with R10P-XO-TOR20 or its hydro-conversion object；

The hydrogen supply hydrocarbon SH refers to that normal boiling point is polycyclic higher than the double ring arene of 330 DEG C of fractional saturation and/or fractional saturation Aromatic hydrocarbons；The ratio of hydrogen supply hydrocarbon SH weight and conventional liquid the hydrocarbon component total weight in logistics SHS-TOR20 in logistics SHS-TOR20, Hydrogen supply hydrocarbon SH weight and conventional liquid the hydrocarbon component total weight in logistics R10P-XO-TOR20 in high effluent stream R10P-XO-TOR20 Ratio at least 3 weight %；The high effluent stream of conventional liquid the hydrocarbon component protium average weight content in logistics SHS-TOR20 The protium weight content of the conventional liquid hydrocarbon of R10P-XO-TOR20 at least 1.5 weight %.

92. according to claim 91 the method, it is characterised in that：

(2) hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component total weight ratio higher than 10 weight % in logistics SHS-TOR20；

Define normal boiling point in the weight flow SHS-TOR20W and logistics R10P-XO-TOR20 of hydrogen-containing hydrocarbon stream SHS-TOR20 The ratio between weight flow R10P-XO-TOR20-HDW of the hydrocarbon component HD higher than 450 DEG C is KSH200, i.e. KSH200=SHS- TOR20W/R10P-XO-TOR20-HDW, KSH200 are 0.1~10.0.

93. according to claim 92 the method, it is characterised in that：

(2) hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component total weight ratio higher than 15 weight % in logistics SHS-TOR20；

KSH200 is 0.5~5.0.

94. according to claim 92 the method, it is characterised in that：

(2) hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component total weight ratio higher than 20 weight % in logistics SHS-TOR20；

KSH200 is 1.0~3.0.

95. according to claim 91 the method, it is characterised in that：

Sub- hydroconversion reaction zone of (2) second R20 points of the hydrogenation processes at least two serial operation, hydrogen-containing hydrocarbon stream SHS- TOR20 fully enters the first sub- hydroconversion reaction zone R201.

96. according to claim 92 the method, it is characterised in that：

Sub- hydroconversion reaction zone of (2) second R20 points of the hydrogenation processes at least two serial operation, hydrogen-containing hydrocarbon stream SHS- The 30~60% of TOR20 enter the first sub- hydroconversion reaction zone R201 as first via hydrogen-containing hydrocarbon stream SHS-TOR201, remaining Hydrogen-containing hydrocarbon stream SHS-TOR20X enters other sub- hydroconversion reaction zones.

97. according to claim 91 the method, it is characterised in that：

Hydrogen-containing hydrocarbon stream SHS-TOR20 is prepared as mesh from processing hydrogen supply hydrocarbon precursor logistics SHS-TOR20BF's with hydrogen supply hydrocarbon The hydrogenation reaction effluent HPU1P of target hydroconversion reaction zone HPU1；Hydrogen supply hydrocarbon SH weight accounts for often in hydrogen-containing hydrocarbon stream SHS-TOR20 It advises liquid hydrocarbon component weight ratio and is higher than 6 weight %；

Define normal boiling point in the weight flow SHS-TOR20W and logistics R10P-XO-TOR20 of hydrogen-containing hydrocarbon stream SHS-TOR20 The ratio between weight flow R10P-XO-TOR20-HDW of the hydrocarbon component HD higher than 450 DEG C is KSH200, i.e. KSH200=SHS- TOR20W/R10P-XO-TOR20-HDW, KSH200=0.1~10.

98. according to the method described in claim 97, it is characterised in that：

Hydrogen supply hydrocarbon SH weight accounts for conventional liquid the hydrocarbon component total weight ratio higher than 10 weight % in hydrogen-containing hydrocarbon stream SHS-TOR20；

KSH200=0.2~5；

99. according to the method described in claim 98, it is characterised in that：

In the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen supply hydrocarbon, what it is from coal tar is mainly 350~450 by normal boiling point DEG C the logistics MFS of hydrocarbon MF composition carry out hydrogen supply hydrocarbon hydrogenation reaction HPU1R processed, at least part the hydrocarbon component MF completes hydrogenation modification Hydrogenation reaction effluent HPU1P is obtained by the reaction, the hydrogen-containing hydrocarbon stream SHS-TOR20 obtained based on hydrogenation reaction effluent HPU1P Selected from the one or several of following logistics：

