CN107118799A - DCL/Direct coal liquefaction circulation solvent and preparation method thereof - Google Patents
DCL/Direct coal liquefaction circulation solvent and preparation method thereof Download PDFInfo
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- CN107118799A CN107118799A CN201710264733.XA CN201710264733A CN107118799A CN 107118799 A CN107118799 A CN 107118799A CN 201710264733 A CN201710264733 A CN 201710264733A CN 107118799 A CN107118799 A CN 107118799A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/42—Hydrogen of special source or of special composition
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/44—Solvents
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of DCL/Direct coal liquefaction circulation solvent and preparation method thereof.Wherein, the preparation method comprises the following steps：1) hydrogenation reaction is carried out after coal direct liquefaction oil is mixed with hydrogen；2) by step 1) obtained hydrogenation products isolate hot gas separated by high pressure separator and hot high score oil through high pressure hot separator；3) by step 2) an obtained hot high score oil part is with coal direct liquefaction oil mixing Posterior circle hydrogenation, and the cold high score oil that another part and hot high score air cooling are obtained is mixed into fractionating column；4) fractionating column fractionation obtains that light fraction is oily, middle matter distillate and heavy distillate；5) matter distillate in heavy distillate and part is mixed to get DCL/Direct coal liquefaction circulation solvent.Apply the technical scheme of the present invention, DCL/Direct coal liquefaction is circulated to the hot high score oil in the part in solvent hydrogenation technique and carries out circulation hydrogenation, the reactive hydrogen quantity of heavy arene, improves circulation solvent hydrogen supply performance, improves the conversion ratio and liquefaction oil yield of coal in increase circulation solvent.
Description
Technical field
The present invention relates to direct coal liquefaction technology field, in particular to a kind of DCL/Direct coal liquefaction circulate solvent and its
Preparation method.
Background technology
DCL/Direct coal liquefaction is coal in high temperature, high pressure, face hydrogen, solvent and catalyst in the presence of, hydrogenation generation liquid production
The technical process of product.During DCL/Direct coal liquefaction, solvent has served highly important：Solvent is made into coal slurry with coal, is easy to
The conveying and pressurization of coal；Coal, the free radical fragment polycondensation for preventing pyrolysis of coal from producing can be dissolved, so as to improve liquefied coal coil receipts
Rate；Gas phase hydrogen can be dissolved, hydrogen molecule is spread to coal or catalyst surface；Can be to the direct hydrogen supply of free radical fragment or transmission
Hydrogen.Therefore DCL/Direct coal liquefaction solvent should have stronger solvability to the free radical fragment of pyrolysis of coal, while also possessing good
Hydrogen supply capacity.Solvent is directly the specific function of solvent in coal liquefaction, research discovery portion to the hydrogen supply of free radical fragment
Dividing the polycyclic aromatic hydrocarbon (such as naphthane, dihydro phenanthrene, dihydroanthracene, tetrahydrochysene anthracene) of hydrogenation has very strong hydrogen supply performance.Current real
In the direct coal liquefaction process of existing continuous run in long period, solvent comes from direct coal liquefaction process in itself, i.e. coal direct liquefaction oil
It is made, and is recycled during DCL/Direct coal liquefaction by stabilized hydrogenation, also referred to as circulates solvent.Improve solvent hydrogen supply energy
Power, can promote the conversion of coal, increase liquefied coal coil yield, prepare, convey and in heating furnace while also helping coal slurry
Flowing etc..Therefore, it is coal direct liquefaction skill further to improve the hydrogen supply performance of circulation solvent or the solvent of exploitation function admirable
One importance of art progress.
The content of the invention
The present invention is intended to provide a kind of DCL/Direct coal liquefaction circulation solvent and preparation method thereof, to improve DCL/Direct coal liquefaction circulation
The hydrogen supply performance of solvent.
To achieve these goals, according to an aspect of the invention, there is provided a kind of DCL/Direct coal liquefaction circulates solvent
Preparation method.The preparation method comprises the following steps：1) hydrogenation reaction is carried out after coal direct liquefaction oil is mixed with hydrogen；2) will
Step 1) obtained hydrogenation products isolate hot gas separated by high pressure separator and hot high score oil through high pressure hot separator；3) by step 2) obtained heat
A high score oil part is hydrogenated with coal direct liquefaction oil mixing Posterior circle, the cold high score oil that another part is obtained with hot high score air cooling
It is mixed into fractionating column；4) fractionating column fractionation obtains that light fraction is oily, middle matter distillate and heavy distillate；5) by heavy end
Oil is mixed to get DCL/Direct coal liquefaction circulation solvent with matter distillate in part.
