CN109705891A

CN109705891A - With the coal-based carbon hydrogen material hydrogenation process of 2 parallel coupled formula reactor assemblies

Info

Publication number: CN109705891A
Application number: CN201711066985.8A
Authority: CN
Inventors: 何巨堂
Original assignee: Individual
Current assignee: Luoyang Ruihua New Energy Technology Development Co ltd
Priority date: 2017-10-25
Filing date: 2017-10-25
Publication date: 2019-05-03
Anticipated expiration: 2037-10-25
Also published as: CN109705891B

Abstract

With the coal-based carbon hydrogen material hydrogenation process of 2 parallel coupled formula reactor assemblies, refined altogether suitable for direct hydrogenation liquefaction of coal or kerosene or the reaction process such as stabilized hydrogenation hydrogen supply dissolvent oil；Parallel coupled formula conversion zone 2 reactors NARE, NBRE, NBRE top product be mixed into NARE after self-production material the top of NARE take off liquid space carry out gas-liquid separation obtain collection cups discharge collection liquid and other products, collection liquid is through circulating pump to NARE, NBRE feeding cycle；For ultra-large direct hydrogenation liquefaction of coal reaction system, it can be achieved that the miniaturization of 2 parallel reactors, shares product Separate System of Water-jet and coal slurry recycle pump, simplifies a coal slurry loop reactor internal structure, save the enormous expenditure of reactor field fabrication；The raw material of 2 reactors is not meanwhile, it is capable to control respective optimal reaction condition；Manifold type hydrogenation reaction system can be combined into deep hydrogenation reaction system with other reactor groups.

Description

With the coal-based carbon hydrogen material hydrogenation process of 2 parallel coupled formula reactor assemblies

Technical field

The present invention relates to the coal-based carbon hydrogen material hydrogenation processes with 2 parallel coupled formula reactor assemblies, are suitable for coal Hydrogen direct liquefaction or kerosene is added to refine altogether or the reaction process such as stabilized hydrogenation hydrogen supply dissolvent oil；Parallel coupled formula conversion zone is with 2 Reactor NARE, NBRE, NBRE top product, which is mixed into NARE after self-production material, takes off liquid space progress gas-liquid at the top of NARE The collection liquid of isolated collection cups discharge and other products, collection liquid is through circulating pump to NARE, NBRE feeding cycle；For super Extensive direct hydrogenation liquefaction of coal reaction system, it can be achieved that 2 parallel reactors miniaturization, share product Separate System of Water-jet And coal slurry recycle pump, simplify a coal slurry loop reactor internal structure, saves the enormous expenditure of reactor field fabrication；2 The raw material of platform reactor is not meanwhile, it is capable to control respective optimal reaction condition；Manifold type hydrogenation reaction system can with it is other anti- Device group is answered to be combined into deep hydrogenation reaction system.

Background technique

Conception of the invention is: with the coal-based carbon hydrogen material hydrogenation process of 2 parallel coupled formula reactor assemblies, being applicable in It is refined altogether or the reaction process such as stabilized hydrogenation hydrogen supply dissolvent oil in direct hydrogenation liquefaction of coal or kerosene；Parallel coupled formula conversion zone is used 2 reactors NARE, NBRE, NBRE top product, which is mixed into NARE after self-production material, carries out gas in the de- liquid space in the top of NARE The collection liquid of liquid isolated collection cups discharge and other products, collection liquid is through circulating pump to NARE, NBRE feeding cycle；For Ultra-large direct hydrogenation liquefaction of coal reaction system, it can be achieved that 2 parallel reactors miniaturization, share product gas-liquid separation system System and coal slurry recycle pump simplify a coal slurry loop reactor internal structure, save the enormous expenditure of reactor field fabrication； The raw material of 2 reactors is not meanwhile, it is capable to control respective optimal reaction condition；Manifold type hydrogenation reaction system can with it is other anti- Device group is answered to be combined into deep hydrogenation reaction system.

The present invention has the advantages that

1. 2 reactor gas-liquid products, taking off liquid space progress gas-liquid separation at the top of 1 reactor can be completed 2 At least partly de- liquid function of reactor product mixing and mixture, obtains collection liquid and other products, can simplify wherein one The internal structure of liquid material loop reactor, two pressure liquid circulation reactors share a circulating pump, simplify operation, reduce Expense；

Therefore, it is suitable for constructing the coupled reactor system of large-scale processing amount, separate unit reactor size can be reduced, solved Certainly transportation problem saves field fabrication expense from without making, significantly reduces capital cost of reactor；

2. coupled reactor system, tandem sequence repeats constitute the second level or multistage hydrogenator system of liquid material process, Second reactor system includes: " feed under a gas-liquid and feed second reactor 2RB under second reactor 2RA, a liquid material ", 2RB reactor can be made to constitute high hydrogen partial pressure, low gas liquid rate operating condition, optimization operation；

Therefore, using existing large-scale direct hydrogenation liquefaction of coal reactor manufacturing technology, the present invention can be economically built into The more optimized reaction system of process condition of the ultra-large direct hydrogenation liquefaction of coal process of function；

3. the raw material coal slurry of 2 reactors is the different such as dilute coal slurries of coal slurry and thick coal slurry of composition respectively, it can control It makes respectively optimal reaction condition or and realizes that the equivalent liquefying conversion rate of myopia, that each road coal slurry of control is separately optimized is preheated Journey, conducive to the target for reducing solvent naphtha total amount with slurry is realized；

4. after increasing direct hydrogenation liquefaction of coal pre-reactor, coupled reactor system will in coupled reactor system upstream It is adapted to kerosene to refine altogether, can take into account the oily thermal cracking time is shorter than the Coal liquefaction time, makes full use of direct hydrogenation liquefaction of coal anti- The hydrogen supply function of answering the relatively excessive hydrogen supply agent component in system rear circulation liquid, avoids anti-at direct hydrogenation liquefaction of coal initial stage The heavy oil thermal of the coal charge pyrolysis number of free radical peak phase, the appearance of heavy-oil hydrogenation thermal cracking initial reaction process of answering process to occur Solution number of free radical peak phase forms synchronous superposition, necessarily causes " oil plant pyrolysis free radical and coal charge pyrolysis free radical like that Contention is unfolded to the reactive hydrogen that hydrogen supply agent provides ", to inhibit the normal liquefaction of direct hydrogenation liquefaction of coal initial reaction process anti- It answers.

Of course, it is possible to which direct hydrogenation liquefaction of coal reaction process RU (intermediate or end reaction process) to be generated to the distillation of oil Oil introduces direct hydrogenation liquefaction of coal reaction process RU secondary cycle and uses, and may be used as to be followed with coal slurry solvent naphtha Ring thermal cracking.For example, can by direct hydrogenation liquefaction of coal reaction process AU generation oil in diesel oil (normal boiling point is between 260 ~330 DEG C of distillate) and/or wax oil (normal boiling point between 330~530 DEG C of distillate) to return to direct hydrogenation liquefaction of coal anti- Process AU is answered to recycle cracking, with voluminous naphtha.

Of course, it is possible to which direct hydrogenation liquefaction of coal reaction process AU (intermediate or end reaction process) to be generated to the distillation of oil Oil, introduces stabilized hydrogenation reaction process MR and produces hydrogen supply dissolvent, and then introducing direct hydrogenation liquefaction of coal reaction process AU circulation makes With.

The present invention when refining process altogether for kerosene, can prepare coal slurry hence into the direct liquid of coal hydrogenation with non-coal derived oils The initial step synchronous reaction for changing reaction process AU also is added to the intermediate reaction step of direct hydrogenation liquefaction of coal reaction process AU It is rapid to carry out the second half association response.

The technical solution similar with the present invention has not been reported.

It is an object of the invention to propose the coal-based carbon hydrogen material hydrogenation reaction mistake with 2 parallel coupled formula reactor assemblies Journey refines process or hydrogen supply dissolvent oil stabilized hydrogenation process suitable for direct hydrogenation liquefaction of coal reaction process or kerosene altogether.

Summary of the invention

The coal-based carbon hydrogen material hydrogenation process of 2 parallel coupled formula reactors of the present invention, it is characterised in that:

In coal-based carbon hydrogen material hydrogenation process RU, there are hydrogen, conventional liquid hydrocarbon and there may be the items of catalyst Under part, coal-based carbon hydrogen material carries out at least part hydrogenation reaction RUR and is converted into reaction product RUP, recycles reaction product RUP；

Coal-based carbon hydrogen material hydrogenation process RU includes at least one conversion zone；

Coal-based carbon hydrogen material hydrogenation process RU, comprising at least one with 2 parallel coupled formula reactor groups at reaction Section, conversion zone segment number are denoted as DRX；

One conversion zone is referred to comprising a coal-based carbon hydrogen material hydrogenation reaction step and the step gas-liquid product The technical process of gas-liquid separation step；

The conversion zone DRN of coal-based carbon hydrogen material hydrogenation process RU is with 2 parallel coupled formula reactors NARE, NBRE The conversion zone of composition, reactor NARE, NBRE are up-flow reactor, and reactor NARE headspace is disposed with overhead-liquid Collection cups form top and take off liquid space between reactor NARE overhead-liquid collection cups and reactor NARE top shell；Reaction 2 reactors processing at least coal-based carbon hydrogen material all the way of section DRN；Reactor NBRE product is mixed into NARE after self-production material, NARE inner top, which takes off liquid space, to carry out gas-liquid separation and completes the collection liquid for obtaining collection cups discharge after at least partly de- liquid and other Product, at least part collection liquid is after the pressurization of liquid material circulating pump to NARE, NBRE feeding cycle；Autoreactor NARE discharge Product NP includes reactor NARE product and reactor NBRE product, it is understood that there may be main in the weight of autoreactor NARE discharge The liquid material product formed by solid liquid material may be contained.

The present invention, in general, using 2 parallel coupleds formula reactor NARE, NBRE, every reactor adds in DRN conversion zone The work at least material of material and/or intermediate product containing the coal liquefaction liquid material of oil-containing coal slurry liquid material and/or hydrocarbonaceous liquid material all the way；Reactor The top NBRE product is mixed into NARE after self-production material, is taken off after liquid space completes at least partly de- liquid and is received in NARE inner top Collect the collection liquid and other products that cup is discharged.

The present invention, in general, completing part in the overhead-liquid collection cups of NARE headspace arrangement in DRN conversion zone De- liquid obtains collection liquid, at least part collection liquid through a shared liquid material circulating pump pressurize backward two reactor NARE, NBRE feeding cycle.

The present invention, the coal-based carbon hydrogen material hydrogenator that coal-based carbon hydrogen material hydrogenation process RU, DRN conversion zone uses are Up-flow reactor, mode of operation can a kind or several in following:

1. suspended-bed reactor；

2. fluidized bed reactor；

3. suspension bed and ebullated bed combined reactor；

4. up flow type expanded bed；

5. upflow fixed bed.

The present invention, the coal-based carbon hydrogen material can a kind or several in following:

1. coal dust carries out direct hydrogenation liquefaction of coal reaction in coal-based carbon hydrogen material hydrogenation process RU；

2. it is direct to carry out coal hydrogenation in coal-based carbon hydrogen material hydrogenation process RU for coal or coal liquefaction intermediate product liquid material Liquefaction reaction；

3. reacting the distilled oil for generating oil based on direct hydrogenation liquefaction of coal, carried out in coal-based carbon hydrogen material hydrogenation process RU Heat from hydrogenation cracking reaction；

4. reacting the distilled oil for generating oil based on direct hydrogenation liquefaction of coal, carried out in coal-based carbon hydrogen material hydrogenation process RU Stabilized hydrogenation reaction, the hydrogen supply dissolvent oil that production direct hydrogenation liquefaction of coal reaction process needs.

The present invention, coal-based carbon hydrogen material are that the distilled oil for generating oil is reacted based on direct hydrogenation liquefaction of coal, in coal-based carbon hydrogen material Hydrogenation process RU carries out stabilized hydrogenation and reacts to obtain the stabilized hydrogenation reaction product rich in hydrogen supply hydrocarbon, and production coal hydrogenation is direct The hydrogen supply dissolvent oil that liquefaction reaction process needs；

Coal-based carbon hydrogen material hydrogenation process RU, the first conversion zone using 2 parallel coupled formula reactor groups at reaction Section, 2 reactors processing at least coal-based carbon hydrogen material all the way of the first conversion zone；

In general, the normal boiling point in stabilized hydrogenation reaction product is higher than 250 DEG C of hydro carbons: the weight content of fractional saturation aromatic hydrocarbons It is 0.35~0.70 greater than 15%, aromatic carbon rate；

Generally, the normal boiling point in stabilized hydrogenation reaction product is higher than 250 DEG C of hydro carbons: the weight content of fractional saturation aromatic hydrocarbons It is 0.40~0.65 greater than 20%, aromatic carbon rate；

Coal-based carbon hydrogen material hydrogenation process RU, operating condition are usual are as follows: the hydrogenation catalyst used is Ni-Mo, Ni-Co Or the hydrogenation catalyst of Ni-W system；Reaction temperature is 300~390 DEG C, and hydrogenation pressure is 10~25MPa, and gas-liquid volume ratio is 300~1000NL/kg.

The present invention, coal-based carbon hydrogen material is coal or coal liquefaction intermediate product liquid material, in coal-based carbon hydrogen material hydrogenation reaction mistake Journey RU carries out direct hydrogenation liquefaction of coal reaction；

In direct hydrogenation liquefaction of coal reaction system RU, there are hydrogen, conventional liquid hydrocarbon and there may be the items of catalyst Under part, coal or coal liquefaction intermediate product liquid material carry out at least part direct hydrogenation liquefaction of coal reaction RUR and are converted into coal adding Hydrogen direct liquefaction reaction product RUP；Recycle reaction product RUP；

Direct hydrogenation liquefaction of coal reaction system RU includes at least one conversion zone, comprising at least one with 2 parallel coupleds Formula reactor group at conversion zone；

One conversion zone refers to the gas-liquid separation comprising a Coal liquefaction step and the step gas-liquid product The technical process of step；

The 1st conversion zone of direct hydrogenation liquefaction of coal reaction system RU processes the material containing coal slurry；

Direct hydrogenation liquefaction of coal reaction system RU it is any with 2 parallel coupled formula reactor groups at conversion zone be denoted as Conversion zone DRN, using 2 parallel coupled formulas reactor NARE, NBRE, 2 reactors processing of conversion zone DRN is at least all the way Coal liquid material and/or coal liquefaction intermediate product liquid material, the processing of every reactor at least all the way the material of oil-containing coal slurry liquid material and/or The material of the liquid material of intermediate product containing coal liquefaction and/or hydrocarbonaceous liquid material, reactor NARE, NBRE are up flow type expanded bed reactor；Instead Answer device NBRE top product enter in reactor NARE mixed with self-production material in NARE after into NARE headspace, The overhead-liquid collection cups of NARE headspace arrangement complete the de- liquid in part and obtain collection liquid and other products, at least part Collection liquid is after coal slurry recycle pump pressurizes to NARE, NBRE feeding cycle；The product NP of autoreactor NARE discharge is comprising anti- Answer the mixed material of device NARE product and reactor NBRE product, it is understood that there may be main in the weight of autoreactor NARE discharge The liquid material product being made of material containing solid-liquid.