1. reaction effluent HPU1P is used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS-TOR20 is mixed with logistics HDS Enter the second hydrogenation process R20 afterwards；

2. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and hot high score Gas HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS- TOR20 enters the second hydrogenation process R20 after being mixed with logistics HDS；

3. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and hot high score Gas HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS- TOR20 enters the second hydrogenation process R20, gained liquid after the hot high score oil HPU1-HSO decompressions of at least part, degassing HPU1-HSOA enters the second hydrogenation process R20 after being mixed with logistics HDS；

4. reaction effluent HPU1P, which enters cold anticyclone separation process HPU1-CS, is separated into cold high score oil HPU1-CSO and cold high score Gas HPU1-CSV, the cold high score oil HPU1-CSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS- TOR20 enters the second hydrogenation process R20 after being mixed with logistics HDS；

5. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；At hydrogenated oil HPU1PO points Part is evaporated, separation hydrogenated oil HPU1PO obtains the logistics rich in hydrogen supply the hydrocarbon component, is rich in hydrogen supply the hydrocarbon component at least partially Logistics be used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS-TOR20 mix with logistics HDS after into second add hydrogen Reaction process R20；

6. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；At hydrogenated oil HPU1PO points Part is evaporated, separation hydrogenated oil HPU1PO obtains the logistics rich in hydrogen supply the hydrocarbon component, and at least part is mainly by normal boiling point It is used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS- for 350~450 DEG C of the logistics rich in hydrogen supply the hydrocarbon component composition TOR20 enters the second hydrogenation process R20 after being mixed with logistics HDS.

100. according to the method described in claim 98, it is characterised in that：

In the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen supply hydrocarbon, from coal tar is 60~450 DEG C containing normal boiling point The logistics LMFS of hydrocarbon LMF completes deep hydrofinishing reaction HPU1R and is converted into hydrogenation reaction effluent HPU1P, and normal boiling point is 60~350 DEG C of hydrocarbon is converted into naphtha and diesel component, and normal boiling point is that 350~450 DEG C of hydrocarbon is converted into rich in hydrogen supply hydrocarbon The hydrogenation tail oil of SH is selected from the one of following logistics based on the obtained hydrogen-containing hydrocarbon stream SHS-TOR20 of hydrogenation reaction effluent HPU1P It is a or several：

1. reaction effluent HPU1P, which enters thermal high separation process HPU1-HS, is separated into hot high score oil HPU1-HSO and hot high score Gas HPU1-HSV, the hot high score oil HPU1-HSO of at least part are used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS- TOR20 enters the second hydrogenation process R20 after being mixed with logistics HDS；

2. the intermediate reaction effluent HPU1MP for being prepared as the hydroconversion reaction zone HPU1 of target with hydrogen supply hydrocarbon enters thermal high separation Process HPU1M-HS is separated into hot high score oil HPU1M-HSO and hot gas separated by high pressure separator HPU1MP-HSV, the hot high score oil of at least part HPU1M-HSO is used as hydrogen-containing hydrocarbon stream SHS-TOR20, and hydrogen-containing hydrocarbon stream SHS-TOR10 enters hydroconversion reaction zone HPU21, at least Gained degassing oil HPU1M-HSOA enters second after being mixed with logistics HDS after a part of hot high score oil HPU1M-HSO decompressions degassing Hydrogenation process R20；

3. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；At hydrogenated oil HPU1PO points Part is evaporated, separation hydrogenated oil HPU1PO obtains the logistics rich in hydrogen supply the hydrocarbon component, is rich in hydrogen supply the hydrocarbon component at least partially Logistics be used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS-TOR20 mix with logistics HDS after into second add hydrogen Reaction process R20；

4. separation reaction effluent HPU1P obtains hydrogenated oil HPU1PO and hydrogen-rich gas；At hydrogenated oil HPU1PO points Part is evaporated, separation hydrogenated oil HPU1PO obtains the logistics rich in hydrogen supply the hydrocarbon component, and at least part is mainly by normal boiling point It is used as hydrogen-containing hydrocarbon stream SHS-TOR20, hydrogen-containing hydrocarbon stream SHS- for 350~450 DEG C of the logistics rich in hydrogen supply the hydrocarbon component composition TOR20 enters the second hydrogenation process R20 after being mixed with logistics HDS.