Further, coal direct liquefaction oil is generated by coal by Direct Hydrogenation liquefaction during coal direct liquefaction,
For DCL/Direct coal liquefaction full distillate oil or more than 200 DEG C distillates；It is preferred that, the boiling range scope of coal direct liquefaction oil is 200~500
℃。
Further, step 1) in hydrogenation reaction temperature be 300~420 DEG C, reaction pressure be 8.0~20.0MPa, master
Agent cumulative volume air speed is 0.5~4.0h-1, hydrogen-oil ratio be 300~1500v/v, recycle ratio is 1:1~3:1.
Further, step 1) in hydrogenation reaction use catalyst be made up of active component and carrier, wherein, activearm
Be divided into the oxide of VIII race or/and VI race's metal in the periodic table of elements, the content of active component account for catalyst weight 5~
30%, carrier is unformed aluminum oxide or alumina silicate.
Further, active component is the one or more in Co, Mo, Ni, W metal oxide,
Further, step 3) in hot high score oil refer to>300 DEG C of cut；It is preferred that, hot high score oil refers to>320 DEG C
Cut.
Further, step 4) in, light fraction oil refers to<200 DEG C of cut, middle matter distillate refers to 200~350 DEG C
Cut, heavy end refers to>350 DEG C of cut.
Further, light fraction<220 DEG C, middle 230~350 DEG C of matter distillate.
Further, step 1) in, hydrogenation reaction is carried out in hydrogenation reactor, and hydrogenation reactor is ebullating bed reactor
One in device, paste state bed reactor, expanded bed reactor, or fluidized bed reactor, paste state bed reactor, expanded bed reactor
Plant the cascade reaction system constituted with fixed bed reactors.
According to another aspect of the present invention solvent is circulated there is provided a kind of DCL/Direct coal liquefaction.DCL/Direct coal liquefaction circulation is molten
Agent is prepared by any of the above-described kind of preparation method.
Apply the technical scheme of the present invention, DCL/Direct coal liquefaction is circulated to the hot high score oil in the part in solvent hydrogenation technique and carried out
The reactive hydrogen quantity of heavy arene, improves circulation solvent hydrogen supply performance, improves the conversion of coal in circulation hydrogenation, increase circulation solvent
Rate and liquefaction oil yield, so as to lift the economy of coal liquefaction technology.
Brief description of the drawings
The Figure of description for constituting the part of the application is used for providing a further understanding of the present invention, and of the invention shows
Meaning property embodiment and its illustrate be used for explain the present invention, do not constitute inappropriate limitation of the present invention.In the accompanying drawings：
Fig. 1 shows the schematic flow sheet of the preparation method of DCL/Direct coal liquefaction circulation solvent according to embodiments of the present invention.
Embodiment
It should be noted that in the case where not conflicting, the feature in embodiment and embodiment in the application can phase
Mutually combination.Describe the present invention in detail below with reference to the accompanying drawings and in conjunction with the embodiments.
According to a kind of typical embodiment of the present invention, there is provided the preparation method that a kind of DCL/Direct coal liquefaction circulates solvent.Should
Preparation method comprises the following steps：1) hydrogenation reaction is carried out after coal direct liquefaction oil is mixed with hydrogen；2) by step 1) obtain
Hydrogenation products through high pressure hot separator isolate hot gas separated by high pressure separator and hot high score oil；3) by step 2) obtained hot high score oil one
Point with coal direct liquefaction oil mixing Posterior circle hydrogenation, the cold high score oil that another part and hot high score air cooling are obtained is mixed into point
Evaporate tower；4) fractionating column fractionation obtains that light fraction is oily, middle matter distillate and heavy distillate；5) by heavy distillate and part
Matter distillate is mixed to get DCL/Direct coal liquefaction circulation solvent.