The present invention, direct hydrogenation liquefaction of coal reaction system RU, at least two conversion zone comprising liquid phase material serial operation, First conversion zone be with 2 parallel coupled formula reactor groups at conversion zone, the process of direct hydrogenation liquefaction of coal reaction system RU Mode, can a kind or several in following:

1. direct hydrogenation liquefaction of coal reaction system RU, 2 conversion zones comprising liquid phase material serial operation；

First conversion zone is the conversion zone formed with 2 parallel coupleds formula reactor 1ARE, 1BRE, the discharge of the first conversion zone Product 1NTP containing liquid phase；

The second conversion zone is set up, a up flow type expanded bed direct hydrogenation liquefaction of coal reactor 2ARE is used；First reaction The product 1NTP containing liquid phase of section enters the lower part reactor 2ARE as lower charging and flows up through main reaction region, is converted into Reactor 2ARE is discharged in reaction product 2ARE-RP；

2. direct hydrogenation liquefaction of coal reaction system RU, 2 conversion zones comprising liquid phase material serial operation；

First conversion zone is the conversion zone formed with 2 parallel coupleds formula reactor 1ARE, 1BRE, the discharge of the first conversion zone The liquid material 1ALPA being mainly made of material containing solid-liquid on product 1NTP and weight containing liquid phase；

The second conversion zone is set up, a up flow type expanded bed direct hydrogenation liquefaction of coal reactor 2ARE, the first reaction are used Section product liquid material 1ALPA enters the lower part reactor 2ARE as lower charging and flows up through main reaction region, is converted into reaction and produces Reactor 2ARE is discharged in object 2ARE-RP；

Meanwhile first the product 1NTP containing liquid phase of conversion zone enter the top reactor 2ARE as upper feeding, and it is anti- Material in device 2ARE is answered to be mixed；

Reactor 2ARE, is arranged overhead-liquid collection cups, and collection liquid is recycled back into the lower part reaction compartment of reactor 2ARE In；

3. direct hydrogenation liquefaction of coal reaction system RU, 2 conversion zones comprising liquid phase material serial operation；

First conversion zone is the conversion zone formed with 2 parallel coupleds formula reactor 1ARE, 1BRE, the discharge of the first conversion zone The liquid material product 1ALPX being mainly made of material containing solid-liquid on product 1NTP and weight containing liquid phase；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first reaction Product 1NTP of the section containing liquid phase is lower charging, and another reactor is with the first conversion zone liquid material product 1ALPX for lower charging；

In the 2nd conversion zone, reactor 2ARE, 2BRE are up flow type expanded bed reactor；Reactor 2BRE top product into Enter to enter after mixing the headspace of 2ARE, the top of 2ARE headspace arrangement with self-production material in 2ARE in reactor 2ARE The liquid material of portion's liquid collection cups discharge, to 2ARE, 2BRE feeding cycle after coal slurry recycle pump pressurizes；Autoreactor 2ARE discharge Product 2TNP be the mixed material comprising reactor 2ARE product and reactor 2BRE product；

Recycle the second conversion zone reaction product；

4. direct hydrogenation liquefaction of coal reaction system RU, 2 conversion zones comprising liquid phase material serial operation；

First conversion zone is the conversion zone formed with 2 parallel coupleds formula reactor 1ARE, 1BRE, the discharge of the first conversion zone Mainly by the group of material containing solid-liquid on the liquid material product 1ALPX that is mainly made of material containing solid-liquid on liquid phase product 1NTP, weight, weight At liquid material product 1ALPY；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first reaction Liquid phase product 1NTP is upper feeding, with the first conversion zone liquid material product 1ALPX is lower charging section, and another reactor is with liquid material Product 1ALPY is lower charging；

Recycle the second conversion zone reaction product；

5. direct hydrogenation liquefaction of coal reaction system RU, 3 conversion zones comprising liquid phase material serial operation；

First conversion zone is the conversion zone formed with 2 parallel coupleds formula reactor 1ARE, 1BRE, the discharge of the first conversion zone The liquid material product 1ALPX being mainly made of material containing solid-liquid on liquid phase product 1NTP, weight；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first reaction Section liquid phase product 1NTP is lower charging, and another reactor is with the first conversion zone liquid material product 1ALPX for lower charging；Second is anti- The liquid material product 2ALPX that answer section discharge liquid phase product 2NTP, is mainly made of material containing solid-liquid in weight；

Third conversion zone, using 2 parallel coupleds formula reactor 3ARE, 3BRE, wherein a reactor is with the second reaction Section liquid phase product 2NTP is lower charging, and another reactor is with the second conversion zone liquid material product 2ALPB for lower charging；

Recycle third conversion zone reaction product；

6. direct hydrogenation liquefaction of coal reaction system RU, 3 conversion zones comprising liquid phase material serial operation；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first reaction Section liquid phase product 1NTP is lower charging, and another reactor is with the first conversion zone liquid material product 1ALPX for lower charging；Second is anti- Answer section discharge liquid phase product 2NTP, the liquid material product 2ALPX being mainly made of material containing solid-liquid in weight, in weight mainly by containing The liquid material product 2ALPY of solid-liquid material composition；

Third conversion zone, using 2 parallel coupleds formula reactor 3ARE, 3BRE, wherein a reactor is with the second reaction Liquid phase product 2NTP is upper feeding, with the second conversion zone liquid material product 2ALPX is lower charging section, and another reactor is with second Conversion zone liquid material product 2ALPY is lower charging；

Recycle third conversion zone reaction product；

7. direct hydrogenation liquefaction of coal reaction system RU, 3 conversion zones comprising liquid phase material serial operation；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first reaction Liquid phase product 1NTP is upper feeding, with the first conversion zone liquid material product 1ALPX is lower charging section, and another reactor is with first Conversion zone liquid material product 1ALPY is lower charging；Mainly by material containing solid-liquid on second conversion zone discharge liquid phase product 2NTP, weight The liquid material product 2ALPX of composition；

Third conversion zone, using 2 parallel coupleds formula reactor 3ARE, 3BRE, wherein a reactor is with the second reaction Section liquid phase product 2NTP is lower charging, and another reactor is with the second conversion zone liquid material product 2ALPX for lower charging；

Recycle third conversion zone reaction product；

8. direct hydrogenation liquefaction of coal reaction system RU, 3 conversion zones comprising liquid phase material serial operation；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first reaction Liquid phase product 1NTP is upper feeding, with the first conversion zone liquid material product 1ALPX is lower charging section, and another reactor is with first Conversion zone liquid material product 1ALPY is lower charging；Mainly by material containing solid-liquid on second conversion zone discharge liquid phase product 2NTP, weight The liquid material product 2ALPY being mainly made of material containing solid-liquid on the liquid material product 2ALPX of composition, weight；

Third conversion zone, using 2 parallel coupleds formula reactor 3ARE, 3BRE, wherein a reactor is with the second reaction Liquid phase product 2NTP is upper feeding, with the first conversion zone liquid material product 2ALPA is lower charging section, and another reactor is with second Conversion zone liquid material product 2ALPY is lower charging；

Recycle third conversion zone reaction product；

9. direct hydrogenation liquefaction of coal reaction system RU, comprising 1 pre-hydrotreating reaction section 0PRE, one with 2 parallel coupleds Formula reactor group at the first conversion zone and subsequent reactions section that may be present；

In pre-hydrotreating reaction section 0PRE, it is anti-that coal slurry material F1 progress coal liquefaction pre-hydrotreating reaction is converted into coal liquefaction pre-add hydrogen Product 0PRE-RP, at least part pre-hydrotreating reaction product 0PRE-RP is answered to enter the first conversion zone as charging under reactor In reactor；

10. direct hydrogenation liquefaction of coal reaction system RU, comprising 1 pre-hydrotreating reaction section 0PRE, one with 2 parallel coupleds Formula reactor group at the first conversion zone and subsequent reactions section that may be present；

In pre-hydrotreating reaction section 0PRE, it is anti-that coal slurry material F1 progress coal liquefaction pre-hydrotreating reaction is converted into coal liquefaction pre-add hydrogen Product 0PRE-RP is answered, the liquid material product being mainly made of material containing solid-liquid in weight is obtained based on pre-hydrotreating reaction product 0PRE-RP 0PLPX, at least part liquid material product 0PLPX enter in the reactor of the first conversion zone as charging under reactor.

The present invention, in general, in direct hydrogenation liquefaction of coal reaction system RU, it is any with 2 parallel coupled formula reactor groups at Conversion zone be denoted as conversion zone DRN, using 2 parallel coupleds formula reactor NARE, NBRE, there are autoreactor NARE inner tops The liquid material product being mainly made of material containing solid-liquid in the weight of liquid collection cups discharge.

The present invention, direct hydrogenation liquefaction of coal reaction system RU can process non-coal base weight while processing coal slurry raw material Oil.

The present invention uses 2 parallel coupled formula reactors in the conversion zone DRN of direct hydrogenation liquefaction of coal reaction system RU NARE, NBRE, a reactor processing oil coal slurry liquid material and/or coal liquefaction intermediate product liquid material, another reactor can add The hydro-conversion thing liquid material of the non-coal base weight oil of work or non-coal base weight oil.

The present invention, direct hydrogenation liquefaction of coal reaction system RU can process non-coal base weight while processing coal slurry raw material Oil；

In direct hydrogenation liquefaction of coal reaction system RU, it is direct that the hydrogenation reaction residence time of non-coal base weight oil is shorter than coal hydrogenation The liquefaction reaction residence time.

The present invention, in general, in the conversion zone DRN of direct hydrogenation liquefaction of coal reaction system RU, it is anti-using 2 parallel coupled formulas Device NARE, NBRE are answered, a reactor processes the coal liquid material and/or coal liquefaction intermediate product liquid material that solid concentration is CA, separately The coal liquid material and/or coal liquefaction intermediate product liquid material that one reactor processing solid concentration is CB, solid concentration CA and CB phase It is same or different.

The present invention, in general, in direct hydrogenation liquefaction of coal reaction system RU, the conversion ratio of the moisture-and-ash-free basis component of feed coal It is 70~98%.

The present invention can process non-coal base while processing coal slurry raw material in direct hydrogenation liquefaction of coal reaction system RU Heavy oil, the heat from hydrogenation cracking reaction conversion ratio of non-coal base weight oil are 40~90%.

The present invention, in general, in the conversion zone DRN of direct hydrogenation liquefaction of coal reaction system RU, it is anti-using 2 parallel coupled formulas Device NARE, NBRE are answered, a reactor processes the coal liquid material and/or coal liquefaction intermediate product liquid material that solid concentration is CA, separately The coal liquid material and/or coal liquefaction intermediate product liquid material that one reactor processing solid concentration is CB, solid concentration are CA and CB Absolute difference be 5~35%.

The present invention, in general, in direct hydrogenation liquefaction of coal reaction system RU, the dilute coal slurry of simultaneous processing and thick coal slurry, dilute coal slurry Coal concentration C A be 35~50%, the coal concentration C B of thick coal slurry is 50~70%.

The present invention, in general, in direct hydrogenation liquefaction of coal reaction system RU, simultaneous processing dilute coal slurry F1 and thick coal slurry F2 is thick The ratio of the weight flow F1-W of the weight flow F2-W of coal slurry F2 and dilute coal slurry F1 are slurry slurry than K100, K100=(F2-W)/ (F1-W), K100 is 0.01~1.0.

The present invention, in general, being calculated in direct hydrogenation liquefaction of coal reaction system RU with all feeding, the weight of hydrogen supply dissolvent DS The weight ratio of amount and coal dust is 0.5~2.0.

The present invention, in general, the direct hydrogenation liquefaction of coal of coal dust experience reacted in direct hydrogenation liquefaction of coal reaction system RU The operating condition of journey are as follows: reaction temperature be 400~485 DEG C, reactor pressure be 6~30MPa, vapor phase hydrogen volumetric concentration 50~ 95%, gas-liquid volume ratio is 300~2500Nm³/ t, direct hydrogenation liquefaction of coal catalyst loading be dry pulverized coal weight 0.1~ 3 mass %, co-catalyst additive amount are that sulphur in co-catalyst/catalyst activity metal molar ratio is 1.0~2.0, and coal slurry is solid Bulk concentration is 40~60 mass %, and reaction time is 0.5~4 hour.

The present invention, in direct hydrogenation liquefaction of coal reaction system RU, the direct hydrogenation liquefaction of coal catalyst used can be one Kind composite hydrogenation catalyst, includes high-activity component and low activity component；The high-activity component metal and low activity component The weight ratio of metal is 1: 10 to 10: 1；The high-activity component is or mixtures thereof the water soluble salt compound of molybdenum；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%, the direct liquid of coal hydrogenation Change catalyst water content and is lower than 2wt%；The powdered granule that the particle diameter of direct hydrogenation liquefaction of coal catalyst is 1~100 μm.

The present invention, in direct hydrogenation liquefaction of coal reaction system RU, the direct hydrogenation liquefaction of coal catalyst used can be and receive Rice ultra-fine grain aqua oxidation iron catalyst and/or iron oxide and/or pyrite and/or bloodstone and/or molybdenum oxide and/or molybdenum sulfide And/or ammonium molybdate and/or nickel sulfide.

The present invention, in general, in direct hydrogenation liquefaction of coal reaction system RU, it is at least former all the way in the raw material of whole hydrocarbon containing liquids Material contains hydrogen supply agent, and the hydrogen supply agent is mainly made of the hydro carbons that normal boiling point is 250~530 DEG C, fractional saturation in hydrogen supply agent It is 0.35~0.70 that the weight content of aromatic hydrocarbons, which is greater than 15%, aromatic carbon rate,.

The present invention, it is generally, at least former all the way in direct hydrogenation liquefaction of coal reaction system RU, the raw material of whole hydrocarbon containing liquids Material contains hydrogen supply agent, and the hydrogen supply agent is mainly made of the hydro carbons that normal boiling point is 250~530 DEG C, fractional saturation in hydrogen supply agent It is 0.45~0.60 that the weight content of aromatic hydrocarbons, which is greater than 25%, aromatic carbon rate,.

The present invention, in general, at least part for including in raw material coal slurry is with slurry in direct hydrogenation liquefaction of coal reaction system RU Solvent naphtha, a kind or several in following materials:

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

2. oil product logistics obtained by high temperature coal-tar or its distillate or its hot procedure；Hot procedure is selected from coking Journey or catalytic cracking process or catalytic pyrolysis process or hydrogenation process；

3. oil product obtained by the distillate oil of direct hydrogenation liquefaction of coal process product or its hot procedure；Hot procedure is selected from Coking or catalytic cracking process or catalytic pyrolysis process or hydrogenation process；

4. oil product obtained by shale oil or its distillate or its hot procedure；Hot procedure is selected from coking or catalysis Cracking process or catalytic pyrolysis process or hydrogenation process；

5. oil product obtained by ethylene cracking tar or its hot procedure；Hot procedure is selected from coking or catalytic cracking Process or catalytic pyrolysis process or hydrogenation process；

6. oil product obtained by petroleum based heavy fuel oils hot procedure；Hot procedure be selected from coking or catalytic cracking process or Catalytic pyrolysis process or hydrogenation process；

7. oil product hot procedure obtained by tar sand base weight oil or its hot procedure is selected from coking or catalytic cracking Process or catalytic pyrolysis process or hydrogenation process；

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

Detailed description of the invention

Below in conjunction with attached drawing the present invention is described in detail, attached drawing is to draw to describe the present invention, but it cannot be limited Fixed application range of the invention.

Fig. 1 is 2 typical direct hydrogenation liquefaction of coal process floating bed hydrogenation reactor assemblies in parallel, belongs to setting The up flow type floating bed hydrogenation reactor assembly for forcing liquid product recycle system, can be used for ultra-large direct hydrogenation liquefaction of coal Reaction system.

As shown in Figure 1, in reactor 1ARE system, the mixture 1AF1 of the coal and hydrogen that are conveyed through pipeline 151, Be mixed into mixture 1ATF with the circulation liquid phase 1ARL1 (gas phase may be contained) conveyed through pipeline 159, through pipeline 152 convey into Enter the bottom of reactor 1ARE, the feed distributor 1ATFS of usually reacted device bottom feed inlet top installation (does not show in figure Carrying out predistribution out) is evenly distributed to charging as far as possible on the entire horizontal feed section of distribution plate 1AS；1ATFS charging point Orchestration can be arbitrary suitable construction, such as aperture or the distribution pipe cracked, aperture or the distribution cap cracked；Distribution plate 1AS, can To be arbitrary suitable construction, usually using multiple allocation unit 1ASK, under each allocation unit 1ASK setting distribution plate 1AS Portion's feed pipe (not shown) and the top distribution plate 1AS bubble-cap (not shown), air-liquid from the lower part distribution plate 1AS, Solid particle mixed phase material enters the top distribution plate 1AS bubble-cap after distribution plate 1AS lower part feed pipe passes through distribution plate 1AS In, then by distribution plate 1AS top bubble-cap and the lower part distribution plate 1AS feed pipe the upper section pipeline section across distribution plate 1AS it Between gap spray to distributor upper surface, then disperse, collide, mixing, turn to after flow up, in reactor, 1ARE master is anti- Progress direct hydrogenation liquefaction of coal during the uplink in space is answered to react the top product 1ARP for being converted into reactor 1ARE.