101. according to the method described in claim 97, it is characterised in that：

In the hydroconversion reaction zone HPU1 for being prepared as target with hydrogen-containing hydrocarbon stream SHS-TOR20, it is to produce hydrogen supply hydrocarbon to greatest extent Target.

102. according to claim 91 the method, it is characterised in that：

Hydrogen-containing hydrocarbon stream SHS-TOR20 is to be containing normal boiling point from what the second hydrogenation reaction effluent R20P of separation was obtained The distillate of 300~490 DEG C of the hydrocarbon components.

103. according to claim 91 the method, it is characterised in that：

Hydrogen-containing hydrocarbon stream SHS-TOR20 is to be containing normal boiling point from what the second hydrogenation reaction effluent R20P of separation was obtained The distillate of 330~450 DEG C of the hydrocarbon components.

104. according to claim 97 the method, it is characterised in that：

Hydrogen supply hydrocarbon precursor logistics SHS-TOR20BF is contained often from what the second hydrogenation reaction effluent R20P of separation was obtained Advise the distillate that boiling point is 300~490 DEG C of the hydrocarbon components.

105. according to claim 97 the method, it is characterised in that：

Hydrogen supply hydrocarbon precursor logistics SHS-TOR20BF is contained often from what the second hydrogenation reaction effluent R20P of separation was obtained Advise the distillate that boiling point is 330~450 DEG C of the hydrocarbon components.

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

(1) in the first hydrogenation process R10, the hydrogen gas stream used is new hydrogen logistics.

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

(2) in the second hydrogenation process R20, R10P-XO-TOR20 points of logistics is the roads N branch feed stream R10P-XO- TOR201, logistics R10P-XO-TOR202 ..., logistics R10P-XO-TOR20N, wherein N >=2；

The logistics R20NE-SL that acquisition is mainly made of liquid phase from the inner space of N platform up-flow reactors R20NE, at least one Fraction of stream R20NE-SL is recycled back into the reaction compartment of the arbitrary reactor within the scope of R201E to R20NE；

The logistics R20ME-SL that acquisition is mainly made of liquid phase from the inner space of M platform up-flow reactors R1ME, at least one Fraction of stream R20ME-SL is recycled back to the reaction compartment of any one reactor after reactor R20NE.

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

The operating condition of (2) second hydrogenation process R20 is：Temperature is 300~500 DEG C, pressure is 6.0~30.0MPa, hydrogen Gas/feedstock oil volume ratio is 300: 1~4000: 1, hydrogenation catalyst R20C is added that weight is HDS weight 0.001~8.0%, Volume space velocity is 0.1~10.0hr^-1。

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

The operating condition of (2) second hydrogenation process R20 is：Temperature is 350~460 DEG C, pressure be 10.0~25.0MPa, Hydrogen/feedstock oil volume ratio is 300: 1~2000: 1, hydrogenation catalyst R10C additions weight is HDS weight 0.01~ 5.0%, volume space velocity is 0.2~5.0hr^-1。

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

The operating condition of (2) second hydrogenation process R20 is：Temperature is 380~460 DEG C, pressure be 17.0~23.0MPa, Hydrogen/feedstock oil volume ratio is 500: 1~1200: 1, hydrogenation catalyst R10C is added that weight is HDS weight 0.3~3.0%, Volume space velocity is 0.3~2.0hr^-1。

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

It is carried out in the first hydrogenation process R10, hydrocarbon HDS inferior to add first plus hydrogen based on hydrogen aromatic hydrocarbons either shallow saturated reaction anti- R10R, gum asphalt hydrogenation and removing rate is answered to be more than 3%, carbon residue hydrogenation and removing rate and be more than 3%；

(2) the protium weight of conventional liquid hydrocarbon contains in the second hydrogenation process R20, the second hydrogenation reaction effluent R20P Amount is higher than 9.0%；

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

It is carried out in the first hydrogenation process R10, hydrocarbon HDS inferior to add first plus hydrogen based on hydrogen aromatic hydrocarbons either shallow saturated reaction anti- R10R, gum asphalt hydrogenation and removing rate is answered to be more than 5%, carbon residue hydrogenation and removing rate and be more than 5%；

(2) conventional in coal tar, the second hydrogenation reaction effluent R20P in the second hydrogenation process R20, hydrocarbon HDS inferior The protium weight content of liquid hydrocarbon is higher than 10.0%；

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

The hydrogenation reactor R20X that (2) second hydrogenation process R20 are used is 1~5.