Solvent is directly the specific function of solvent in coal liquefaction to the hydrogen supply of free radical fragment, partially hydrogenated polycyclic
Aromatic hydrocarbons (such as naphthane, dihydro phenanthrene, dihydroanthracene, tetrahydrochysene anthracene) has very strong hydrogen supply performance, therefore circulation solvent is moderately hydrogenated with
Effect is best.The inventors found that the component in middle temperature solvent is in strong hydrogen supply state, hydrogenation can be because being hydrogenated with again
Cross reduction hydrogen supply performance；Component is in the not enough state of hydrogen supply in high-temperature solvent, and hydrogenation can make its hydrogen supply performance enhancement again, plus
Hydrogen is not enough or hydrogenation transition is all unfavorable for solvent hydrogen supply.Apply the technical scheme of the present invention, DCL/Direct coal liquefaction circulation solvent is added
The hot high score oil in part in hydrogen technique carries out the reactive hydrogen quantity of heavy arene in circulation hydrogenation, increase circulation solvent, and raising is followed
Ring solvent hydrogen supply performance, improves the conversion ratio and liquefaction oil yield of coal, so as to lift the economy of coal liquefaction technology.
It is preferred that, coal direct liquefaction oil is generated by coal by Direct Hydrogenation liquefaction during coal direct liquefaction, is
DCL/Direct coal liquefaction full distillate oil or more than 200 DEG C distillates；It is preferred that, the boiling range scope of coal direct liquefaction oil is 200~500
℃.Because during DCL/Direct coal liquefaction, solvent has served highly important, should possess good hydrogen supply performance, simultaneously
Also there are good ground solubility property, dispersive property and slurry performance.According to the similar principle mixed, structure in solvent is approximate with coal molecule
Polycyclic aromatic hydrocarbon have stronger solvability to the free radical fragment of pyrolysis of coal.Boiling range scope control ensure that molten in this scope
Performance of the agent in coal liquefaction, too heavy or too light performance can be affected.
It is preferred that, step 1) in hydrogenation reaction temperature be 300~420 DEG C, reaction pressure be 8.0~20.0MPa, host
Cumulative volume air speed is 0.5~4.0h-1, hydrogen-oil ratio be 300~1500v/v, recycle ratio (recycle oil：Feedstock oil mass ratio) it is 1:1
~3:1.Solvent needed for coal direct liquefaction oil can be processed at this point in the reaction during DCL/Direct coal liquefaction.According to this hair
A kind of bright typical embodiment, step 1) in the catalyst that uses of hydrogenation reaction be made up of active component and carrier, wherein, it is living
Property component be VIII race or/and VI race's metal in the periodic table of elements oxide, the content of active component account for catalyst weight 5~
30%, carrier is unformed aluminum oxide or alumina silicate.It is preferred that, active component is one kind in Co, Mo, Ni, W metal oxide
Or it is a variety of.
It is preferred that, step 3) in hot high score oil refer to>300 DEG C of cut；It is preferred that, hot high score oil refers to>320 DEG C evaporate
Point.Cut in the range of this is exactly to circulate the fraction section that deficiency is hydrogenated with solvent.
It is preferred that, step 4) in, light fraction oil refers to<200 DEG C of cut, middle matter distillate refers to 200~350 DEG C
Cut, heavy end refers to>350 DEG C of cut.Boiling range scope control purpose is to serve subsequent process flow herein, and lightweight evaporates
Matter distillate in oil and part is divided to be evaporated for carrying out matter distillate and whole heavys in Deep Hydrotreating production petrol and diesel oil, part
Divide oil to be used for coal liquefaction unit and circulate solvent, facilitate industrialized production.
It is preferred that, light fraction<220 DEG C, middle 230~350 DEG C of matter distillate.
According to a kind of typical embodiment of the present invention, step 1) in, hydrogenation reaction is carried out in hydrogenation reactor, hydrogenation
Reactor be fluidized bed reactor, paste state bed reactor, expanded bed reactor, or fluidized bed reactor, paste state bed reactor,
A kind of cascade reaction system of and fixed bed reactors composition in expanded bed reactor.
Solvent is circulated there is provided a kind of DCL/Direct coal liquefaction according to a kind of typical embodiment of the present invention.The DCL/Direct coal liquefaction
Circulation solvent is prepared by any of the above-described kind of preparation method.
Beneficial effects of the present invention are further illustrated below in conjunction with embodiment.