As shown in Figure 1, top product 1ARP passes through between reactor 1ARE upper inside wall and liquid collection cups 1AV outer wall Behind annular gap, liquid is taken off into the part being made of reactor head wall and liquid collection cups 1AV on the top reactor 1ARE Space.As shown in Figure 1, the liquid in top product preferentially settles into collection cups 1AV under the effect of gravity, and in collection cups Gradually deviate from bubble during decline inside 1AV, the circulation liquid phase 1ARL for deviating from bubble enters leading for the bottom collection cups 1AV It flows downward in pipe 1AVP and reactor is discharged, enter in circulation force (forcing) pump 1APUMP through piping 158, the circulation fluid after pressurization Phase 1ARL1 is conveyed through piping 159, is then mixed into mixture 1ATF with mixture 1AF1, is delivered into instead through pipeline 152 Answer cyclic process in device 1ARE.

As shown in Figure 1, top product 1ARP, which is separated into, recycles liquid phase 1ARL and net product 1ARTP, net product 1ARTP is Gas, liquid, solid body particle mixed phase material, under the action of reactor 1ARE top gas phase pressure, by being inserted into liquid collection cups 1AV Reactor 1ARE is discharged in 157 uplink of product diversion pipe under liquid level, into Downstream processing process.

As shown in Figure 1, the mode of operation of reactor 1BRE is same as the mode of operation of reactor 1ARE.In reactor 1BRE system In system, the mixture 1BF1 of the coal and hydrogen that are conveyed through pipeline 161, with the circulation liquid phase 1BRL1 conveyed through pipeline 169 (may contain gas phase) is mixed into mixture 1BTF, and the bottom of reactor 1BRE is delivered into through pipeline 162, usual reacted device The feed distributor 1BTFS (not shown) of bottom feed inlet top installation, which carries out predistribution, is evenly distributed charging as far as possible Onto the entire horizontal feed section of distribution plate 1BS；Gas, liquid, solid body particle mixed phase material from the lower part distribution plate 1BS, warp It is flowed up after crossing distribution plate 1BS, it is anti-that direct hydrogenation liquefaction of coal is carried out during the uplink in reactor 1BRE main reaction space The top product 1BRP of reactor 1BRE should be converted into.

As shown in Figure 1, top product 1BRP passes through between reactor 1BRE upper inside wall and liquid collection cups 1BV outer wall Behind annular gap, liquid is taken off into the part being made of reactor head wall and liquid collection cups 1BV on the top reactor 1BRE Space.As shown in Figure 1, the liquid in top product preferentially settles into collection cups 1BV under the effect of gravity, and in collection cups Gradually deviate from bubble during decline inside 1BV, the circulation liquid phase 1BRL for deviating from bubble enters leading for the bottom collection cups 1BV It flows downward in pipe 1BVP and reactor is discharged, enter in circulation force (forcing) pump 1BPUMP through piping 168, the circulation fluid after pressurization Phase 1BRL1 is conveyed through piping 169, is then mixed into mixture 1BTF with mixture 1BF1, is delivered into instead through pipeline 162 Answer cyclic process in device 1BRE.

As shown in Figure 1, top product 1BRP, which is separated into, recycles liquid phase 1BRL and net product 1BRTP, net product 1BRTP is Gas, liquid, solid body particle mixed phase material, under the action of reactor 1BRE top gas phase pressure, by being inserted into liquid collection cups 1BV Reactor 1BRE is discharged in 167 uplink of product diversion pipe under liquid level, into Downstream processing process.

As shown in Figure 1, net product 1ARTP, the net product 1BRTP in the top reactor 1BRE at the top of reactor 1ARE, are merged into The net product 1TNP of general top, is delivered to downstream process through pipeline 170.

Fig. 2 be the 1st kind of typical process of the invention schematic diagram and basic model process of the invention.

As shown in Fig. 2, in reactor 1ARE system, the mixture 1AF1 of the coal and hydrogen that are conveyed through pipeline 151, (gas phase may be contained, the liquid containing liquid product and 1BRE from 1ARE with the circulation liquid phase 1ARL1 conveyed through pipeline 159 Phase product) be mixed into mixture 1ATF, the bottom of reactor 1ARE is delivered into through pipeline 152, usual reacted device bottom into The feed distributor 1ATFS (not shown) of material mouth top installation, which carries out predistribution, makes charging be evenly distributed to distribution as far as possible On the entire horizontal feed section of disk 1AS；Gas, liquid, solid body particle mixed phase material from the lower part distribution plate 1AS, by distribution It is flowed up after disk 1AS, direct hydrogenation liquefaction of coal reaction conversion is carried out during the uplink in reactor 1ARE main reaction space For the top product 1ARP of reactor 1ARE.

As shown in Fig. 2, top product 1ARP passes through between reactor 1ARE upper inside wall and liquid collection cups 1AV outer wall Behind annular gap, liquid is taken off into the part being made of reactor head wall and liquid collection cups 1AV on the top reactor 1ARE Space, with old process shown in Fig. 1 the difference is that, carry out portion after being mixed with the product 1BRTP for carrying out autoreactor 1BRE Divide de- liquid.As shown in Fig. 2, the liquid in the mix products of top preferentially settles into collection cups 1AV under the effect of gravity, and Gradually deviate from bubble during decline inside collection cups 1AV, the circulation liquid phase 1ARL for deviating from bubble enters the bottom collection cups 1AV It flows downward in the conduit 1AVP in portion and reactor is discharged, enter in circulation force (forcing) pump 1APUMP through piping 158, after pressurization First circulation liquid phase 1ARL1 is conveyed through piping 159, is then mixed into mixture 1ATF with mixture 1AF1, defeated through pipeline 152 It is fed into cyclic process in reactor 1ARE.

As shown in Fig. 2, top product 1ARP, which is separated into, recycles liquid phase 1ARL and net product 1ARTP, net product 1ARTP is Gas, liquid, solid body particle mixed phase material, under the action of reactor 1ARE top gas phase pressure, by being inserted into liquid collection cups 1AV Reactor 1ARE is discharged in 157 uplink of product diversion pipe under liquid level, and the joint by pipeline 170 as association response section produces only Object 1TNP enters in Downstream processing process.

As shown in Fig. 2, in reactor 1BRE system, the mixture 1BF1 of the coal and hydrogen that are conveyed through pipeline 161, (gas phase may be contained, the liquid containing liquid product and 1BRE from 1ARE with the circulation liquid phase 1BRL1 conveyed through pipeline 169 Phase product) be mixed into mixture 1BTF, the bottom of reactor 1BRE is delivered into through pipeline 162, usual reacted device bottom into The feed distributor 1BTFS (not shown) of material mouth top installation, which carries out predistribution, makes charging be evenly distributed to distribution as far as possible On the entire horizontal feed section of disk 1BS；Gas, liquid, solid body particle mixed phase material from the lower part distribution plate 1BS, by distribution Disk 1BS is flowed up, and direct hydrogenation liquefaction of coal reaction is carried out during the uplink in reactor 1BRE main reaction space and is converted into The top product 1BRTP of reactor 1BRE.

As shown in Fig. 2, the difference is that, top product 1BRTP enters through pipeline 167 with old process shown in Fig. 1 The part being made of reactor head wall and liquid collection cups 1AV on the top reactor 1ARE takes off liquid space, and carrys out autoreaction Part, which is carried out, after product 1ARP mixing in device 1ARE takes off liquid.As shown in Fig. 2, the liquid in the mix products of top is made in gravity It is preferentially settled into collection cups 1AV with lower, and gradually deviates from bubble during decline inside collection cups 1AY, deviate from gas The circulation liquid phase 1ARL of bubble, which enters in the conduit 1AVP of the bottom collection cups 1AV to flow downward, is discharged reactor, through piping 158 into Enter to recycle the second circulation liquid phase 1BRL1 in force (forcing) pump 1APUMP, after pressurization to convey through piping 169, then with mixture 1BF1 is mixed into mixture 1BTF, delivers into cyclic process in reactor 1BRE through pipeline 162.

The schematic diagram of 1st kind of typical process of the invention shown in Fig. 2 is that 2 typical direct hydrogenation liquefaction of coal processes are used Floating bed hydrogenation reactor group at parallel coupled reaction system, reactor 1ARE, reactor 1BRE product in reactor (top) mixing inside 1ARE, shares liquid collecting cup 1AV at the top of reactor 1ARE, 2 reactors can be completed using 1 circulating pump Liquid product circulation, rather than two reactors as shown in Figure 1 respectively use 1 circulating pump that could complete respective liquid phase produces Object circulation；And the internal structure of reactor 1BRE in Fig. 2, the internal structure than reactor 1BRE in Fig. 1 is simple, eliminates collection Liquid cup 1BV and catheter 1BVP；Circulation liquid material in 2 reactors is the liquid product of liquid product and 1BRE from 1ARE Mixture, in this way, 2 reactors constitute manifold type direct hydrogenation liquefaction of coal reaction system.

The first typical process of the invention as shown in Figure 2, for direct hydrogenation liquefaction of coal device, the advantage is that:

1. compared with 2 sets of independent reactor assemblies shown in FIG. 1, process of the present invention shown in Fig. 2 saves 1 set of liquid phase Product recycle system compares (including liquid collecting cup, catheter, circulating pump), therefore economical；

2. construct the reactor assembly of large-scale processing amount, followed with a ultra-large type reactor using 1 set of liquid product Loop system compares (including liquid collecting cup, catheter, circulating pump), completes the coupling reaction system of same task, and 1 set of liquid is also used only Phase product recycle system compares (including liquid collecting cup, catheter, circulating pump)；Meanwhile separate unit reactor 1ARE, 1BRE can be reduced Diameter and weight, make it suitable for transport and ask to solving reactor manufactory reactant transport device to the transport of coal liquefaction factory Topic can save compared with the ultra-large type reactor (rather than manufacturing in reactor professional factory) of field fabrication because scene is made Make and increased expensive expense, significantly reduce capital cost of reactor, be also more conducive to guarantee reactor apparatus quality, can also shorten anti- The device manufacturing cycle is answered, therefore economical.

Fig. 3 is the schematic diagram of the 2nd kind of typical process of the invention, the base of the 1st kind of typical process of the invention shown in Fig. 2 On plinth, the 2nd conversion zone of suspended-bed reactor composition is increased, carries out the reaction of depth direct hydrogenation liquefaction of coal, first is anti- It answers section to combine net product 1TNP, all enters second stage reactor 2ARE as lower charging.

As shown in figure 3, the first conversion zone conveyed through pipeline 251 combines net product 1TNP in reactor 2ARE system, Mixing is mixed into the circulation liquid phase 2ARL1 (gas phase may be contained, contain the liquid product from 2ARE) conveyed through pipeline 259 Expect 2ATF, the bottom of reactor 2ARE is delivered into through pipeline 252, the charging of usually reacted device bottom feed inlet top installation Distributor 2ATFS (not shown) carry out predistribution make charging be evenly distributed to as far as possible distribution plate 2AS it is entire it is horizontal into Expect on section；Gas, liquid, solid body particle mixed phase material from the lower part distribution plate 2AS, flows up after distribution plate 2AS, The top that direct hydrogenation liquefaction of coal reaction is converted into reactor 2ARE is carried out during the uplink in reactor 2ARE main reaction space Product 2ARP.

As shown in figure 3, top product 2ARP enters being collected by reactor head wall and liquid for the top reactor 2ARE The part of cup 2AV composition carries out partially taking off liquid after taking off liquid space.As shown in figure 3, the liquid in top product is under the effect of gravity It preferentially settles into collection cups 2AV, and gradually deviates from bubble during decline inside collection cups 2AV, deviate from bubble Circulation liquid phase 2ARL, which enters in the conduit 2AVP of the bottom collection cups 2AY to flow downward, is discharged reactor, enters through piping 258 and follows In ring force (forcing) pump 2APUMP, the circulation liquid phase 2ARL1 after pressurization is conveyed through piping 259, is then mixed into mixture 2AF1 Mixture 2ATF delivers into cyclic process in reactor 2ARE through pipeline 252.

Fig. 4 is the schematic diagram of the 3rd kind of typical process of the invention, on the basis of the 1st kind of typical process of the invention, is increased The 2nd conversion zone for having added a suspended-bed reactor to form carries out the reaction of depth direct hydrogenation liquefaction of coal, the discharge of the first conversion zone 2 products: as the liquid product of charging 1ALPA under second stage reactor 2ARE and as second stage reactor 2ARE upper feeding Top gas-liquid product 1TNP.

As shown in figure 4, different from process shown in Fig. 3, the collection liquid for carrying out autoreactor 1ARE enters through piping 158 to be recycled In force (forcing) pump 1APUMP, recycles and increase liquid product 1ALPA in force (forcing) pump 1APUMP outputting material, liquid product 1ALPA warp Piping 163 delivers into 2ARE.

As shown in figure 4, in reactor 2ARE system, liquid product 1ALPA, the hydrogen 2AH1 conveyed through pipeline 250, with The circulation liquid phase 2ARL1 (may contain gas phase) conveyed through pipeline 259 is mixed into mixture 2ATF, delivers into through pipeline 252 The bottom of reactor 2ARE, the feed distributor 2ATFS (not shown) of usually reacted device bottom feed inlet top installation Carrying out predistribution is evenly distributed to charging as far as possible on the entire horizontal feed section of distribution plate 2AS；Under distribution plate 2AS The gas, liquid, solid body particle mixed phase material in portion, flows up after distribution plate 2AS, in the upper of reactor 2ARE main reaction space The top product 2ARP that direct hydrogenation liquefaction of coal reaction is converted into reactor 2ARE is carried out during row.

As shown in figure 4, top product 2ARP passes through between reactor 2ARE upper inside wall and liquid collection cups 2AV outer wall Behind annular gap, liquid is taken off into the part being made of reactor head wall and liquid collection cups 2AV on the top reactor 2ARE Space carries out part and takes off liquid after mixing with the product 1TNP for carrying out autoreactor 1ARE.As shown in figure 4, in the mix products of top Liquid preferentially settles into collection cups 2AV under the effect of gravity, and gradually deviates from during decline inside collection cups 2AV Bubble, the circulation liquid phase 2ARL for deviating from bubble, which enters in the conduit 2AYP of the bottom collection cups 2AV to flow downward, is discharged reactor, passes through Piping 258 enters in circulation force (forcing) pump 2APUMP, and the circulation liquid phase 2ARL1 after pressurization is conveyed through piping 259, then with it is mixed It closes object 2AH1 and is mixed into mixture 2ATF, deliver into cyclic process in reactor 2ARE through pipeline 252.

As shown in figure 4, reactor 2ARE top material is separated into circulation liquid phase 2ARL and net product 2ARTP, net product 2ARTP is gas, liquid, solid body particle mixed phase material, under the action of reactor 2ARE top gas phase pressure, by being inserted into liquid Reactor 2ARE is discharged in 257 uplink of product diversion pipe under collection cups 2AV liquid level, into Downstream processing process.

3rd kind of typical process of the invention as shown in Figure 4, compared with the 2nd kind of typical process of the invention as shown in Figure 3, For direct hydrogenation liquefaction of coal device, it is characterized in that: one section of gas phase reaction product, the overwhelming majority are directly entered with material 1TNP Reactor 2ARE is discharged at the top of reactor 2ARE, does not pass through the main body reaction compartment of reactor 2ARE；The main body of reactor 2ARE Reaction compartment is using new hydrogen so hydrogen partial pressure is high；Be directly entered the liquid phase at the top of reactor 2ARE with material 1TNP, part or Enter in the main body reaction compartment of 2ARE mostly as the collection liquid of liquid collecting cup 2AV, rest part is expelled directly out reactor At the top of 2ARE.

Fig. 5 is the schematic diagram of the 4th kind of typical process of the invention, on the basis of the 1st kind of typical process of the invention, weight The second conversion zone is formed using parallel coupled reaction system again, constitutes overall 2 sections of serial flows, the reactor of the second conversion zone 2ARE receives the gas-liquid mixed phase product 1TNP from the first conversion zone, and the reactor 2BRE of the second conversion zone, which is received, comes from first The product liquid 1ALPB of conversion zone.