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

The hydrogenation reactor R20X that (2) second hydrogenation process R20 are used is 2~4.

115. according to claim 97 the method, it is characterised in that：

(2) the coal tar fraction group that hydrogen supply hydrocarbon precursor logistics SHS-TOR20-BF is mainly 350~450 DEG C by normal boiling point At；

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

(3) enter hydrogen purification list as hydrogen SRV-C to be purified in recovery section SR, at least part hydrogen rich gas gas SRV First GH100 is separated into purifying hydrogen of hydrogen SRV-CH and purification tail gas SRV-CC, and at least part purifying hydrogen of hydrogen SRV-CH is returned plus hydrogen Reaction process recycles.

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

(1) hydrocarbon HDS inferior contains organic oxygen；

(3) hydrogen-rich being mainly made of hydrogen in volume is obtained in removal process SR, the second hydrogenation reaction effluent R20P of recycling The gas gas SRV and liquid stream SRL being mainly made of conventional liquid hydrocarbon, at least first part's hydrogen rich gas gas SRV return to the Two hydrogenation process R20 are recycled as reaction process circulating hydrogen SRV-TO-R10, at least second part hydrogen rich gas Gas SRV with based on the second hydrogenation reaction effluent R20P containing most of hydrogen in the second hydrogenation reaction effluent R20P, It is recycled as the circulating hydrogen SRV-200 for reducing steam partial pressure after the logistics R10P-HH mixing of most of vapor；

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

(1) hydrocarbon HDS inferior comes from coal tar F00；

The hydrocarbon for being mainly 60~360 DEG C by normal boiling point is separated into coal tar F00 separate section FRAC, coal tar F00 to form Light fraction FOL and the main weight by normal boiling point more than the hydrocarbon HD comprising normal boiling point higher than 450 DEG C that 360 DEG C of hydrocarbon forms Fraction FOMH, at least part heavy distillat FOMH are used as hydrocarbon HDS inferior；At least part light fraction FOL enters pre- hydrogenation process RFOL is converted into hydrogenation reaction effluent RFOL-P, hydrogenation reaction effluent RFOL-P or its generation oil or it generates oil distillate Oil, into the first hydrogenation process R10 or the second hydrogenation process R20.

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

(1) hydrocarbon HDS inferior comes from coal tar F00；

The hydrocarbon for being mainly 60~360 DEG C by normal boiling point is separated into coal tar F00 separate section FRAC, coal tar F00 to form Light fraction FOL and the main weight by normal boiling point more than the hydrocarbon HD comprising normal boiling point higher than 450 DEG C that 360 DEG C of hydrocarbon forms Fraction FOMH, at least part heavy distillat FOMH are used as hydrocarbon HDS inferior；

Hydrogenation reaction effluent RFOL-P enters thermal high separation process RFOL-P-THPS and is separated into hot gas separated by high pressure separator RFOL-P- THPS-V and hot high score oil RFOL-P-THPS-L；

Based on the logistics RFOL-P-THPS-LX of hot high score oil RFOL-P-THPS-L, into the first hydrogenation process R10 or Two hydrogenation process R20；

(3) hydrogen-rich being mainly made of hydrogen in volume is obtained in removal process SR, the second hydrogenation reaction effluent R20P of recycling The gas gas SRV and liquid stream SRL being mainly made of conventional liquid hydrocarbon, at least part hydrogen rich gas gas SRV is returned plus hydrogen Reaction process recycles；

The removal process of hot gas separated by high pressure separator RFOL-P-THPS-V and the second hydrogenation reaction effluent of at least part at least partially The removal process SR of R20P is shared.

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

(1) hydrocarbon HDS inferior comes from coal tar F00；

(4) adding hydrogen upgrading reaction process R60, in hydrogen and under adding hydrogen upgrading catalyst R60C existence conditions, at least part Liquid stream SRL is carried out plus hydrogen upgrading reaction R60R is obtained plus hydrogen upgrading reaction product R60P, adds the effect of hydrogen upgrading reaction R60R Fruit is imurity-removal or reduces hydrocarbon ils density or reduce hydrocarbon ils boiling point；

The hydro-upgrading reaction process of hot gas separated by high pressure separator RFOL-P-THPS-V is reacted at least part plus hydrogen upgrading at least partially Process R60 is shared.