Embodiment
As shown in figure 1, the coal direct liquefaction oil in head tank 10 enters heating furnace 20 after raw material pump and hydrogen back-mixing, plus
Material after heat, which enters, carries out stabilized hydrogenation reaction in hydrogenation reactor 30, the material that the top of hydrogenation reactor 30 comes out is through hot high
Pressure separator 40 is separated into hot gas separated by high pressure separator and hot high score oil, and hot gas separated by high pressure separator isolates cold gas separated by high pressure separator after entering cold high pressure separator 60
With cold high score oil, the effluent that the bottom of high pressure hot separator 40 is isolated point two-way, all the way into recycle oil collecting tank 50, through following
Ring oil pump is mixed into hydrogenation reactor 30 with feedstock oil and circulated；Another Lu Yuleng high scores oil together enters fractionating column 70,
Be fractionated into the light fraction oil that tower 70 isolates mix with matter distillate in part together entrance downstream unit for processing fuel
Product (such as automobile-used petrol and diesel oil), it is that coal is direct to be fractionated into matter distillate and heavy distillate mixing in the part that tower 70 is isolated
Liquefied circulating solvent.
In order to further verify processing method provided by the present invention, using coal direct liquefaction oil as raw material, in 300ml expansions
Tested on bed hydroprocessing device using Hydrobon catalyst, further illustrate having for the present invention with comparative example in conjunction with the embodiments
Beneficial effect.
In the present invention, PDQI is hydrogen supply index, represents the hydrogen supply capacity of solvent, refers to be located at cycloalkanes on cycloalkyl aromatic hydrocarbons
The ratio between quality and solvent quality of β hydrogen atoms of base, i.e., be located at β hydrogen of cycloalkyl on cycloalkyl aromatic hydrocarbons former in every gram hydrogen supply dissolvent
The milligram number of son.
Embodiment 1-3 prepares circulation solvent according to technological process shown in Fig. 1, and table 1 shows DCL/Direct coal liquefaction oil nature, table
2 show the hydrogenation catalyst and hydrogenation catalyst performance used in embodiment 1-3 and comparative example 1-3, and table 3 gives embodiment
1-3 and comparative example 1-3 hydrogenation process conditions, table 4 show embodiment 1-3 and comparative example 1-3 circulation solvent property.
Comparative example be using coal direct liquefaction oil listed by table 1 as raw material, using with embodiment identical experimental rig, catalysis
The hydropyrolysis experiment that agent, experimental condition are carried out.
The raw material oil nature of table 1
The Hydrobon catalyst property of table 2
The hydropyrolysis experiment process conditions of table 3
Table 4 circulates solvent property
By embodiment 1 in table 4 and comparative example 1, embodiment 2 and comparative example 2, embodiment 3 and comparative example 3 contrast can be with
Find out, the monocyclic and two ring aromatic content increase of present invention circulation solvent, hydrogen supply index is improved, the hot high score oil of declaratives
Circulation carries out secondary or multiple hydrogenation so that wherein heavy arene reactive hydrogen quantity increase, so as to reach that raising circulation solvent is supplied
The purpose of hydrogen performance.
As can be seen from the above description, the above embodiments of the present invention realize following technique effect：
(1) DCL/Direct coal liquefaction can be circulated to heavy constituent in solvent oily (i.e.>300 DEG C of distillates) by circulation realize it is secondary
Or be repeatedly hydrogenated with, promote reactive hydrogen quantity in the further hydrogenation of heavy arene in heavy constituent oil, increase heavy constituent oil, raising is followed
The hydrogen supply performance of ring solvent, promotes the conversion of coal, improves DCL/Direct coal liquefaction oil yield.
(2) it is the achievable multiple hydrogenation for circulating heavy constituent aromatic hydrocarbons in solvent using existing apparatus reaction member, improves dress
Put utilization rate.
(3) solvent processing unit (plant) can be circulated by existing DCL/Direct coal liquefaction and directly transforms realization, reforming technology is simple, changes
Cause low, it is easy to lift direct coal liquefaction technology economy.
The preferred embodiments of the present invention are the foregoing is only, are not intended to limit the invention, for the skill of this area
For art personnel, the present invention can have various modifications and variations.Within the spirit and principles of the invention, that is made any repaiies
Change, equivalent substitution, improvement etc., should be included in the scope of the protection.
