CN106906001A - The coal of inertinite content high and the method for mink cell focus coprocessing - Google Patents
The coal of inertinite content high and the method for mink cell focus coprocessing Download PDFInfo
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- CN106906001A CN106906001A CN201710280841.6A CN201710280841A CN106906001A CN 106906001 A CN106906001 A CN 106906001A CN 201710280841 A CN201710280841 A CN 201710280841A CN 106906001 A CN106906001 A CN 106906001A
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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
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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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
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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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention is a kind of method on coal of inertinite content high Yu mink cell focus coprocessing, and it includes：Mink cell focus, first are not hydrogenated with circulation solvent and catalyst mixes, slurry oil is obtained, hydrocracking obtains the first product, separates, obtain the first light fraction oil and the first heavy distillate；First heavy distillate, second are not hydrogenated with circulation solvent and coal dust mixes, be made coal, hydrocracking obtains the second product, separates, obtain the second light fraction oil and the second heavy distillate；A part of isolated residue of second heavy distillate and the 3rd heavy distillate, wherein the 3rd heavy distillate is not hydrogenated with circulation solvent as first, for preparing slurry oil；Another part is not hydrogenated with circulation solvent as second, for preparing coal；First light fraction oil is carried out into hydrogenation upgrading with the second light fraction oil, third product is obtained, separated, obtain naphtha, aviation kerosine and diesel oil.The present invention improves the conversion ratio of inertinite content coal higher, increased the yield of fluid product.
Description
Technical field
The present invention relates to a kind of coal of inertinite content high and the method for mink cell focus coprocessing, specifically, the present invention is logical
Crossing mink cell focus pretreatment reduces its viscosity, its hydrogen supply is improved, then with the coal coprocessing of inertinite content high, so as to realize height
The purpose of the maximized production clear gusoline of coal and mink cell focus of inertinite content.
Background technology
2015, Chinese crude oil processing capacity reached 5.22 hundred million tons, and net importation amount is 3.34 hundred million tons, crude oil external dependence degree
Up to 64%, it is contemplated that be up to 500,000,000 tons to the year two thousand twenty crude oil import amount, imbalance between supply and demand sharply seriously threatens national energy security.
And China possesses abundant low-disintegration coal charcoal resource, these low-disintegration coal reactivities are high, can be with by direct coal liquefaction technology
Fuel for cleaning vehicle is converted coal into, is the important channel for effectively alleviating China's oil imbalance between supply and demand, at present, except China
Outward, the U.S., Germany, Japan etc. all develop respective direct coal liquefaction technology.But it is molten easily to there is circulation in direct coal liquefaction technology
The problem of agent oil shortage, once shortage occurs in solvent naphtha, then needs the extraction section heavy constituent oil from diesel oil distillate whole to ensure
The stable operation of individual device, so as to reduce the yield of product oil, and circulation solvent by after repeatedly circulation, easily there is lightweight
Change phenomenon, solvent lighting easily causes coal dust sedimentation and its hydrogen supply hydraulic performance decline, so that blocking pipeline and reactor, influence is entirely
The stable operation of device.
In order to improve or eliminating the problem of solvent naphtha shortage in direct coal liquefaction technology, product oil yield is improved, it is straight in coal
Connect it is liquefied on the basis of, researcher attempts circulation solvent mink cell focus (such as heavy crude, the slag for needing DCL/Direct coal liquefaction
Oil, catalytic cracked oil pulp, coal tar etc.) substitute, it is all or part of to cancel circulation solvent, and achieve good effect.With coal
Direct liquefaction technology is compared, and the technology of refining has the advantages of oily yield is high, hydrogen consumption is low, hydrogen utilization rate is high to kerosene altogether.And kerosene is common
Refining technology can also make light materialization of heavy oil while coal liquefaction is made, therefore, increasingly paid attention to by researcher.The U.S., moral
State, Canada, Japan, China etc. develop various kerosene and refine technology altogether in succession.Come from presently disclosed coal-residual coprocessing technique
See, kerosene can altogether be refined and be divided into two major classes：The first kind is the common sweetening process of kerosene that one way passes through, and the distinguishing feature of the technique is
Solvent need not be circulated during coal-residual coprocessing；Equations of The Second Kind is the common sweetening process of kerosene for circulating freshening, and the distinguishing feature of the technique is
Still need to circulate solvent during coal-residual coprocessing.