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

(1) hydrocarbon HDS inferior comes from coal tar F00；

The hydrocarbon for being mainly 60~450 DEG C by normal boiling point is separated into coal tar F00 separate section FRAC, coal tar F00 to form Light fraction FOLM and mainly by normal boiling point more than the heavy distillat FOD, at least part heavy distillat FOD that 450 DEG C of hydrocarbon forms As hydrocarbon HDS inferior；At least part light fraction FOLM is converted into hydrogenation reaction effluent into pre- hydrogenation process RFOLM RFOLM-P, hydrogenation reaction effluent RFOLM-P or its generation oil or its generation oil distillate oil, into the first hydrogenation process R10 or the second hydrogenation process R20.

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

(1) hydrocarbon HDS inferior comes from coal tar F00；

The hydrocarbon for being mainly 60~450 DEG C by normal boiling point is separated into coal tar F00 separate section FRAC, coal tar F00 to form Light fraction FOLM and mainly by normal boiling point more than the heavy distillat FOD, at least part heavy distillat FOD that 450 DEG C of hydrocarbon forms As hydrocarbon HDS inferior；

Hydrogenation reaction effluent RFOLM-P enters thermal high separation process RFOLM-P-THPS and is separated into hot gas separated by high pressure separator RFOLM-P- THPS-V and hot high score oil RFOLM-P-THPS-L；

Based on the logistics RFOLM-P-THPS-LX of hot high score oil RFOLM-P-THPS-L, into the first hydrogenation process R10 or Second hydrogenation process R20；

The removal process of hot gas separated by high pressure separator RFOLM-P-THPS-V and the second hydrogenation reaction effluent of at least part at least partially The removal process SR of R20P is shared.

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

(1) hydrocarbon HDS inferior comes from coal tar F00；

The hydro-upgrading reaction process of hot gas separated by high pressure separator RFOLM-P-THPS-V and at least part plus hydrogen upgrading are anti-at least partially Process R60 is answered to share.

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

(1) hydrocarbon HDS inferior comes from coal tar F00；

The hydrocarbon for being mainly 60~360 DEG C by normal boiling point is separated into coal tar F00 separate section FRAC, coal tar F00 to form Light fraction FOL, mainly by normal boiling point be in the middle coalite tar that 360~450 DEG C of hydrocarbon forms fraction FOM and mainly by The heavy distillat FOD that hydrocarbon of the normal boiling point more than 450 DEG C forms, at least part heavy distillat FOD are used as hydrocarbon HDS inferior；At least one Fraction FOM is converted into hydrogenation reaction effluent RFOM-P, hydrogenation reaction effluent RFOM- into pre- hydrogenation process RFOM in part P or its generation oil or its generation oil distillate oil, into the first hydrogenation process R10 or the second hydrogenation process R20.

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

(1) hydrocarbon HDS inferior comes from coal tar F00；

The hydrocarbon for being mainly 60~360 DEG C by normal boiling point is separated into coal tar F00 separate section FRAC, coal tar F00 to form Light fraction FOL, mainly by normal boiling point be in the middle coalite tar that 360~450 DEG C of hydrocarbon forms fraction FOM and mainly by The heavy distillat FOD that hydrocarbon of the normal boiling point more than 450 DEG C forms, at least part heavy distillat FOD are used as hydrocarbon HDS inferior；

Hydrogenation reaction effluent RFOM-P enters thermal high separation process RFOM-P-THPS and is separated into hot gas separated by high pressure separator RFOM-P- THPS-V and hot high score oil RFOM-P-THPS-L；

Based on the logistics RFOM-P-THPS-LX of hot high score oil RFOM-P-THPS-L, into the first hydrogenation process R10 or Two hydrogenation process R20；

The removal process of hot gas separated by high pressure separator RFOM-P-THPS-V and the second hydrogenation reaction effluent of at least part at least partially The removal process SR of R20P is shared.

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

(1) hydrocarbon HDS inferior comes from coal tar F00；

The hydro-upgrading reaction process of hot gas separated by high pressure separator RFOM-P-THPS-V is reacted at least part plus hydrogen upgrading at least partially Process R60 is shared.