Claims (10)
1. a kind of DCL/Direct coal liquefaction circulates the preparation method of solvent, it is characterised in that comprise the following steps：
1) hydrogenation reaction is carried out after coal direct liquefaction oil is mixed with hydrogen；
2) by step 1) obtained hydrogenation products isolate hot gas separated by high pressure separator and hot high score oil through high pressure hot separator；
3) by step 2) the obtained hot high score oil part and coal direct liquefaction oil mixing Posterior circle hydrogenation, another part and
The cold high score oil that the hot high score air cooling is obtained is mixed into fractionating column；
4) fractionating column fractionation obtains that light fraction is oily, middle matter distillate and heavy distillate；
5) heavy distillate and the part middle matter distillate are mixed to get the DCL/Direct coal liquefaction and circulate solvent.
2. preparation method according to claim 1, it is characterised in that the coal direct liquefaction oil is coal direct liquefaction mistake
Generated in journey by coal by Direct Hydrogenation liquefaction, be DCL/Direct coal liquefaction full distillate oil or more than 200 DEG C distillates；It is preferred that,
The boiling range scope of the coal direct liquefaction oil is 200~500 DEG C.
3. preparation method according to claim 1, it is characterised in that step 1) described in the temperature of hydrogenation reaction be 300
~420 DEG C, reaction pressure be that 8.0~20.0MPa, host cumulative volume air speed are 0.5~4.0h-1, hydrogen-oil ratio be 300~1500v/
V, recycle ratio is 1:1~3:1.
4. preparation method according to claim 1, it is characterised in that step 1) described in the catalyst that uses of hydrogenation reaction
It is made up of active component and carrier, wherein, the active component is the oxidation of VIII race or/and VI race's metal in the periodic table of elements
Thing, the content of the active component accounts for the 5~30% of the catalyst weight, and the carrier is unformed aluminum oxide or silicic acid
Aluminium.
5. preparation method according to claim 4, it is characterised in that the active component aoxidizes for Co, Mo, Ni, W metal
One or more in thing.
6. preparation method according to claim 1, it is characterised in that step 3) described in hot high score oil refer to>300 DEG C
Cut；It is preferred that, hot high score oil refers to>320 DEG C of cut.
7. preparation method according to claim 1, it is characterised in that step 4) in, the light fraction oil refers to<200
DEG C cut, the middle matter distillate refers to 200~350 DEG C of cut, and the heavy end refers to>350 DEG C of cut.
8. preparation method according to claim 7, it is characterised in that the light fraction<220 DEG C, the middle matter cut
230~350 DEG C of oil.
9. preparation method according to claim 1, it is characterised in that step 1) in, the hydrogenation reaction is in hydrogenation reaction
Carried out in device, the hydrogenation reactor is fluidized bed reactor, paste state bed reactor, expanded bed reactor, or ebullated bed is anti-
The cascade reaction system for answering a kind of and fixed bed reactors in device, paste state bed reactor, expanded bed reactor to constitute.
10. a kind of DCL/Direct coal liquefaction circulates solvent, it is characterised in that as the preparation method any one of claim 1 to 9
Prepare.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108977223A (en) * | 2018-07-25 | 2018-12-11 | 国家能源投资集团有限责任公司 | The preparation method and system of coal liquefaction circulation solvent |
| CN112175651A (en) * | 2019-07-04 | 2021-01-05 | 南京延长反应技术研究院有限公司 | Preparation system and method of coal direct liquefaction circulating solvent |
| CN115491221A (en) * | 2022-10-09 | 2022-12-20 | 国家能源集团宁夏煤业有限责任公司 | Solvent for coal hydrogenation liquefaction and coal hydrogenation liquefaction method |
| CN116162481A (en) * | 2023-01-09 | 2023-05-26 | 中国神华煤制油化工有限公司 | Direct coal liquefaction circulating hydrogen supply solvent and preparation method and application thereof |
| CN116218560A (en) * | 2023-01-10 | 2023-06-06 | 孙少哲 | Coal hydrogenation upgrading method |
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| CN116162481A (en) * | 2023-01-09 | 2023-05-26 | 中国神华煤制油化工有限公司 | Direct coal liquefaction circulating hydrogen supply solvent and preparation method and application thereof |
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