As shown in figure 5, the difference is that, carrying out the collection liquid of autoreactor 1ARE through piping with process shown in Fig. 2 158 enter in circulation force (forcing) pump 1APUMP, and the first circulation liquid phase 1ARL1 after pressurization is conveyed through piping 159 returns to 1ARE, Second circulation liquid phase 1BRL1 after pressurization is conveyed through piping 169 returns to 1BRE, the liquid product after in addition increasing pressurization 1ALPB delivers into 2BRE through piping 166.

As shown in figure 5, the first conversion zone conveyed through pipeline 251 combines net product 1TNP in reactor 2ARE system, Mixing is mixed into the circulation liquid phase 2ARL1 (gas phase may be contained, contain the liquid product from 2ARE) conveyed through pipeline 259 Expect 2ATF, the bottom of reactor 2ARE is delivered into through pipeline 252, the charging of usually reacted device bottom feed inlet top installation Distributor 2ATFS (not shown) carry out predistribution make charging be evenly distributed to as far as possible distribution plate 2AS it is entire it is horizontal into Expect on section；Gas, liquid, solid body particle mixed phase material from the lower part distribution plate 2AS, flows up after distribution plate 2AS, The top that direct hydrogenation liquefaction of coal reaction is converted into reactor 2ARE is carried out during the uplink in reactor 2ARE main reaction space Product 2ARP.

As shown in figure 5, the top product 2BRTP for carrying out autoreactor 2BRE enter the top reactor 2ARE by reactor top The part of portion's wall and liquid collection cups 2AV composition takes off liquid space, mixes with the product 2ARP come in autoreactor 2ARE laggard Row part takes off liquid.As shown in figure 5, the liquid in the mix products of top preferentially settles into collection cups 2AV under the effect of gravity, And gradually deviating from bubble during decline inside collection cups 2AV, the circulation liquid phase 2ARL for deviating from bubble enters collection cups 2AV It flows downward in the conduit 2AVP of bottom and reactor is discharged, enter in circulation force (forcing) pump 2APUMP through piping 258, after pressurization First circulation liquid phase 2ARL1 is conveyed through piping 259, is then mixed into mixture 2ATF with mixture 2AF1, through pipeline 252 Deliver into cyclic process in reactor 2ARE.

As shown in figure 5, in reactor 2BRE system, the hydrogen object 2BH1 conveyed through pipeline 260 is and defeated through pipeline 269 Circulation coal 2BRL1 (gas phase may be contained, the liquid product containing liquid product and 2BRE from the 2ARE) mixing sent For mixture 2BTF, the bottom of reactor 2BRE is delivered into through pipeline 262, usually reacted device bottom feed inlet top installation Feed distributor 2BTFS (not shown) carry out predistribution make charging be evenly distributed to the entire of distribution plate 2BS as far as possible On horizontal feed section；Gas, liquid, solid body particle mixed phase material from the lower part distribution plate 1BS, after distribution plate 2BS upwards Flowing carries out direct hydrogenation liquefaction of coal reaction during the uplink in reactor 2BRE main reaction space and is converted into reactor The top product 2BRP of 2BRE.

As shown in figure 5, top product 2BRTP is through the entrance of pipeline 267 top reactor 2ARE by reactor head wall Liquid space is taken off with the part of liquid collection cups 2AV composition, carries out part after mixing with the product 2ARP come in autoreactor 2ARE De- liquid.As shown in figure 5, the liquid in the mix products of top preferentially settles into collection cups 2AV under the effect of gravity, and receiving Gradually deviate from bubble during decline inside collection cup 2AY, the circulation liquid phase 2ARL for deviating from bubble enters the bottom collection cups 2AV Conduit 2AVP in flow downward reactor be discharged, enter in circulation force (forcing) pump 2APUMP through piping 258, the after pressurization Two circulation liquid phase 2BRL1 are conveyed through piping 269, then deliver into cyclic process in reactor 2BRE through pipeline 262.

Fig. 6 is the schematic diagram of the 5th kind of typical process of the invention, the base of the 1st kind of typical process of the invention shown in Fig. 2 It on plinth, reuses parallel coupled reaction system and forms the second conversion zone, constitute overall 2 sections of serial flows, the second conversion zone Reactor 2ARE receives gas-liquid mixed phase product 1TNP, liquid product 1ALPA from the first conversion zone, the reaction of the second conversion zone Device 2BRE receives the product liquid 1ALPB from the first conversion zone in received reaction starting point.

As shown in fig. 6, the difference is that, carrying out autoreactor 1ARE with the 1st kind of typical process of the invention shown in Fig. 2 Collection liquid through piping 158 enter circulation force (forcing) pump 1APUMP in, the first circulation liquid phase 1ARL1 after pressurization is through piping 159 conveyings return to 1ARE, and the second circulation liquid phase 1BRL1 after pressurization is conveyed through piping 169 and returned to 1BRE, in addition increase The first liquid product 1ALPA after pressurization is delivered into 2ARE through piping 163, the second liquid phase product after increasing pressurization 1ALPB is delivered into 2BRE through piping 166.

As shown in fig. 6, in reactor 2ARE system, the first liquid product 1ALPA for being conveyed through pipeline 163, through pipeline The hydrogen 2AH1 of 250 conveyings, (may contain gas phase, containing from 2ARE's with the circulation liquid phase 2ARL1 conveyed through pipeline 259 Liquid product) it is mixed into mixture 2ATF, the bottom of reactor 2ARE is delivered into through pipeline 252, usual reacted device bottom The feed distributor 2ATFS (not shown) of feed inlet top installation, which carries out predistribution, is evenly distributed to charging as far as possible point On entire horizontal feed section with disk 2AS；Gas, liquid, solid body particle mixed phase material from the lower part distribution plate 2AS, through excessive With being flowed up after disk 2AS, direct hydrogenation liquefaction of coal reaction is carried out during the uplink in reactor 2ARE main reaction space and is turned Turn to the top product 2ARP of reactor 2ARE.

The top product 2BRTP for carrying out autoreactor 2BRE that is conveyed as shown in Figure 6 through pipeline 267, it is conveyed through pipeline 170 First conversion zone combines net product 1TNP, into the top reactor 2ARE by reactor head wall and liquid collection cups 2AV The part of composition takes off liquid space, and part is carried out after mixing with the product 2ARP come in autoreactor 2ARE and takes off liquid.As shown in fig. 6, Liquid in the mix products of top preferentially settles into collection cups 2AV under the effect of gravity, and inside the collection cups 2AV under Gradually deviate from bubble during drop, the circulation liquid phase 2ARL for deviating from bubble enters in the conduit 2AVP of the bottom collection cups 2AV downwards Flowing discharge reactor, enters in circulation force (forcing) pump 2APUMP through piping 258, the first circulation liquid phase 2ARL1 warp after pressurization Piping 259 conveys, and mixture 2ATF is then mixed into 2AH1, delivers into circulation in reactor 2ARE through pipeline 252 and adds Work.

As shown in fig. 6, in reactor 2BRE system, the liquid product for carrying out autoreactor 1ARE that is conveyed through pipeline 166 1ALPB, the hydrogen 2BH1 conveyed through pipeline 260 (may contain gas phase, contain with the circulation liquid phase 2BRL1 conveyed through pipeline 269 Have the liquid product of liquid product and 2BRE from 2ARE) it is mixed into mixture 2BTF, reactor is delivered into through pipeline 262 The bottom of 2BRE, the feed distributor 2BTFS (not shown) of usually reacted device bottom feed inlet top installation carry out pre- Distribution is evenly distributed to charging as far as possible on the entire horizontal feed section of distribution plate 2BS；From the lower part distribution plate 1BS Gas, liquid, solid body particle mixed phase material, flows up, the uplink mistake in reactor 2BRE main reaction space after distribution plate 2BS The top product 2BRTP that direct hydrogenation liquefaction of coal reaction is converted into reactor 2BRE is carried out in journey.

As shown in fig. 6, top product 2BRTP is through the entrance of pipeline 267 top reactor 2ARE by reactor head wall Liquid space is taken off with the part of liquid collection cups 2AV composition, carries out part after mixing with the product 2ARP come in autoreactor 2ARE De- liquid.As shown in fig. 6, the liquid in the mix products of top preferentially settles into collection cups 2AV under the effect of gravity, and receiving Gradually deviate from bubble during decline inside collection cup 2AV, the circulation liquid phase 2ARL for deviating from bubble enters the bottom collection cups 2AV Conduit 2AVP in flow downward reactor be discharged, enter in circulation force (forcing) pump 2APUMP through piping 258, the after pressurization Two circulation liquid phase 2BRL1 are conveyed through piping 269, then deliver into cyclic process in reactor 2BRE through pipeline 262.

Fig. 7 is the schematic diagram of the 6th kind of typical process of the invention, the base of the 4th kind of typical process of the invention shown in Fig. 5 It on plinth, reuses parallel coupled reaction system and forms third conversion zone, the reactor 3ARE of third conversion zone is received from the The reactor 3BRE of the gas-liquid mixed phase product of two conversion zones, third conversion zone receives the liquid product from the second conversion zone.

As shown in fig. 7, the difference is that, reactor 2ARE collection liquid enters through piping 258 with process shown in Fig. 5 It recycles in force (forcing) pump 2APUMP, the first circulation liquid phase 2ARL1 after pressurization is conveyed through piping 259 and returned to 2ARE, after pressurization Second circulation liquid phase 2BRL1 is conveyed through piping 269 and is returned to 2BRE, and the liquid product 2ALPB after in addition increasing pressurization passes through Pipeline 266 delivers into 3BRE.

As shown in fig. 7, the second conversion zone conveyed through pipeline 351 combines net product 2TNP in reactor 3ARE system, Mixing is mixed into the circulation liquid phase 3ARL1 (gas phase may be contained, contain the liquid product from 3ARE) conveyed through pipeline 359 Expect 3ATF, the bottom of reactor 3ARE is delivered into through pipeline 352, the charging of usually reacted device bottom feed inlet top installation Distributor 3ATFS (not shown) carry out predistribution make charging be evenly distributed to as far as possible distribution plate 3AS it is entire it is horizontal into Expect on section；Gas, liquid, solid body particle mixed phase material from the lower part distribution plate 3AS, flows up after distribution plate 3AS, The top that direct hydrogenation liquefaction of coal reaction is converted into reactor 3ARE is carried out during the uplink in reactor 3ARE main reaction space Product 3ARP.

As shown in fig. 7, the top product 3BRTP for carrying out autoreactor 3BRE enter the top reactor 3ARE by reactor top The part of portion's wall and liquid collection cups 3AV composition takes off liquid space, mixes with the product 3ARP come in autoreactor 3ARE laggard Row part takes off liquid.As shown in fig. 7, the liquid in the mix products of top preferentially settles into collection cups 3AV under the effect of gravity, And gradually deviating from bubble during decline inside collection cups 3AV, the circulation liquid phase 3ARL for deviating from bubble enters collection cups 3AV It flows downward in the conduit 3AVP of bottom and reactor is discharged, enter in circulation force (forcing) pump 3APUMP through piping 358, after pressurization First circulation liquid phase 3ARL1 is conveyed through piping 359, is then mixed into mixture 3ATF with mixture 3AF1, through pipeline 352 Deliver into cyclic process in reactor 3ARE.

It is the liquid product 2ALPB that is conveyed through pipeline 266, defeated through pipeline 360 as shown in fig. 7, in reactor 3BRE system The hydrogen 3BH1 sent (may contain gas phase, contain the liquid phase from 3ARE with the circulation coal 3BRL1 conveyed through pipeline 369 The liquid product of product and 3BRE) it is mixed into mixture 3BTF, the bottom of reactor 3BRE is delivered into through pipeline 362, usually The feed distributor 3BTFS (not shown) of reacted device bottom feed inlet top installation, which carries out predistribution, makes charging as far as possible It is evenly distributed on the entire horizontal feed section of distribution plate 3BS；Gas, liquid, solid body particle mixed phase from the lower part distribution plate 3BS Material flows up after distribution plate 3BS, and it is direct that coal hydrogenation is carried out during the uplink in reactor 3BRE main reaction space Liquefaction reaction is converted into the top product 3BRTP of reactor 3BRE.

As shown in fig. 7, top product 3BRTP is through the entrance of pipeline 367 top reactor 3ARE by reactor head wall Liquid space is taken off with the part of liquid collection cups 3AV composition, carries out part after mixing with the product 3ARP come in autoreactor 3ARE De- liquid.As shown in fig. 7, the liquid in the mix products of top preferentially settles into collection cups 3AV under the effect of gravity, and receiving Gradually deviate from bubble during decline inside collection cup 3AV, the circulation liquid phase 3ARL for deviating from bubble enters the bottom collection cups 3AV Conduit 3AVP in flow downward reactor be discharged, enter in circulation force (forcing) pump 3APUMP through piping 358, the after pressurization Two circulation liquid phase 3BRL1 are conveyed through piping 369, then deliver into cyclic process in reactor 3BRE through pipeline 362.

Fig. 8 is the schematic diagram of the 7th kind of typical process of the invention, the base of the 4th kind of typical process of the invention shown in Fig. 5 It on plinth, reuses parallel coupled reaction system and forms third conversion zone, the reactor 3ARE of third conversion zone is received from the The mixed phase product and liquid product of two conversion zones, the reactor 3BRE of third conversion zone receive the liquid phase from the second conversion zone and produce Object.

As shown in figure 8, the difference is that, reactor 2ARE collection liquid enters through piping 258 with process shown in Fig. 5 It recycles in force (forcing) pump 2APUMP, the first circulation liquid phase 2ARL1 after pressurization is conveyed through piping 259 and returned to 2ARE, after pressurization Second circulation liquid phase 2BRL1 is conveyed through piping 269 and is returned to 2BRE, and the liquid product 2ALPA after in addition increasing pressurization passes through Pipeline 263 delivers into 3ARE, and the liquid product 2ALPB after in addition increasing pressurization delivers into 3BRE through piping 266.

It is the liquid phase material 2ALPA that is conveyed through pipeline 263, defeated through pipeline 350 as shown in figure 8, in reactor 3ARE system The hydrogen 3AH1 sent (may contain gas phase, containing from 3ARE, 3BRE with the circulation liquid phase 3ARL1 conveyed through pipeline 359 Liquid product) it is mixed into mixture 3ATF, the bottom of reactor 3ARE is delivered into through pipeline 352, usual reacted device bottom The feed distributor 3ATFS (not shown) of feed inlet top installation, which carries out predistribution, is evenly distributed to charging as far as possible point On entire horizontal feed section with disk 3AS；Gas, liquid, solid body particle mixed phase material from the lower part distribution plate 3AS, through excessive With being flowed up after disk 3AS, direct hydrogenation liquefaction of coal reaction is carried out during the uplink in reactor 3ARE main reaction space and is turned Turn to the top product 3ARP of reactor 3ARE.

As shown in figure 8, combining net product 2TNP through the second conversion zone that pipeline 270 conveys, being come from through what pipeline 367 conveyed The top product 3BRTP of reactor 3BRE enter the top reactor 3ARE by reactor head wall and liquid collection cups 3AV The part of composition takes off liquid space, and part is carried out after mixing with the product 3ARP come in autoreactor 3ARE and takes off liquid.As shown in figure 8, Liquid in the mix products of top preferentially settles into collection cups 3AV under the effect of gravity, and inside the collection cups 3AV under Gradually deviate from bubble during drop, the circulation liquid phase 3ARL for deviating from bubble enters in the conduit 3AVP of the bottom collection cups 3AV downwards Flowing discharge reactor, enters in circulation force (forcing) pump 3APUMP through piping 358, the first circulation liquid phase 3ARL1 warp after pressurization Piping 359 conveys, and is then mixed into mixture 3ATF with mixture 3AH1, delivers into reactor 3ARE through pipeline 352 Cyclic process.