Although sweetening process technology realizes the common processing of coal and mink cell focus to above-mentioned kerosene altogether, but coal property and mink cell focus
Property on coal-residual coprocessing result influence it is larger：First, refining coal typically chooses the lignite of age and the cigarette of youth to kerosene altogether
Coal (including jet coal, weakly caking coal, dross coal and part bottle coal), the conversion ratio when conversion ratio of general lignite is with DCL/Direct coal liquefaction
It is basically identical, but bituminous coal conversion ratio can decrease, the especially bituminous coal of inertinite content (15%-45%) higher, wherein not
The coal of conversion is eventually gathered in liquefied residue, increases liquefied residue yield, and this is that we are undesirable.Second, weight
The property of matter oil directly affects the property for being made into coal.In independent DCL/Direct coal liquefaction, typically require that the viscosity of coal exists
50-500mPa.s (80 DEG C), and the viscosity of residual oil itself is high, when preparing coal with the mink cell focus of this big viscosity, on the one hand
The mix ratio of coal dust in coal can be greatly lowered, be typically only capable to control the content of coal dust in coal in 30%-
40%, so as to reduce the ability that coal liquification device processes coal, reduce utilization rate of equipment and installations；On the other hand oily coal can be greatly improved
The viscosity of slurry, this high-viscosity coal is unfavorable for the conveying of pump, and heat transfer and mass transfer effect are poor.3rd, mink cell focus
Hydrogen supply capacity can directly affect lique faction of coal effect.During coal-residual coprocessing, mink cell focus splits except itself there is hydrogenation
Change reaction outer, in addition it is also necessary to for coal liquefaction is provided and transfer activity hydrogen, research finds that part hydrogenation of aromatics and cycloalkane have hydrogen supply energy
Power, and alkane does not have hydrogen supply capacity, therefore, in order to ensure the effect of coal-residual coprocessing, the current common sweetening process of above-mentioned kerosene
Petroleum residual oil used be both selected from greatly the residual oil of aromatic hydrocarbons and naphthene content naphthene base crude higher, in m- naphthene base crude
Residual oil and its mixture, and the residual oil of paraffinic base crude oil is then generally precluded from outside.Actually by the slag with paraffinic base crude oil
Oil contains substantial amounts of alkane, if it carries out common processing with coal, the Cetane number of the diesel oil for obtaining can be higher.
How the viscosity of mink cell focus is reduced so that reaction system processes coal and mink cell focus to greatest extent, and contains inertinite
Amount coal higher keeps conversion ratio higher, so as to expand inertinite content coal higher and paraffinicity mink cell focus higher
The scope of application, improve product diesel oil Cetane number, be those skilled in the art's problem demanding prompt solution.In the prior art,
Mainly pre-processed by thermal cracking to reduce the viscosity of mink cell focus, but thermal cracking temperature is higher, typically in 450-480
DEG C, easily there is coking phenomenon in mink cell focus, makes overall oil yield reduction, and be not directed to how to improve the hydrogen supply energy of mink cell focus
Power.Therefore, it is necessary to develop a kind of new kerosene sweetening process altogether, inertinite content coal higher can either be made to keep higher
Conversion ratio, and have good adaptability to various mink cell focuses such that it is able to production fuel oil as much as possible.
The content of the invention
It is a primary object of the present invention to, there is provided the side of a kind of coal of new inertinite content high and mink cell focus coprocessing
Method, technical problem to be solved is the conversion ratio for making it improve inertinite content coal higher, increases the yield of fluid product,
Thus more suitable for practicality.