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

(3) hydrogen-rich being mainly made of hydrogen in volume is obtained in removal process SR, the second hydrogenation reaction effluent R20P of recycling Gas gas SRV and the possibility being mainly made of conventional liquid hydrocarbon contain the liquid stream SRL of solid particle；

Separation liquid stream SRL obtains the thermal cracking heavy oil streams R20P-H0 of the hydrocarbon component containing normal boiling point more than 350 DEG C, At least part thermal cracking heavy oil streams R20P-HO removes the first hydrogenation process R10 as recycle oil R20P-HO-TOR10.

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

The thermal cracking heavy oil streams that the hydrocarbon component that it is mainly 350~530 DEG C by normal boiling point that separation liquid stream, which obtains, forms R20P-HO, at least part thermal cracking heavy oil streams R20P-HO go the first hydrogenation reaction as recycle oil R20P-HO-TOR10 Process R10.

129. according to claim 118 the method, it is characterised in that：

The thermal cracking heavy oil streams that the hydrocarbon component that it is mainly 350~530 DEG C by normal boiling point that separation liquid stream, which obtains, forms R20P-HO and the thermal cracking residue that mainly the hydrocarbon component by normal boiling point more than 530 DEG C forms, at least part thermal cracking heavy oil Logistics R20P-HO removes the first hydrogenation process R10 as recycle oil R20P-HO-TOR10.

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

(1) in the first hydrogenation process R10, the logistics R10P-XO-TOR20 containing hydrocarbon ils in R10P based on R10P passes through Enter the second hydrogenation process R20 after heating furnace heating.

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

Separation liquid stream obtains the thermal cracking heavy oil streams R20P-HO of the hydrocarbon component containing normal boiling point more than 350 DEG C, at least A part of thermal cracking heavy oil streams R20P-HO removes the second hydrogenation process R20 as recycle oil R20P-HO-TOR20.

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

Separation liquid stream obtains the thermal cracking heavy oil streams R20P- that the hydrocarbon component mainly by normal boiling point more than 350 DEG C forms HO, at least part thermal cracking heavy oil streams R20P-HO remove the second hydrogenation process as recycle oil R20P-HO-TOR20 R20。

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

The thermal cracking heavy oil streams that the hydrocarbon component that it is mainly 350~530 DEG C by normal boiling point that separation liquid stream, which obtains, forms R20P-HO and the thermal cracking residue that mainly the hydrocarbon component by normal boiling point more than 530 DEG C forms, at least part thermal cracking heavy oil Logistics R20P-HO removes the second hydrogenation process R20 as recycle oil R20P-HO-TOR20.

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

(1) in the first hydrogenation process R10, using floating bed hydrogenation reactor, the hydrogenation catalyst R10C used, with first Hydrogenation process R10 chargings enter the first hydrogenation process R10 together.

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

(1) in the first hydrogenation process R10, using floating bed hydrogenation reactor, the hydrogenation catalyst R10C used, with first Hydrogenation process R10 chargings enter the first hydrogenation process R10 together；

(2) in the second hydrogenation process R20, new catalyst is no longer added, hydrogenation catalyst R20C is from first at this time The hydrogenation catalyst R10C of hydrogenation process R10.

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

(2) in the second hydrogenation process R20, using floating bed hydrogenation reactor, the hydrogenation catalyst R20C used, addition is not It is same as the heat from hydrogenation cracking reaction catalyst R20C-2 of hydrogenation catalyst R10C, hydrogenation catalyst R20C is split comprising heat from hydrogenation at this time Change the catalysts R20C-2 and hydrogenation catalyst R10C from the first hydrogenation process R10.

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

(1) in the first hydrogenation process R10, using floating bed hydrogenation reactor, the hydrogenation catalyst R10C used, with first Hydrogenation process R10 chargings enter the first hydrogenation process R10, the first hydrogenation process R10 and are not present second together The heat from hydrogenation cracking reaction catalyst R20C-2 that hydrogenation process R20 is used；

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

(1) in the first hydrogenation process R10, using floating bed hydrogenation reactor, the hydrogenation catalyst R10C used, with first Hydrogenation process R10 chargings enter the first hydrogenation process R10 together；Second existing for first hydrogenation process R10 The heat from hydrogenation cracking reaction catalyst R20C-2 that hydrogenation process R20 is used is with detaching the second hydrogenation reaction effluent Hydrocarbon ils recycle stream obtained by R20P is into the first hydrogenation process R10's；