It is the liquid product 2ALPB that is conveyed through pipeline 266, defeated through pipeline 360 as shown in figure 8, in reactor 3BRE system The hydrogen 3BH1 sent (may contain gas phase, contain the liquid phase from 3ARE with the circulation coal 3BRL1 conveyed through pipeline 369 The liquid product of product and 3BRE) it is mixed into mixture 3BTF, the bottom of reactor 3BRE is delivered into through pipeline 362, usually The feed distributor 3BTFS (not shown) of reacted device bottom feed inlet top installation, which carries out predistribution, makes charging as far as possible It is evenly distributed on the entire horizontal feed section of distribution plate 3BS；Gas, liquid, solid body particle mixed phase from the lower part distribution plate 3BS Material flows up after distribution plate 3BS, and it is direct that coal hydrogenation is carried out during the uplink in reactor 3BRE main reaction space Liquefaction reaction is converted into the top product 3BRTP of reactor 3BRE.

As shown in figure 8, top product 3BRTP is through the entrance of pipeline 367 top reactor 3ARE by reactor head wall Liquid space is taken off with the part of liquid collection cups 3AV composition, carries out part after mixing with the product 3ARP come in autoreactor 3ARE De- liquid.As shown in figure 8, the liquid in the mix products of top preferentially settles into collection cups 3AV under the effect of gravity, and receiving Gradually deviate from bubble during decline inside collection cup 3AV, the circulation liquid phase 3ARL for deviating from bubble enters the bottom collection cups 3AV Conduit 3AVP in flow downward reactor be discharged, enter in circulation force (forcing) pump 3APUMP through piping 358, the after pressurization Two circulation liquid phase 3BRL1 are conveyed through piping 369, then deliver into cyclic process in reactor 3BRE through pipeline 362.

Fig. 9 is the schematic diagram of the 8th kind of typical process of the invention, the base of the 5th kind of typical process of the invention shown in Fig. 6 It on plinth, reuses parallel coupled reaction system and forms third conversion zone, the reactor 3ARE of third conversion zone is received from the The reactor 3BRE of the mixed phase product of two conversion zones, third conversion zone receives the liquid product from the second conversion zone.

As shown in figure 9, the difference is that, reactor 2ARE collection liquid enters through piping 258 with process shown in Fig. 6 It recycles in force (forcing) pump 2APUMP, the first circulation liquid phase 2ARL1 after pressurization is conveyed through piping 259 and returned to 2ARE, after pressurization Second circulation liquid phase 2BRL1 is conveyed through piping 269 and is returned to 2BRE, and the liquid product 2ALPB after in addition increasing pressurization passes through Pipeline 266 delivers into 3BRE.

As shown in figure 9, the working method of the reactor 3ARE of third conversion zone, reactor 3BRE, send out with shown in Fig. 7 The reactor 3ARE of the third conversion zone of the 6th kind of bright typical process, the working method of reactor 3BRE are identical.

Figure 10 is the schematic diagram of the 9th kind of typical process of the invention, the 5th kind of typical process of the invention shown in Fig. 6 On the basis of, it reuses parallel coupled reaction system and forms third conversion zone, the reactor 3ARE reception of third conversion zone comes from The reactor 3BRE of the mixed phase product and liquid product of second conversion zone, third conversion zone receives the liquid phase from the second conversion zone Product.

As shown in Figure 10, with process shown in Fig. 6 the difference is that, reactor 2ARE collection liquid through piping 258 into Enter to recycle the first circulation liquid phase 2ARL1 in force (forcing) pump 2APUMP, after pressurization and convey return 2ARE through piping 259, after pressurization Second circulation liquid phase 2BRL1 through piping 269 convey return 2BRE, in addition increase pressurization after liquid product 2ALPA warp Piping 263 delivers into 3ARE, and the liquid product 2ALPB after in addition increasing pressurization delivers into 3BRE through piping 266.

As shown in Figure 10, the working method of the reactor 3ARE of third conversion zone, reactor 3BRE, with shown in Fig. 8 The reactor 3ARE of the third conversion zone of 7th kind of typical process of invention, the working method of reactor 3BRE are identical.

Figure 11 is the schematic diagram of the 10th kind of typical process of the invention, of the invention the 2nd kind typical process shown in Fig. 3 On the basis of, the pre-hydrotreating reaction section of suspended-bed reactor 0PRE composition is increased, either shallow direct hydrogenation liquefaction of coal is carried out Reaction obtains either shallow direct hydrogenation liquefaction of coal reaction product, and the net product 0PRTP of pre-hydrotreating reaction section all enters as lower charging Reactor 1ARE.

As shown in figure 11, in reactor 0PRE system, the mixture of the coal and hydrogen that are conveyed through pipeline 051 0PF1 is mixed into mixture 0PTF with the circulation liquid phase 0PRL1 (may contain gas phase) conveyed through pipeline 059, defeated through pipeline 052 It is fed into the bottom of reactor 0PRE, the feed distributor 0PTFS of usually reacted device bottom feed inlet top installation is (in figure not Show) carry out predistribution make charging be evenly distributed on the entire horizontal feed section of distribution plate 0PS as far as possible；From distribution plate The gas, liquid, solid body particle mixed phase material of the lower part 0PS, flows up after distribution plate 0PS, empty in reactor 0PRE main reaction Between uplink during carry out direct hydrogenation liquefaction of coal reaction and be converted into the top product 0PRP of reactor 0PRE.

As shown in figure 11, top product 0PRP passes through between reactor 0PRE upper inside wall and liquid collection cups 0PV outer wall Annular gap after, taken off into the part being made of reactor head wall and liquid collection cups 0PV on the top reactor 0PRE Liquid space.As shown in figure 11, the liquid in top product preferentially settles into collection cups 0PV under the effect of gravity, and is receiving Gradually deviate from bubble during decline inside collection cup 0PV, the circulation liquid phase 0PRL for deviating from bubble enters the bottom collection cups 0PV Conduit 0PVP in flow downward reactor be discharged, enter in circulation force (forcing) pump 0PPUMP through piping 058, following after pressurization Ring liquid phase 0PRL1 is conveyed through piping 059, is then mixed into mixture 0PTF with mixture 0PF1, through pipeline 052 convey into Enter cyclic process in reactor 0PRE.

As shown in figure 11, top product 0PRP, which is separated into, recycles liquid phase 0PRL and net product 0PRTP, and net product 0PRTP is Gas, liquid, solid body particle mixed phase material, under the action of reactor 0PRE top gas phase pressure, by being inserted into liquid collection cups 0PV Reactor 0PRE is discharged in 057 uplink of product diversion pipe under liquid level, into the first conversion zone reactor 1ARE of downstream.

Figure 12 is the schematic diagram of the 11st kind of typical process of the invention, with the 10th kind of exemplary flow of the invention shown in Figure 11 Journey the difference is that, the liquid product 0PLPA of pre-hydrogenator 0PRE enters the reactor 1ARE's of the first conversion zone Bottom is fed in 1ATF, and the top gas-liquid product 0PRTP of pre-hydrogenator 0PRE is at least without the reaction of the first conversion zone The main body reaction compartment of device 1ARE, Figure 12 show the top gas-liquid product 0PRTP of pre-hydrogenator 0PRE without The case where reactor 1ARE of one conversion zone.

As shown in figure 12, with process shown in Figure 11 the difference is that, reactor 0PRE collection liquid through piping 058 into Enter to recycle the circulation liquid phase 0PRL1 in force (forcing) pump 0PPUMP, after pressurization and convey return 0PRE through piping 059, in addition increases Liquid product 0PLPA after pressurization delivers into 1ARE through piping 063.

It, can be by the charging of two parallel reactors in an order of reaction in downstream based on process shown in Fig. 5 to Figure 12 It is exchanged, technological effect is still identical.

Specific embodiment

The present invention described in detail below.

Pressure of the present invention, refers to absolute pressure.

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

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

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

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

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

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

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

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

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

Middle matter hydrocarbon of the present invention is diesel component, refers to that normal boiling point is 200~330 DEG C of hydro carbons.

Wax oil component of the present invention refers to that normal boiling point is 330~530 DEG C of hydro carbons.

Heavy hydrocarbon of the present invention refers to that normal boiling point is higher than 330 DEG C of hydro carbons.

Hydrogen to oil volume ratio of the present invention refers to the normal of the standard state volume flow of hydrogen and specified oily logistics The ratio of pressure, 20 DEG C of volume flow.

Hydrogen supply hydrocarbon is described below.

Hydrogen supply hydrocarbon described herein refers to the hydrocarbon component in direct hydrogenation liquefaction of coal reaction process with hydrogen supply function, Hydrogen supply hydrocarbon includes the polycyclic aromatic hydrocarbon of the double ring arene of fractional saturation, fractional saturation, is the confession that direct hydrogenation liquefaction of coal process uses The ideal composition of hydrogen solvent naphtha.In hydrogen supply hydrocarbon, the hydrogen supply speed of dihydro body is all larger than tetrahydro body, the dihydro body of thrcylic aromatic hydrocarbon and double The dihydro body of cycloaromatics is compared, and it is low that hydrogen supply speed has height to have；Although test it has been proved that polycyclic aromatic hydrocarbon without hydrogen supply capacity, There is the ability of transmitting hydrogen.At 400 DEG C, the opposite hydrogen supply speed of following component is as follows:

DCL/Direct coal liquefaction process described in detail below, it includes direct hydrogenation liquefaction of coal method and other DCL/Direct coal liquefaction sides Method.

DCL/Direct coal liquefaction process of the present invention refers to the method that processing coal directly obtains hydrocarbon liquid, according to solvent The oily difference with catalyst, the difference of pyrolysis way and the difference and process conditions that add hydrogen mode, can be divided into following several Technique:

1. dissolution pyrolysis liquefaction process: low-ash extract can be made to pyrolysis of coal extracting using heavy solvent, and (Japan claims Swelling charcoal)；Extract the available oils based on mink cell focus at supercritical conditions using light solvent.This method does not have to hydrogen, Though former process yield is high but product is still solid, latter technique such as supercritical extraction (extraction) method (SCE) extract content is not It is too high；

2. solvent adds hydrogen to extract liquefaction process: if any solvent refined coal process I and II (SRC-1 and SRC-II), Exxon donor solvent process EDS, Japanese New Energy Development Organization liquefaction process (NEDOL) etc., using hydrogen, but pressure is less high, and solvent naphtha has apparent work With；

3. Hydrogenation method: such as the H coal process (H- of the old and new's liquefaction process (IG and the NewlG) and the U.S. of Germany ) etc. Coal this kind is belonged to；

4. coal and residual oil joint processing method (C0processing): oily coal refines altogether, refers to simultaneously spreading out to coal and non-coal Oil generation carries out total processing, usually once passes through reactor together with coal by solvent naphtha of residual oil, does not have to recycle oil.Residual oil is sent out simultaneously Raw hydrocracking is converted into light oil.The technique that the U.S., Canada, Germany and former Soviet Union etc. have nothing in common with each other；

5. underground liquefaction process: solvent being injected subterranean coal, makes coal depolymerization and dissolution, in addition the impact force of fluid collapses coal It dissipates, the coal not being completely dissolved is then suspended in solvent, is extracted solution out with pump and is separated processing；

6. destructive distillation liquefaction process: coal is first pyrolyzed and obtains tar, then carries out hydrocracking and upgrading to tar.

Direct hydrogenation liquefaction of coal process is described below.

Direct hydrogenation liquefaction of coal process of the present invention, refers to the side of the Coal Liquefaction under solvent naphtha existence condition Method, solvent naphtha, which can be, improves the hydrogen supply dissolvent oil of hydrogen supply capacity by stabilized hydrogenation process or without by stabilized hydrogenation process Modified solvent naphtha, according to the difference of solvent naphtha, the difference of catalyst and hydrogenation process conditions, there are many different process, such as with Under several techniques:

1. solvent adds hydrogen to extract liquefaction process: if any solvent refined coal process I and II (SRC-I and SRC-II), Exxon donor solvent process EDS, Japanese New Energy Development Organization liquefaction process (NEDOL) etc., using hydrogen, but pressure is less high, and solvent naphtha has apparent work With；

2. Hydrogenation method: such as the H coal process (H- of the old and new's liquefaction process (IG and the NewlG) and the U.S. of Germany ) etc. Coal this kind is belonged to；

3. coal and residual oil joint processing method (C0processing): once passing through together with coal using residual oil as solvent naphtha anti- Device is answered, recycle oil is not had to；Hydrocracking occurs is converted into light oil to residual oil simultaneously；The U.S., Canada, Germany and former Soviet Union etc. are each There is different technique；

4. Chinese Shenhua Group coal direct liquefaction method；

5. a kind of thermally dissolving and catalytic method with lignite preparing liquid fuel that patent CN100547055C states clearly, belongs in lignite Pressure plus hydrogen direct liquefaction process, including Coal liquefaction process and liquefied coal coil hydrogenation modification process totally two processes.In order to mention The conversion ratio and realization coal feedstock of high coal direct liquefaction enter reactor, and coal leads to before entering reactor Coal dust often is made, is made into coal with the solvent naphtha for having good hydrogen supply capacity, coal is pressurized, enters coal liquefaction after heating Reactor.

During direct hydrogenation liquefaction of coal, no matter which kind of coal faces hydrogen direct liquefaction process, and target is to obtain oil product, is chased after The function of asking is " coal turns oil ", it is necessary to which existing chemical change is " coal hydrogenation ", and the common trait of current such technology is to make With solvent naphtha and catalyst, the conventional boiling range of solvent naphtha is generally 200~530 DEG C, most is for 200~450 DEG C, the best 265~430 DEG C, solvent naphtha majority is distilled oil or its hydrogenation modification oil, and contained aromatic hydrocarbons majority is the virtue of 2~4 ring structures Hydrocarbon.Therefore, either which kind of coal faces hydrogen direct liquefaction process, and (usually coal liquefaction is light for the outer oil extraction of its generation or liquefied coal coil Oil) or liquefied coal coil modified oil as long as its composition has raw material compositing characteristic of the present invention the method for the present invention can be used It is processed into high aromatic hydrogenation heat cracking reaction process BR.

Direct hydrogenation liquefaction of coal process of the present invention refers to using coal and molecule hydrogen that may be present as raw material, It is hydrogen supply dissolvent oil with specific oil product (the usually hydrogenation modification oil of liquefied coal coil), in certain operating condition (as operated Temperature, operating pressure, solvent naphtha/coal weight ratio, hydrogen/solvent naphtha volume ratio and suitable hydrogenation catalyst) under, coal is directly sent out The reaction process of the hydrogenation liquefactions such as raw carbon-carbon bond thermal cracking, free radical stabilized hydrogenation.

Direct hydrogenation liquefaction of coal oil of the present invention, refers to the oil product that the Coal Liquefaction reaction process generates, it It is present in Coal Liquefaction reaction effluent, is the synthesis based on hydrogen supply dissolvent oil, reaction consumption coal and reaction transfer hydrogen Reaction product.

After direct hydrogenation liquefaction of coal reaction process works well, hydrogen supply dissolvent oil generallys use Coal Liquefaction and reacted The hydrogenation modification oil of the self-produced liquefied coal coil of journey (usually conventional distillate of the boiling range higher than 165 DEG C), liquefied coal coil add hydrogen to change Property process main target be production direct hydrogenation liquefaction of coal reaction process solvent naphtha, be specifically exactly to improve in oil product The content of " component with good hydrogen supply function ", for example naphthenic base benzene class, the content of bicyclic alkyl benzene class component are improved, it is based on Liquefied coal coil contains the fact that a large amount of double ring arenes and a large amount of thrcylic aromatic hydrocarbons, and liquefied coal coil hydrogenation modification process is one " suitable The hydrogenation process of degree aromatic hydrocarbons saturation ".

The final goal of Coal liquefaction process is the outer oil product supplied of production, and usual liquefied coal coil hydrogenation modification process generates Hydrogenation modification oil be two parts: a part be used as Coal liquefaction process hydrogen supply dissolvent oil, a part be used as coal liquefaction The outer oil extraction of liquefaction process.In general, at least part coal liquefaction light oil that Coal liquefaction process generates is used as outside coal oil process Oil extraction A, it is molten that remaining liquefied coal coil is used as liquefied coal coil hydrogenation modification process feedstock oil production Coal liquefaction process hydrogen supply There is the outer oil extraction of A and B two-way in agent oil and outer oil extraction B, the final whereabouts of the outer oil extraction of A and B two-way is usually through too deep at this time Degree plus hydrogen grading process produce high-quality oil product such as diesel oil distillate, naphtha cut.