The object of the invention to solve the technical problems is realized using following technical scheme.Proposed according to the present invention
Inertinite content a kind of high coal and mink cell focus coprocessing method, it includes：
1) mink cell focus, first are not hydrogenated with circulation solvent and catalyst mixes, slurry oil is obtained；Described slurry oil is carried out
First hydrocracking is reacted, and obtains the first product；The first described product is separated, the first light fraction oil and the first weight is obtained
Matter distillate；
2) the first described heavy distillate, second are not hydrogenated with circulation solvent and coal dust mixes, be made coal, will
Described coal carries out the second hydrocracking reaction, obtains the second product, and the second described product is separated, and obtains
Two lightweight distillates and the second heavy distillate；
3) the second heavy distillate described in is divided into two parts, a part of isolated residue and the 3rd heavy distillate,
The 3rd wherein described heavy distillate is not hydrogenated with circulation solvent as first, for preparing slurry oil；Another part is used as second
Circulation solvent is not hydrogenated with, for preparing coal；
4) the 3rd hydrogenation upgrading is carried out with the second described light fraction oil by described first light fraction is oily, obtain the
Three products, described third product is separated, and obtains naphtha, aviation kerosine and diesel oil.
The object of the invention to solve the technical problems can also be applied to the following technical measures to achieve further.
Preferably, the method for the coal of foregoing inertinite content high and mink cell focus coprocessing, wherein described coal tar bag
Include the heavy distillate after coalite tar, high temperature coal-tar and its processing；
The low value-added product oil of the petroleum refining is catalytic cracked oil pulp, residual oil, solvent extraction are obtained aromatic hydrocarbons, ethene
At least one in pyrolysis fuel oil.
Preferably, the method for the coal of foregoing inertinite content high and mink cell focus coprocessing, wherein described catalyst
Metal active constituent is at least one in Fe, Ni, Co, Mo, Ti, W；The quality of the active component of the catalyst is mink cell focus
0.002-2%；It is 1 that described first is not hydrogenated with circulation solvent with the mass ratio of mink cell focus：10-6：4.
Preferably, the method for the coal of foregoing inertinite content high and mink cell focus coprocessing, wherein the first described hydrogenation
The reaction temperature of cracking reaction is 370-430 DEG C, and hydrogen dividing potential drop is 12-20MPa, and gas liquid ratio is 400-1500, and air speed is 0.5-
1.5h-1；
The reaction temperature of the second hydrocracking reaction is 430-470 DEG C, and hydrogen dividing potential drop is 15-22MPa, and gas liquid ratio is
600-1800, air speed is 0.3-0.8h-1；
The reaction temperature of the 3rd described hydrogenation upgrading is 320-420 DEG C.Hydrogen dividing potential drop is 10-20MPa, and air speed is 0.5-
4.0h-1。
Preferably, the method for the coal of foregoing inertinite content high and mink cell focus coprocessing, wherein the first described product
Separated by high-temperature separator and cold catch pot, the separation temperature of described high-temperature separator is 250-370 DEG C, described
The separation temperature of cold catch pot is room temperature；
The second described product is separated by high-temperature separator and cold catch pot；
Described residue and the 3rd heavy distillate are separated by vacuum distillation.
Preferably, the method for the coal of foregoing inertinite content high and mink cell focus coprocessing, wherein the first described lightweight
Distillate boiling range is that the end point of distillation is less than 370 DEG C, and the cutting temperature of the first heavy distillate is more than 350 DEG C；
Described the second light fraction oil boiling range is that the end point of distillation is less than 370 DEG C, and the cutting temperature of the second heavy distillate is big
In 350 DEG C；
The separation of described the 3rd mink cell focus and residue realizes that the end point of distillation of the 3rd mink cell focus is less than by vacuum distillation
Equal to 520 DEG C.
Preferably, the method for the coal of foregoing inertinite content high and mink cell focus coprocessing, wherein in described coal
The weight/mass percentage composition of coal dust is 40-50%, and the particle diameter of described coal dust is less than 0.3mm, and moisture is less than or equal to 4.0%.
Preferably, the method for the coal of foregoing inertinite content high and mink cell focus coprocessing, wherein described second does not add
The mass ratio that hydrogen circulation solvent is accounted in the second heavy distillate is 50-90%.
By above-mentioned technical proposal, under the coal of inertinite content high of the invention at least has with the method for mink cell focus coprocessing
Row advantage：
(1) mink cell focus of the invention considerably reduces the viscosity of mink cell focus by pre-hydrotreating, can guarantee that and is prepared
The concentration of coal is obtained more than 40%, the working ability of Direct coal liquefaction device is had substantially no effect on；
(2) mink cell focus of the present invention and first is not hydrogenated with circulation solvent by pre- hydrogenation, the aromatic hydrocarbons in system is changed into part
Hydrogenation of aromatics, improves hydrogen supply capacity, and the light oil higher containing alkane in product is separated, only more multiple with aromatic hydrocarbons is rich in
Matter distillate further increases its hydrogen supply capacity as the solvent naphtha for preparing coal；
(3) the solvent naphtha boiling point that the present invention prepares coal is higher than 350 DEG C, improves the high temperatures of solvent naphtha or coal
Can, it also avoid the secondary cracking of the light fraction oil of liquefaction generation；
(4) scope of application of mink cell focus is expanded, it is particularly possible to the residual oil for processing paraffinic base crude oil；Improve lazy matter
The conversion ratio of group content coal higher can make the yield of fluid product can reach more than 70% to 90-93%, compare existing method
Improve 1-15 percentage points.
Described above is only the general introduction of technical solution of the present invention, in order to better understand technological means of the invention,
And can be practiced according to the content of specification, below with presently preferred embodiments of the present invention and coordinate accompanying drawing describe in detail as after.
Brief description of the drawings
Fig. 1 is the process chart of the coal with the method for mink cell focus coprocessing of inertinite content high of the invention；
Fig. 2 is the process chart of comparative example 1.
Specific embodiment
Further to illustrate the present invention to reach technological means and effect that predetermined goal of the invention is taken, below in conjunction with
Accompanying drawing and preferred embodiment, to the method for the coal according to inertinite content high proposed by the present invention and mink cell focus coprocessing, its is specific
Implementation method, structure, feature and its effect, describe in detail as after.In the following description, different " embodiment " or " implementation
What example " referred to is not necessarily same embodiment.Additionally, the special characteristic, structure or feature in one or more embodiments can be by any
Suitable form is combined.
The coal of the inertinite content a kind of high that one embodiment of the present of invention is proposed and the method for mink cell focus coprocessing, its bag
Include：
1) mink cell focus, first are not hydrogenated with circulation solvent and catalyst mixes, slurry oil is obtained；Described slurry oil is carried out
First hydrocracking is reacted, and obtains the first product；The first described product is separated, the first light fraction oil and the first weight is obtained
Matter distillate；
2) the first described heavy distillate, second are not hydrogenated with circulation solvent and coal dust mixes, be made coal, will
Described coal carries out the second hydrocracking reaction, obtains the second product, and the second described product is separated, and obtains
Two lightweight distillates and the second heavy distillate；
3) the second heavy distillate described in is divided into two parts, a part of isolated residue and the 3rd heavy distillate,
The 3rd wherein described heavy distillate is not hydrogenated with circulation solvent as first, for preparing slurry oil；Another part is used as second
Circulation solvent is not hydrogenated with, for preparing coal；
4) the 3rd hydrogenation upgrading is carried out with the second described light fraction oil by described first light fraction is oily, obtain the
Three products, described third product is separated, and obtains naphtha, aviation kerosine and diesel oil.
Wherein, mink cell focus can select the low value-added product after low-quality crude oil and PETROLEUM PROCESSING such as：Catalytic cracking
Aromatic hydrocarbons, ethylene cracking tar that slurry oil, residual oil, solvent extraction are obtained etc., it is also an option that middle coalite tar, high temperature coal-tar
And its one or more in the heavy distillate after processing；The metal active constituent of catalyst can be Fe, Ni, Co, Mo, Ti and
One or more in the transition metal such as W；The addition of catalyst determines as the case may be in slurry oil, its active component with
The accounting of mink cell focus is 0.002-2%, and it is 1 not to be hydrogenated with circulation solvent with the mixing proportion of mink cell focus:10-6:4.