In direct hydrogenation liquefaction of coal reaction process, hydrogen supply dissolvent is substantially a kind of the most important of coal liquefaction positive reaction Foreground catalyst, he quickly provides most of reactive hydrogen of coal liquefaction, it directly decides pyrolysis free radical fragment The stable speed of flash hydrogcnation, thus thermal condensation is inhibited to react；In direct hydrogenation liquefaction of coal reaction process, solid catalyst A kind of retarding agent of such as pyrite, molybdenum sulfide substantially more like coal liquefaction negative reaction, it is big that solid catalyst particle adsorbs viscosity Colloid, asphaltene molecules MK, and contact MK with the reactive hydrogen of solid catalyst surface, to inhibit its pyrocondensation；In coal plus In hydrogen direct liquefaction reaction process, a kind of substantially still hydrogen supply agent dehydrogenation simultaneously such as solid catalyst such as pyrite, molybdenum sulfide The recovery catalyst of object SH-Z, solid catalyst particle adsorbs SH-Z, and connects the reactive hydrogen of SH-Z and solid catalyst surface Touching, thus plus hydrogen be restored to the hydrogen supply hydrocarbon for having hydrogen supply capacity, it directly decides the recovery speed of hydrogen supply agent dehydrogen substance SH-Z； In direct hydrogenation liquefaction of coal reaction process, substantially still a kind of target is hydrocracked solid catalyst such as pyrite etc. simultaneously The weak action catalysts of reaction such as asphaltene, preasphaltene being hydrocracked.Therefore, in direct hydrogenation liquefaction of coal reaction process In, in certain sense, solid catalyst such as pyrite, molybdenum sulfide etc. is more like a kind of catalyst of backstage running, to coal Liquefaction target product distillate plays a kind of support property and the effect of promotion property.In coal hydrogenation liquefaction reaction process, due to hydrogen supply The effect of solvent DS is extremely important, and therefore, the operating condition and effect of the stable reaction process of solvent oil hydrogenation are naturally of crucial importance.

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

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

Back-mixing stream expanded bed reaction zone of the present invention, refers to the mode of operation of the reaction zone using expanded bed reactor There are liquid stream back-mixings there is circulation fluid in other words；Back-mixing stream or circulation fluid refer to the intermediate product XK or final at flow points K At least part liquid phase XK-L in product X K is as the upstream reaction zone circulating fluid XK-LR return logistics XK, circulating fluid The reaction product of XK-LR flows through K point and is present among XK.The mode for forming back-mixing stream can be any appropriate mode, such as Built-in inner ring flow cartridge, built-in outer ring flow cartridge, built-in liquid collecting cup+diversion pipe+circulating pump, external circulation pipe etc. are set.

The liquid collecting cup or liquid trap being arranged in reactor of the present invention, refer to being arranged in reactor for collecting The container of liquid, usual top or upper side opening, bottom or lower side installation diversion pipe are for being discharged collection liquid；Expansion The top liquid trap of bed reactor, is typically mounted on the de- liquid zone of gas-liquid material, obtains liquid and gas-liquid mixed phase logistics or obtain Liquids and gases.

Suspended-bed reactor of the present invention, structure type can be any one suitable form, can be empty cylinder Suspended-bed reactor can be using internal circulation guide shell to form piston flow or the back-mixing stream there are interior circulation to shape At circulation in inside or internal outside circulation, can be makes top reaction compartment liquid flow into lower part using its outer circulating tube reacts empty Between shaper outer circulation stream back-mixing flow pattern, can be using top product liquid collect and flow guide system to by circulation plus Pressure system forms the back-mixing flow pattern for forcing inner recirculation flow.

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

Direct hydrogenation liquefaction of coal reaction process of the present invention, usually using up-flow reactor, working method be can choose:

1. floating bed hydrogenation reactor；

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

3. slight expanded-bed.

The high aromatic hydrogenation heat cracking reaction process BR of the present invention, the reactor used, working method can choose:

1. floating bed hydrogenation reactor；

3. up flow type slight expanded-bed；

4. upflow fixed bed；

5. down-flow fixed bed；

6. the low liquid phase systemic circulation hydrogenator of hydrogen to oil volume ratio.

Solvent oil hydrogenation of the present invention stablizes reaction process CR, the reactor used, and working method can choose:

1. floating bed hydrogenation reactor；

3. up flow type slight expanded-bed；

4. upflow fixed bed；

5. down-flow fixed bed；

Oil product obtained by direct hydrogenation liquefaction of coal, including naphtha (60~180 DEG C of fractions of conventional boiling range), the first light diesel fuel (180~220 DEG C of fractions of conventional boiling range), the second light diesel fuel (220~265 DEG C of fractions of conventional boiling range), heavy diesel fuel (conventional boiling range 265~350 DEG C of fractions), light wax oil (350~480 DEG C of fractions of conventional boiling range), (480~530 DEG C of conventional boiling range evaporates wax slop Point), liquefaction residual oil (normal boiling point be higher than 530 DEG C of hydro carbons).

Naphtha (60~180 DEG C of fractions of conventional boiling range) in coal liquefaction products, is target product fraction, as needed, Deep hydrofinishing such as desulfurization, denitrogenation can be carried out to it, it is usually desirable to generation benzene ring hydrogenation saturated reaction as few as possible.

The first light diesel fuel (180~220 DEG C of fractions of conventional boiling range) in coal liquefaction products is often unsuitable for entering coal hydrogenation Direct liquefaction reaction process because boiling point too it is low be easy to vaporize be difficult to serve as liquid phase solvent component；If direct into coal hydrogenation Liquefaction reaction process, the product of further heat cracking reaction are exactly to generate bulk gas and uneconomical；Therefore, unless carburet hydrogen valence It is worth huge, the first light diesel fuel should not usually enter direct hydrogenation liquefaction of coal reaction process or Special hydrogenation thermal cracking process or add hydrogen Cracking process or other thermal cracking processes are processed, and can usually be entered hydrofining reaction process and be carried out desulfurization, denitrogenation, raw Produce cleaning light diesel fuel.

The second light diesel fuel (220~265 DEG C of fractions of conventional boiling range) in coal liquefaction products, stabilized hydrogenation oil product is coal The hydrogen supply dissolvent oil that the boiling point for adding hydrogen direct liquefaction reaction process to need is suitable, hydrogen supply capacity is excellent is in addition straight for coal hydrogenation Liquefaction process, the second light diesel fuel or its stabilized hydrogenation oil are connect, in the front reaction process of direct hydrogenation liquefaction of coal reaction process Play a part of the basic solvent composition of liquid phase, but it is most of in the rear portion reaction process of direct hydrogenation liquefaction of coal reaction process Vaporized, and usually direct hydrogenation liquefaction of coal reaction process is there are the resource of surplus thus to belong to direct hydrogenation liquefaction of coal anti- The major product of process is answered, therefore, the second light diesel fuel of coal liquefaction products or its stabilized hydrogenation oil, usually part is used as lightweight hydrogen supply Solvent naphtha is used for direct hydrogenation liquefaction of coal reaction process, is partially used as plus hydrogen upgraded material is for adding the production of hydrogen upgrading reaction process Final products.

Heavy diesel fuel (265~350 DEG C of fractions of conventional boiling range) in coal liquefaction products, stabilized hydrogenation oil product is coal hydrogenation The hydrogen supply dissolvent oil that the most desirable boiling point of direct liquefaction reaction process is suitable, hydrogen supply capacity is excellent, it is in addition direct for coal hydrogenation Liquefaction process, heavy diesel fuel or its stabilized hydrogenation are oily, and it is basic to play liquid phase in the whole process of direct hydrogenation liquefaction of coal reaction process The effect of solvent composition, and usually direct hydrogenation liquefaction of coal reaction process is there are the resource of surplus thus to belong to coal hydrogenation direct The major product of liquefaction reaction process, therefore, coal liquefaction products heavy diesel fuel or its stabilized hydrogenation oil, usually part is used as heavy and supplies Hydrogen solvent naphtha is used for direct hydrogenation liquefaction of coal reaction process, is partially used as plus hydrogen upgraded material is for adding hydrogen upgrading reaction process raw Produce final products.

Light wax oil (350~480 DEG C of fractions of conventional boiling range) in coal liquefaction products, stabilized hydrogenation oil product is coal hydrogenation The hydrogen supply dissolvent oil that the most desirable boiling point of direct liquefaction reaction process is suitable, hydrogen supply capacity is excellent, it is in addition direct for coal hydrogenation Liquefaction process, light wax oil or its stabilized hydrogenation oil, play liquid phase in the final high temperature stage of direct hydrogenation liquefaction of coal reaction process The effect of basic solvent composition, and the usually direct hydrogenation liquefaction of coal reaction process scarce resource that is difficult to Equilibrium, because This, coal liquefaction products light wax oil or its stabilized hydrogenation oil are usually completely used as heavy hydrogen supply dissolvent oil for the direct liquid of coal hydrogenation Change reaction process, while carrying out the heat from hydrogenation cracking reaction of its lighting process needs.

Wax slop (480~530 DEG C of fractions of conventional boiling range) in coal liquefaction products, these contain solid particle, seriously lack The lighting process of the material of hydrogen, it is necessary to rich in hydrogen supply hydrocarbon the liquid-phase condition for being capable of providing a large amount of active hydrogen atoms under into Row, is unlikely to quick coking just to maintain device long-term operation, dispersion of the coal liquefaction wax slop in the liquid phase in reactor It is also required to the dispersing and dissolving by means of a large amount of hydrogen supply hydrocarbon, the thermal condensation object or coking material of coal liquefaction wax slop are also required to rely on liquefaction Semicoke is aggregation support dispersion and carries out reaction compartment, and therefore, coal liquefaction wax slop enters direct hydrogenation liquefaction of coal and reacted Cheng Jinhang deep conversion is reasonable inevitable choice, and coal liquefaction wax slop is by adding hydrogen in other words obtained by stabilized hydrogenation reaction process Stablizing oil to enter direct hydrogenation liquefaction of coal reaction process to carry out deep conversion is reasonable inevitable choice；In addition straight for coal hydrogenation Liquefaction process, wax slop or its stabilized hydrogenation oil are connect, plays liquid in the final high temperature stage of direct hydrogenation liquefaction of coal reaction process The mutually effect of basic solvent composition, and the usually direct hydrogenation liquefaction of coal reaction process scarce resource that is difficult to Equilibrium, Therefore, coal liquefaction products wax slop or its stabilized hydrogenation oil, it is direct for coal hydrogenation to be usually completely used as heavy hydrogen supply dissolvent oil Liquefaction reaction process, while carrying out the heat from hydrogenation cracking reaction of its lighting process needs.

Since the i.e. liquefaction residual oil of hydro carbons of the normal boiling point higher than 530 DEG C is present in VACUUM TOWER BOTTOM coal liquefaction in coal liquefaction products In bottoms stream, usual discharge system no longer cyclic process is utilized, and certainly, can be partially recycled back to as needed.

Characteristic of the invention is described below.

1. suspended-bed reactor；

2. fluidized bed reactor；

3. suspension bed and ebullated bed combined reactor；

4. up flow type expanded bed；

5. upflow fixed bed.

Recycle the second conversion zone reaction product；

Recycle third conversion zone reaction product；

The present invention uses 2 parallel coupled formula reactors in the conversion zone DRN of direct hydrogenation liquefaction of coal reaction system RU NARE, NBRE, a reactor processing oil coal slurry liquid material and/or coal liquefaction intermediate product liquid material, another reactor can be processed The hydro-conversion thing liquid material of non-coal base weight oil or non-coal base weight oil.

The general control principle of the gas-phase presulfiding hydrogen concentration of detailed description of the present invention hydrogenation process.

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

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

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

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

Hydrogenation reaction effluent or hot high score gas or warm high score gas enter before cold anticyclone separate section, usually first reduce temperature (temperature should be higher than that in the hydrogenation reaction effluent gas phase degree (usually with reactive moieties feed exchange heat) to about 220~100 DEG C Crystallization temperature, the crystallization temperature of sal-ammoniac of sulphur hydrogenation ammonia), then usually injection washing water formation water filling back end hydrogenation is anti-thereto Answer effluent, it may be necessary to which 2 or multiple injection points are set, and washing water is used for absorbing ammonia and issuable other impurity such as chlorine Change hydrogen etc., and the aqueous solution after absorbing ammonia necessarily absorbs hydrogen sulfide.In cold anticyclone separate section, the water filling back end hydrogenation reaction stream Object separates out are as follows: the cold high score gas being mainly made of hydrogen in volume, one mainly by conventional liq hydrocarbon and dissolved hydrogen The cold high score oil of composition, a cold high score water be mainly made of water and dissolved with ammonia, hydrogen sulfide.The cold high score water, The content of middle ammonia is generally 0.5~15% (w), preferably 1~8% (w).One purpose of note washing water is to absorb 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 drop.The injection rate of the washing water should be determined according to following principles: on the one hand, after washing water injects 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, Washing water is used to absorb the ammonia in hydrogenation reaction effluent, prevents the ammonia density of high score gas too high, reduces catalyst activity, usually The lower the ammonia volumetric concentration of high score gas 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), generally should not less than 70% (v), it is suitable not Lower than 80% (v), preferably not below 85% (v).As previously described at least part, be usually 85~100% cold high score gas 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 circulation 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 high score gas to exclude methane, the ethane that reaction generates.For the cold of discharge High score gas can realize hydrogen and non-hydrogen gas component using conventional membrane separation process or pressure swing adsorption technique or oil wash technique Separation, and the hydrogen of recycling is used as new hydrogen.

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

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

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

Embodiment:

Reference examples

Process the factory that 2,000,000 tons/year of coals produce 960,000 tons/year of liquefied coal coils, direct hydrogenation liquefaction of coal reaction process AU, Coal slurry is conveyed to reaction process using a kind of feeding manner of concentration coal slurry of routine, after coal slurry is overpressurized, heats stove heating, into Enter the bottom of up flow type suspension bed the first direct hydrogenation liquefaction of coal reactor；The top first direct hydrogenation liquefaction of coal reactor A UE01 The circulation liquid material of the liquid collecting cup outflow in portion is recycled into the direct liquid of the first coal hydrogenation of up flow type suspension bed after circulating pump pressurizes The bottom for changing reactor, it is upward by the distributor of reactor A UE01 lower disposed after being mixed with charging coal slurry, charging hot hydrogen The main reaction space of reactor A UE01 is flowed into, direct hydrogenation liquefaction of coal reaction is carried out.

Direct hydrogenation liquefaction of coal reaction process AU, the diameter using 3 serial operations is 4.86 meters, length of cylindrical shell sections is 23 meters Suspension bed direct hydrogenation liquefaction of coal reactor, the first direct hydrogenation liquefaction of coal reactor A UE01 product AUE01P enter second Direct hydrogenation liquefaction of coal reactor A UE02, the second direct hydrogenation liquefaction of coal reactor A UE02 product AUE02P enter third coal and add Hydrogen direct liquefaction reactor A UE03, third direct hydrogenation liquefaction of coal reactor A UE03 product AUE03P is as the direct liquid of coal hydrogenation Change reaction final product AUP, carries out Oil-gas Separation, oil product fractionation.

It since reactor diameter is too big, needs to make, therefore, reactor manufacturing expense is high.

Since the gas phase of upstream reactor product all passes through downstream reactor, so, the gas of second, third reactor contains Rate height, that is, liquid Space low efficiency, while containing wide variety of conventional gaseous hydrocarbon, water, hydrogen sulfide, ammonia, carbon monoxide, dioxy in gas phase Change carbon, therefore vapor phase hydrogen concentration low only about 65~70%, and in order to maintain hydrogen partial pressure to be higher than 12.7MPa, operating pressure quilt Compel to be increased to 19MPa.

The operating process of direct hydrogenation liquefaction of coal process AU is described below:

1. catalyst for coal liquefaction, hydrogen supply dissolvent AUDS, coal dust are made into quality of pc concentration in coal process for preparation AM For 45% coal AUF, is pressurizeed with coal force (forcing) pump and input coal heating furnace；Co-catalyst liquid stream pressurization after with oil The coal AUF mixing of coal slurry pressurization pump discharge；

Table 1 is the property of DCL/Direct coal liquefaction reaction process AU feed coal；

Table 2 is the property of DCL/Direct coal liquefaction reaction process AU solvent naphtha；

Table 3 is the catalyst property of DCL/Direct coal liquefaction reaction process AU；

Table 4 is the co-catalyst property of DCL/Direct coal liquefaction reaction process AU；

2. obtaining direct hydrogenation liquefaction of coal reaction product is AUP in direct hydrogenation liquefaction of coal reaction process；

Direct hydrogenation liquefaction of coal reaction process or its feed system will use hydrogen supply dissolvent oil and make flushing oil, cooling down Oil；

Table 5 is direct hydrogenation liquefaction of coal reaction condition summary sheet；

Using forced circulation suspended-bed reactor AUE01, AUE02, AUE03 of 3 serial operations, in every reactor Upper space arranges that built-in gas liquid-liquid separation unit, that is, liquid collection cups, Partial Liquid Phase product enter liquid collection cups, edge Catheter outflow reactor bottom returns to respective reactor inlet after circulating pump pressurizes and forms liquid circulation, liquid circulation Amount is 2.0~2.2 times of coal slurry total amount；Reactor head is discharged along diversion pipe in other mixed phase gas-liquid products；

Direct hydrogenation liquefaction of coal process AU final reacting product AUP temperature is 460 DEG C, and injecting cooling oil and cold hydrogen reduces temperature Degree is to entering high pressure hot separator ATHPS after 410 DEG C；

3., using high pressure hot separator ATHPS, being 410 in temperature in the separate section of Coal Liquefaction reaction product AUP DEG C, pressure be 18~20MPa under conditions of, separation Coal Liquefaction reaction product AUP obtain hot high score oil ATHPS-L and Re Gao Divide gas ATHPS-V；

The hydro carbons in hot high score oil ATHPS-L and hot high score gas ATHPS-V is collected, uses fractionation in fractionating section AFRAC Tower obtains narrow fraction oil product, is that 220~530 DEG C of fractions are sent into solvent oil hydrogenation stabilization process A-CRU by normal boiling point, is supplied Hydrogen solvent naphtha AUDS removes coal process for preparation AM and other uses a little；Obtain about 60 tons/when liquefied residue, go residue to form.

In separation process AF, direct hydrogenation liquefaction of coal reaction product AUP is recycled, obtaining hydrogen volume concentration is 85~88% Hydrogen-rich stream AUH, return to direct hydrogenation liquefaction of coal reaction process and be recycled, the concentrate mode of hydrogen mentions for UF membrane It is pure.

In separation process AF, recycle direct hydrogenation liquefaction of coal reaction product AUP, obtain mainly by conventional boiling range be 250~ The coal liquefaction of 530 DEG C of hydro carbons composition generates oil distillate oil AFD, and it is solid to obtain containing for the hydro carbons comprising normal boiling point higher than 530 DEG C Body dregs of fat AFK；

Part coal liquefaction generates oil distillate oil AFD as material flow A FD1, is used as hydrogen supply dissolvent predecessor hydrocarbon MFB；

Stabilized hydrogenation reaction, which is carried out, in stabilized hydrogenation reaction process MR, hydrogen supply dissolvent predecessor hydrocarbon MFB completes aromatic hydrocarbon molecule Part aromatic ring saturated reaction MRR is converted into stabilized hydrogenation reaction product MRP；

Stabilized hydrogenation reaction product MRP is recycled, hydrogen supply dissolvent DS is obtained；

At least part hydrogen supply dissolvent DS enters direct hydrogenation liquefaction of coal reaction process as hydrogen supply dissolvent LCF-DS, hydrogen supply Solvent LCF-DS and coal dust are formulated as coal slurry LCF use；

Hydrogen supply dissolvent DS is the liquid phase stream containing hydrogen supply dissolvent, the hydro carbons group for being mainly 250~530 DEG C by conventional boiling range At.

Coal Liquefaction reaction process AU, liquefaction oil fractionating section AFRAC, liquefaction oil solvent oil hydrogenation stabilization process are made Liquefied coal coil yield for total system be i.e. 120 tons of 48% (to raw material coal dust)/when, be that the hydrocarbon of normal boiling point C3~380 DEG C evaporates Point, wherein yield of liquefied gas be i.e. 8.0 tons of 4.0% (to raw material coal dust)/when, naphtha yield be 11.5% (to raw material coal dust) I.e. 23.0 tons/when, diesel yield be 65.0 tons of 32.5% (to raw material coal dust)/when.

In above-mentioned total system, hydrogen supply dissolvent amount be 1.22 times of coal dust i.e. 244.0 tons/when, solvent oil hydrogenation was stablized About 243.5 tons of the feed oil of journey production hydrogen supply dissolvent/when, it is the recycle oil being present in total system.

The coal of coal slurry: oily weight ratio is 45.05: 54.95, and the hydrogen supply dissolvent dosage of coal slurry thick in this way is coal blending 122.0%.

Embodiment one

It is anti-for one according to 1 reactor by the direct hydrogenation liquefaction of coal reactors at different levels in reference examples using the present invention Answer the concept of section, on the order of reaction of such 3 serial operations, every grade using 2 diameters is 3.40 meters, length of cylindrical shell sections is 23 meters Parallel coupled formula reactor replaces it, the present invention has the advantages that

1. the first order of reaction, by 2 parallel coupled formula reactor groups at the fresh coal slurry that every reactor receives 50% is former Material；

2. second, third order of reaction, by 2 parallel coupled formula reactor groups at " reactor receives upstream gas for formation Liquid product is lower charging, another reactor reception upstream liquid product is lower charging, and reception upstream liquid product is lower charging Reactor, avoid the intervention of upstream overwhelming majority gas-phase product, by using pure hydrogen material, vapor phase hydrogen concentration can be arrived 88~90%, hydrogen partial pressure is up to 16.7MPa, improves 4.0MPa, effect be it is surprising, be conducive to improve coal liquefaction rate, drop Low gas yield, thermal condensation produce rate.

Upstream liquid product is in the weight from the discharge of upper stage reactor XAUE inner top collection cups mainly by containing solid-liquid The liquid material product for expecting composition conveys after generally going through circulating pump pressurization, also reliable pressure difference gravity flow.

Embodiment two

Based on embodiment one, the first order of reaction, by 2 parallel coupled formula reactor groups at the raw material coal slurry of 2 reactors The different coal slurry of coal concentration, respectively i.e. coal concentration be 45% dilute coal slurry and coal concentration be 55~60% thick coal slurry, but 2 Fresh coal charge (not being coal slurry) total amount that platform reactor receives is identical, controls respectively optimal reaction condition and realizes that myopia is equivalent Liquefying conversion rate, be also convenient to control each road coal slurry warm, conducive to the target for reducing solvent naphtha total amount with slurry is realized.

Reactor diameter is adjusted as required.

The dilute coal slurry warm of high pressure reaches 430 DEG C of method using heating stove heating.

The thick coal slurry warm of high pressure, first heated stove heating reaches 250 DEG C, the circulation coal for being then 465 DEG C with temperature It starches mixed mode mixture temperature is made to reach 430 DEG C and start to react.

Embodiment three

Based on embodiment one, in the second order of reaction, every reactor add 50 tons/when petroleum based heavy fuel oils F100 carry out coal Oily refining altogether, the lighting cracking conversion rate on the basis of 530 DEG C of boiling point of petroleum based heavy fuel oils are greater than 85%.

Table 6 is the analysis data summary table of petroleum based heavy fuel oils F100.

Example IV

Based on reference examples, the factory of the liquefied coal coil of 4,000,000 tons/year of coals is processed, direct hydrogenation liquefaction of coal reaction process AU, When using 3 reactor serial operations, reactor inside diameter needs 7000 millimeters, this is current adds Hydrogen reactor technology of preparing cannot achieve, and according to routine techniques, need to build 2 production lines, every production line processing 2,000,000 Ton/year coal produces about 1,000,000 tons/year of liquefied coal coils, and liquid material collection cups adds hydrogen in this way at the top of the setting of 6 cuff circulating pumps of needs Reactor assembly is needed using 6 circulating pumps.

Using the present invention, three sections of manifold type conversion zones are set up, every section uses 6 to add hydrogen anti-altogether using 2 parallel reactors Device is answered, but only needs 3 circulating pumps, compared with conventional techniques, 3 circulating pumps is eliminated, simplifies the interior of 3 reactors Portion's structure, the effect reduced investment outlay and simplify operation is apparent.

Embodiment five

Based on example IV, the factory that 4,000,000 tons/year of coals produce about 2,000,000 tons/year of liquefied coal coils, stabilized hydrogenation are processed Reaction process MR, stabilized hydrogenation inside reactor diameter need 7000 millimeters, this is current hydrogenator technology of preparing It cannot achieve, according to routine techniques, need to build 2 production lines, liquid material is received at the top of the setting of 2 cuff circulating pumps of needs in this way The hydrogenator system for collecting cup, needs using 2 circulating pumps.

Using the present invention, single hop manifold type reaction system is set up, uses 2 hydrogenation reactions altogether using 2 parallel reactors Device, but 1 circulating pump is only needed, compared with conventional techniques, 1 circulating pump is eliminated, the inside of 1 reactor is simplified Structure, the effect reduced investment outlay and simplify operation is apparent.

The property of 1 DCL/Direct coal liquefaction reaction process AU feed coal of table

The property of 2 DCL/Direct coal liquefaction reaction process AU solvent naphtha of table

The catalyst property of 3 DCL/Direct coal liquefaction reaction process AU of table

Serial number	Project	Data	Remarks
				1	Active component	Nanoscale FeOOH
2	Carrier	Part material coal
				3	Additive amount, (Fe/ dry coal), wt%	1.00
4	The Fe content of fine coal supported catalyst, wt%	5.6±0.5	Permanganimetric method
				5	The granularity of fine coal supported catalyst, wt%		Laser particle size method
	≤74μm	≥80
					74 μm of >	< 20
6	Catalyst is aqueous, wt%	≤4	Gravimetric method

The co-catalyst property of 4 DCL/Direct coal liquefaction reaction process AU of table

5 direct hydrogenation liquefaction of coal reaction condition summary sheet of table

The analysis data summary table of 6 petroleum based heavy fuel oils F100 of table

Serial number	Project	Kuwait's residual oil
			1	Vacuum distillation range, DEG C	538 DEG C of >
2	Density (20 DEG C), kg/m³	1.0273
			3	API	5.8
4	Total sulfur, %	5.11
			5	Ramsbottom carbon residue, %	21.90
6	Nickel, ppm	34
			7	Vanadium, ppm	116

Claims

1. with the coal-based carbon hydrogen material hydrogenation process of 2 parallel coupled formula reactor assemblies, it is characterised in that:

In coal-based carbon hydrogen material hydrogenation process RU, there are hydrogen, conventional liquid hydrocarbon and there may be under conditions of catalyst, Coal-based carbon hydrogen material carries out at least part hydrogenation reaction RUR and is converted into reaction product RUP, recycles reaction product RUP；

Coal-based carbon hydrogen material hydrogenation process RU includes at least one conversion zone, anti-with 2 parallel coupled formulas comprising at least one The conversion zone for answering device to form；Conversion zone segment number is denoted as DRX；

One conversion zone refers to the gas-liquid comprising a coal-based carbon hydrogen material hydrogenation reaction step and the step gas-liquid product The technical process of separating step；

The conversion zone DRN of coal-based carbon hydrogen material hydrogenation process RU is formed with 2 parallel coupleds formula reactor NARE, NBRE Conversion zone, reactor NARE, NBRE be up-flow reactor, reactor NARE headspace be disposed with overhead-liquid collection Cup forms top and takes off liquid space between reactor NARE overhead-liquid collection cups and reactor NARE top shell；Conversion zone DRN 2 reactors processing at least coal-based carbon hydrogen material all the way；Reactor NBRE product is mixed into NARE after self-production material, in NARE Top takes off liquid space and carries out obtaining the collection liquid and other products that collection cups are discharged after at least partly de- liquid is completed in gas-liquid separation, until Few a part of collection liquid is after the pressurization of liquid material circulating pump to NARE, NBRE feeding cycle；The product NP of autoreactor NARE discharge Include reactor NARE product and reactor NBRE product, it is understood that there may be mainly by possible in the weight of autoreactor NARE discharge The liquid material product formed containing solid liquid material.

2. coal-based carbon hydrogen material hydrogenation process according to claim 1, it is characterised in that:

In DRN conversion zone, using 2 parallel coupled formula reactors NARE, NBRE, every reactor processing at least oil-containing coal all the way The material and/or hydrocarbonaceous liquid material of the material of slurries material and/or the liquid material of intermediate product containing coal liquefaction；The top reactor NBRE product is mixed into In NARE after self-production material, is taken off after liquid space completes at least partly de- liquid in NARE inner top and obtain the collection liquid of collection cups discharge With other products.

3. coal-based carbon hydrogen material hydrogenation process according to claim 1, it is characterised in that:

In DRN conversion zone, the de- liquid in part is completed in the overhead-liquid collection cups of NARE headspace arrangement and obtains collection liquid, until Few a part of collection liquid is through shared backward two reactors NARE, NBRE feeding cycle of liquid material circulating pump pressurization.

4. coal-based carbon hydrogen material hydrogenation process according to claim 1, it is characterised in that:

The coal-based carbon hydrogen material hydrogenator that coal-based carbon hydrogen material hydrogenation process RU, DRN conversion zone uses is up flow type reaction Device, mode of operation, a kind or several in following:

1. suspended-bed reactor；

2. fluidized bed reactor；

3. suspension bed and ebullated bed combined reactor；

4. up flow type expanded bed；

5. upflow fixed bed.

5. coal-based carbon hydrogen material hydrogenation process according to claim 1, it is characterised in that:

The coal-based carbon hydrogen material, a kind or several in following:

2. coal or coal liquefaction intermediate product liquid material carry out direct hydrogenation liquefaction of coal in coal-based carbon hydrogen material hydrogenation process RU Reaction；

3. reacting the distilled oil for generating oil based on direct hydrogenation liquefaction of coal, carry out adding hydrogen in coal-based carbon hydrogen material hydrogenation process RU Heat cracking reaction；

4. reacting the distilled oil for generating oil based on direct hydrogenation liquefaction of coal, carry out adding hydrogen in coal-based carbon hydrogen material hydrogenation process RU Stablize reaction, the hydrogen supply dissolvent oil that production direct hydrogenation liquefaction of coal reaction process needs.

6. coal-based carbon hydrogen material hydrogenation process according to claim 1, it is characterised in that:

Coal-based carbon hydrogen material is that the distilled oil for generating oil is reacted based on direct hydrogenation liquefaction of coal, in coal-based carbon hydrogen material hydrogenation reaction mistake Journey RU carries out stabilized hydrogenation and reacts to obtain the stabilized hydrogenation reaction product rich in hydrogen supply hydrocarbon, and production direct hydrogenation liquefaction of coal reacted The hydrogen supply dissolvent oil that journey needs；

Coal-based carbon hydrogen material hydrogenation process RU, the first conversion zone using 2 parallel coupled formula reactor groups at conversion zone, the 2 reactors processing at least coal-based carbon hydrogen material all the way of one conversion zone.

7. coal-based carbon hydrogen material hydrogenation process according to claim 6, it is characterised in that:

Normal boiling point in stabilized hydrogenation reaction product is higher than 250 DEG C of hydro carbons: the weight content of fractional saturation aromatic hydrocarbons is greater than 15%, Aromatic carbon rate is 0.35~0.70.

8. coal-based carbon hydrogen material hydrogenation process according to claim 6, it is characterised in that:

Normal boiling point in stabilized hydrogenation reaction product is higher than 250 DEG C of hydro carbons: the weight content of fractional saturation aromatic hydrocarbons is greater than 20%, Aromatic carbon rate is 0.40~0.65.

9. coal-based carbon hydrogen material hydrogenation process according to claim 6, it is characterised in that:

Coal-based carbon hydrogen material hydrogenation process RU, the hydrogenation catalyst used are the hydrogenation catalyst of Ni-Mo, Ni-Co or Ni-W system Agent；Reaction temperature is 300~390 DEG C, and hydrogenation pressure is 10~25MPa, and gas-liquid volume ratio is 300~1000NL/kg.

10. coal-based carbon hydrogen material hydrogenation process according to claim 1, it is characterised in that:

Coal-based carbon hydrogen material is coal or coal liquefaction intermediate product liquid material, carries out coal in coal-based carbon hydrogen material hydrogenation process RU and adds The reaction of hydrogen direct liquefaction；

In direct hydrogenation liquefaction of coal reaction system RU, there are hydrogen, conventional liquid hydrocarbon and there may be under conditions of catalyst, Coal or coal liquefaction intermediate product liquid material carry out at least part direct hydrogenation liquefaction of coal reaction RUR, and to be converted into coal hydrogenation direct Liquefaction reaction product RUP；Recycle reaction product RUP；

Direct hydrogenation liquefaction of coal reaction system RU includes at least one conversion zone, anti-with 2 parallel coupled formulas comprising at least one The conversion zone for answering device to form；

One conversion zone refers to the gas-liquid separation step comprising a Coal liquefaction step and the step gas-liquid product Technical process；

Direct hydrogenation liquefaction of coal reaction system RU it is any with 2 parallel coupled formula reactor groups at conversion zone be denoted as reaction Section DRN, using 2 parallel coupled formula reactor NARE, NBRE, 2 reactors processing of conversion zone DRN at least coal all the way Liquid material and/or coal liquefaction intermediate product liquid material, every reactor processing at least material and/or liquid containing coal of oil-containing coal slurry liquid material all the way The material and/or hydrocarbonaceous liquid material, reactor NARE, NBRE for changing intermediate product liquid material are up flow type expanded bed reactor；Reactor NBRE top product enters in reactor NARE mix with self-production material in NARE after enter the headspace of NARE, NARE is interior to be pushed up The overhead-liquid collection cups of portion's space layout complete the de- liquid in part and obtain collection liquid and other products, at least part collection liquid warp To NARE, NBRE feeding cycle after coal slurry recycle pump pressurization；The product NP of autoreactor NARE discharge is comprising reactor NARE The mixed material of product and reactor NBRE product, it is understood that there may be mainly by material containing solid-liquid in the weight of autoreactor NARE discharge The liquid material product of composition.

11. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

Direct hydrogenation liquefaction of coal reaction system RU, at least two conversion zone comprising liquid phase material serial operation, the first conversion zone are With 2 parallel coupled formula reactor groups at conversion zone, the flow model of direct hydrogenation liquefaction of coal reaction system RU, selected from following In a kind or several:

First conversion zone is the conversion zone formed with 2 parallel coupleds formula reactor 1ARE, 1BRE, and gassiness is discharged in the first conversion zone The product 1NTP of liquid phase；

The second conversion zone is set up, a up flow type expanded bed direct hydrogenation liquefaction of coal reactor 2ARE is used；First conversion zone Product 1NTP containing liquid phase enters the lower part reactor 2ARE as lower charging and flows up through main reaction region, is converted into reaction Reactor 2ARE is discharged in product 2ARE-RP；

First conversion zone is the conversion zone formed with 2 parallel coupleds formula reactor 1ARE, 1BRE, and gassiness is discharged in the first conversion zone The liquid material 1ALPA being mainly made of material containing solid-liquid on the product 1NTP and weight of liquid phase；

The second conversion zone is set up, using a up flow type expanded bed direct hydrogenation liquefaction of coal reactor 2ARE, the first conversion zone is produced Thing liquid material 1ALPA enters the lower part reactor 2ARE as lower charging and flows up through main reaction region, is converted into reaction product Reactor 2ARE is discharged in 2ARE-RP；

Meanwhile first the product 1NTP containing liquid phase of conversion zone enter the top reactor 2ARE as upper feeding, with reactor Material is mixed in 2ARE；

Reactor 2ARE, is arranged overhead-liquid collection cups, and collection liquid is recycled back into the lower part reaction compartment of reactor 2ARE；

First conversion zone is the conversion zone formed with 2 parallel coupleds formula reactor 1ARE, 1BRE, and gassiness is discharged in the first conversion zone The liquid material product 1ALPX being mainly made of material containing solid-liquid on the product 1NTP and weight of liquid phase；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is contained with the first conversion zone The product 1NTP of liquid phase is lower charging, and another reactor is with the first conversion zone liquid material product 1ALPX for lower charging；

In the 2nd conversion zone, reactor 2ARE, 2BRE are up flow type expanded bed reactor；Reactor 2BRE top product enters anti- Answer the headspace for entering 2ARE after mixing in device 2ARE with self-production material in 2ARE, the top liquid of 2ARE headspace arrangement The liquid material of body collection cups discharge, to 2ARE, 2BRE feeding cycle after coal slurry recycle pump pressurizes；The production of autoreactor 2ARE discharge Object 2TNP is the mixed material comprising reactor 2ARE product and reactor 2BRE product；

Recycle the second conversion zone reaction product；

First conversion zone is the conversion zone formed with 2 parallel coupleds formula reactor 1ARE, 1BRE, and gas-liquid is discharged in the first conversion zone It is mainly made of material containing solid-liquid on the liquid material product 1ALPX that is mainly made of material containing solid-liquid on phase product 1NTP, weight, weight Liquid material product 1ALPY；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first conversion zone gas Liquid product 1NTP is upper feeding, with the first conversion zone liquid material product 1ALPX is lower charging, and another reactor is with liquid material product 1ALPY is lower charging；

Recycle the second conversion zone reaction product；

First conversion zone is the conversion zone formed with 2 parallel coupleds formula reactor 1ARE, 1BRE, and gas-liquid is discharged in the first conversion zone The liquid material product 1ALPX being mainly made of material containing solid-liquid on phase product 1NTP, weight；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first conversion zone gas Liquid product 1NTP is lower charging, and another reactor is with the first conversion zone liquid material product 1ALPX for lower charging；Second conversion zone The liquid material product 2ALPX being mainly made of material containing solid-liquid on discharge liquid phase product 2NTP, weight；

Third conversion zone, using 2 parallel coupleds formula reactor 3ARE, 3BRE, wherein a reactor is with the second conversion zone gas Liquid product 2NTP is lower charging, and another reactor is with the second conversion zone liquid material product 2ALPB for lower charging；

Recycle third conversion zone reaction product；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first conversion zone gas Liquid product 1NTP is lower charging, and another reactor is with the first conversion zone liquid material product 1ALPX for lower charging；Second conversion zone Discharge liquid phase product 2NTP, the liquid material product 2ALPX being mainly made of material containing solid-liquid in weight, in weight mainly by containing solid-liquid Expect the liquid material product 2ALPY of composition；

Third conversion zone, using 2 parallel coupleds formula reactor 3ARE, 3BRE, wherein a reactor is with the second conversion zone gas Liquid product 2NTP is upper feeding, take the second conversion zone liquid material product 2ALPX as lower charging, and another reactor is with the second reaction Section liquid material product 2ALPY is lower charging；

Recycle third conversion zone reaction product；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first conversion zone gas Liquid product 1NTP is upper feeding, take the first conversion zone liquid material product 1ALPX as lower charging, and another reactor is with the first reaction Section liquid material product 1ALPY is lower charging；It is mainly made of material containing solid-liquid on second conversion zone discharge liquid phase product 2NTP, weight Liquid material product 2ALPX；

Third conversion zone, using 2 parallel coupleds formula reactor 3ARE, 3BRE, wherein a reactor is with the second conversion zone gas Liquid product 2NTP is lower charging, and another reactor is with the second conversion zone liquid material product 2ALPX for lower charging；

Recycle third conversion zone reaction product；

Second conversion zone, using 2 parallel coupleds formula reactor 2ARE, 2BRE, wherein a reactor is with the first conversion zone gas Liquid product 1NTP is upper feeding, take the first conversion zone liquid material product 1ALPX as lower charging, and another reactor is with the first reaction Section liquid material product 1ALPY is lower charging；It is mainly made of material containing solid-liquid on second conversion zone discharge liquid phase product 2NTP, weight Liquid material product 2ALPX, the liquid material product 2ALPY that is mainly made of material containing solid-liquid in weight；

Third conversion zone, using 2 parallel coupleds formula reactor 3ARE, 3BRE, wherein a reactor is with the second conversion zone gas Liquid product 2NTP is upper feeding, take the first conversion zone liquid material product 2ALPA as lower charging, and another reactor is with the second reaction Section liquid material product 2ALPY is lower charging；

Recycle third conversion zone reaction product；

9. direct hydrogenation liquefaction of coal reaction system RU, comprising 1 pre-hydrotreating reaction section 0PRE, one it is anti-with 2 parallel coupled formulas The first conversion zone for answering device to form and subsequent reactions section that may be present；

Coal liquefaction pre-hydrotreating reaction, which is carried out, in pre-hydrotreating reaction section 0PRE, coal slurry material F1 is converted into the production of coal liquefaction pre-hydrotreating reaction Object 0PRE-RP, at least part pre-hydrotreating reaction product 0PRE-RP enter the reaction of the first conversion zone as charging under reactor In device；

10. direct hydrogenation liquefaction of coal reaction system RU, comprising 1 pre-hydrotreating reaction section 0PRE, one it is anti-with 2 parallel coupled formulas The first conversion zone for answering device to form and subsequent reactions section that may be present；

Coal liquefaction pre-hydrotreating reaction, which is carried out, in pre-hydrotreating reaction section 0PRE, coal slurry material F1 is converted into the production of coal liquefaction pre-hydrotreating reaction Object 0PRE-RP obtains the liquid material product being mainly made of material containing solid-liquid in weight based on pre-hydrotreating reaction product 0PRE-RP 0PLPX, at least part liquid material product 0PLPX enter in the reactor of the first conversion zone as charging under reactor.

12. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In direct hydrogenation liquefaction of coal reaction system RU, it is any with 2 parallel coupled formula reactor groups at conversion zone be denoted as reaction Section DRN, using 2 parallel coupleds formula reactor NARE, NBRE, there are the discharges of autoreactor NARE inner top liquid collection cups The liquid material product being mainly made of material containing solid-liquid in weight.

13. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

Direct hydrogenation liquefaction of coal reaction system RU processes non-coal base weight oil while processing coal slurry raw material.

14. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In the conversion zone DRN of direct hydrogenation liquefaction of coal reaction system RU, using 2 parallel coupled formula reactor NARE, NBRE, one Platform reactor processing oil coal slurry liquid material and/or coal liquefaction intermediate product liquid material, another reactor process non-coal base weight oil or non-coal The hydro-conversion thing liquid material of base weight oil.

15. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

Direct hydrogenation liquefaction of coal reaction system RU processes non-coal base weight oil while processing coal slurry raw material；

It is shorter than direct hydrogenation liquefaction of coal in the hydrogenation reaction residence time of direct hydrogenation liquefaction of coal reaction system RU, non-coal base weight oil Reaction time.

16. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In the conversion zone DRN of direct hydrogenation liquefaction of coal reaction system RU, using 2 parallel coupled formula reactor NARE, NBRE, one Platform reactor processes the coal liquid material and/or coal liquefaction intermediate product liquid material that solid concentration is CA, and another reactor processing is solid The coal liquid material and/or coal liquefaction intermediate product liquid material, solid concentration CA and CB that bulk concentration is CB are identical or different.

17. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In direct hydrogenation liquefaction of coal reaction system RU, the conversion ratio of the moisture-and-ash-free basis component of feed coal is 70~98%.

18. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In direct hydrogenation liquefaction of coal reaction system RU, while processing coal slurry raw material, non-coal base weight oil, non-coal base weight oil are processed Heat from hydrogenation cracking reaction conversion ratio be 40~90%.

19. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In the conversion zone DRN of direct hydrogenation liquefaction of coal reaction system RU, using 2 parallel coupled formula reactor NARE, NBRE, one Platform reactor processes the coal liquid material and/or coal liquefaction intermediate product liquid material that solid concentration is CA, and another reactor processing is solid Bulk concentration is the coal liquid material and/or coal liquefaction intermediate product liquid material of CB, solid concentration be CA and the absolute difference of CB be 5~ 35%.

20. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In direct hydrogenation liquefaction of coal reaction system RU, the dilute coal slurry of simultaneous processing and thick coal slurry, the coal concentration C A of dilute coal slurry is 35~ 50%, the coal concentration C B of thick coal slurry is 50~70%.

21. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In direct hydrogenation liquefaction of coal reaction system RU, simultaneous processing dilute coal slurry F1 and thick coal slurry F2, the weight flow of thick coal slurry F2 The ratio of the weight flow F1-W of F2-W and dilute coal slurry F1 is slurry slurry than K100, K100=(F2-W)/(F1-W), K100 0.01 ~1.0.

22. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In direct hydrogenation liquefaction of coal reaction system RU, calculated with all feeding, the weight of the weight of hydrogen supply dissolvent DS and coal dust it Than being 0.5~2.0.

23. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In direct hydrogenation liquefaction of coal reaction system RU, the operating condition of the direct hydrogenation liquefaction of coal reaction process of coal dust experience are as follows: Reaction temperature is 400~485 DEG C, and reactor pressure is 6~30MPa, vapor phase hydrogen volumetric concentration 50~95%, gas-liquid volume ratio For 300~2500Nm³/ t, direct hydrogenation liquefaction of coal catalyst loading are 0.1~3 mass % of dry pulverized coal weight, co-catalysis Agent additive amount is that sulphur in co-catalyst/catalyst activity metal molar ratio is 1.0~2.0, and coal slurry solid concentration is 40~60 Quality %, reaction time are 0.5~4 hour.

24. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In direct hydrogenation liquefaction of coal reaction system RU, the direct hydrogenation liquefaction of coal catalyst used is that a kind of composite hydrogenation is urged Agent includes high-activity component and low activity component；The weight ratio of the high-activity component metal and low activity component metals is 1 : 10 to 10: 1；The high-activity component is or mixtures thereof the water soluble salt compound of molybdenum；The low activity group is divided into oxidation Iron ore or iron sulfide ore, wherein iron in ore content is not less than 40wt%, and direct hydrogenation liquefaction of coal catalyst water content is low In 2wt%；The powdered granule that the particle diameter of direct hydrogenation liquefaction of coal catalyst is 1~100 μm.

25. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

In direct hydrogenation liquefaction of coal reaction system RU, the direct hydrogenation liquefaction of coal catalyst used is a nanometer ultra-fine grain hydration Ferric oxide catalyst and/or iron oxide and/or pyrite and/or bloodstone and/or molybdenum oxide and/or molybdenum sulfide and/or ammonium molybdate and/or Nickel sulfide.

26. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

At least raw material contains hydrogen supply agent all the way in direct hydrogenation liquefaction of coal reaction system RU, the raw material of whole hydrocarbon containing liquids, institute It states hydrogen supply agent to be mainly made of the hydro carbons that normal boiling point is 250~530 DEG C, the weight content of fractional saturation aromatic hydrocarbons is big in hydrogen supply agent In 15%, aromatic carbon rate be 0.35~0.70.

27. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

At least raw material contains hydrogen supply agent all the way in direct hydrogenation liquefaction of coal reaction system RU, the raw material of whole hydrocarbon containing liquids, institute It states hydrogen supply agent to be mainly made of the hydro carbons that normal boiling point is 250~530 DEG C, the weight content of fractional saturation aromatic hydrocarbons is big in hydrogen supply agent In 25%, aromatic carbon rate be 0.45~0.60.

28. direct hydrogenation liquefaction of coal reaction system according to claim 10, it is characterised in that:

At least part solvent naphtha with slurry for including in direct hydrogenation liquefaction of coal reaction system RU, raw material coal slurry, selected from following 1 kind or several in material:

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

2. oil product logistics obtained by high temperature coal-tar or its distillate or its hot procedure；Hot procedure be selected from coking or Catalytic cracking process or catalytic pyrolysis process or hydrogenation process；

3. oil product obtained by the distillate oil of direct hydrogenation liquefaction of coal process product or its hot procedure；Hot procedure is selected from coking Process or catalytic cracking process or catalytic pyrolysis process or hydrogenation process；

4. oil product obtained by shale oil or its distillate or its hot procedure；Hot procedure is selected from coking or catalytic cracking Process or catalytic pyrolysis process or hydrogenation process；

6. oil product obtained by petroleum based heavy fuel oils hot procedure；Hot procedure is selected from coking or catalytic cracking process or catalysis Cracking process or hydrogenation process；