What the first hydrocracking was reacted can be carried out in 1 or 2 slurry bed systems or bubbling bed reactor, and reaction temperature is
370-430 DEG C, hydrogen dividing potential drop is 12-20MPa, and gas liquid ratio is 400-1500, and air speed is 0.5-1.5h-1。
The separation of the first product is combined by one or more high-temperature separators and cold catch pot and realized, its high temperature point
It it is 300-370 DEG C from the separation temperature of device, the separation temperature of cold catch pot is room temperature；Isolated the first light fraction oil
Boiling range is that the end point of distillation is less than 370 DEG C, and the first heavy distillate boiling range is more than 350 DEG C.
Coal particle size is less than 0.3mm, and moisture is no more than 4.0%, and coal dust content is 40-50% in coal, because of the
Contain catalyst in one heavy distillate and the second heavy distillate, therefore without additionally addition catalysis in the slurry oil for preparing
Agent.
Second hydrocracking reaction is carried out in two or more up flow type paste state bed reactors, and reaction temperature is 430-
470 DEG C, hydrogen dividing potential drop is 15-22MPa, and gas liquid ratio is 600-1800, and air speed is 0.3-0.8h-1。
The separation of the second product realizes that second for obtaining is light by one or more high-temperature separators and cold catch pot
Matter distillate is distillate of the end point of distillation less than 370 DEG C, and the boiling range of the second heavy distillate is more than 350 DEG C of distillate.
For preparing coal slurry second not to be hydrogenated with the mass ratio that accounts in the second heavy distillate of circulation solvent be 50%-
90%；The separation of the 3rd heavy distillate and residue realizes that the end point of distillation of the 3rd mink cell focus is no more than 520 by vacuum distillation
℃。
3rd hydrogenation upgrading reaction is carried out in fixed bed reactors, uses hydrofinishing agent Cracking catalyst, hydrogen dividing potential drop
It is 10-20MPa, reaction temperature is 320-420 DEG C, and air speed is 0.5-4.0h-1。
Process chart of the invention is as shown in Figure 1.The coal of present invention inertinite content high and the side of mink cell focus coprocessing
The device that method is used refines device, solvent oil circulation device and oil product upgrading processing dress altogether including slurry oil pretreatment unit, kerosene
Put, wherein, slurry oil pretreatment unit includes：Slurry oil tank 1, preheater 2, reactor 3, high-temperature separator 4, cold catch pot 5；Coal
Refining device includes oil altogether：Coal tank 6, hydrogen preheater 7, coal preheater 8, paste state bed reactor 9, high-temperature separator
10, cold catch pot 11, vacuum distillation tower 12；Oil product upgrading processing unit (plant) includes：Fixed bed reactors 13, separator 14 steams
Evaporate tower 15, the order of connection that above-mentioned kerosene refines device altogether is followed successively by slurry oil pretreatment unit, kerosene and refines device and oil product upgrading altogether
Processing unit (plant), the two ends of described solvent oil circulation device connect the vacuum distillation during slurry oil tank 1 and kerosene refine device altogether respectively
Tower 12.
Embodiment 1
The property of the decompression residuum in the present embodiment is shown in Table 1；The coal component of the inertinite content high in the present embodiment is new
The para bituminous coal in boundary area, its property is shown in Table 2.
The coal of the inertinite content a kind of high that one embodiment of the present of invention is proposed and the method for mink cell focus coprocessing, its bag
Include：
(1) decompression residuum of table 1 and first circulation solvent is not hydrogenated with by 7:3 ratios are made slurry oil, are urged in oil-soluble Mo
In the presence of agent, the first pre-hydrotreating reaction is carried out under the conditions of 400 DEG C of temperature, pressure 17MPa, gas liquid ratio 1000, obtain first
Light fraction oil and the first heavy distillate, the addition of Mo catalyst is the 0.03% of decompression residuum weight；
(2) the bituminous coal A and second in the first heavy distillate and table 2 circulation solvent is not hydrogenated with by 0.5:1:1 ratio
Coal is made, the second hydrocracking reaction is carried out under the conditions of 450 DEG C of temperature, pressure 19MPa, gas liquid ratio 1500, obtain
Two lightweight distillates and the second heavy distillate；
(3) the 60% the second heavy distillates are not hydrogenated with circulation solvent as second and return to step (2) with liquefaction coal
Slurry, another 40% the second heavy distillate after vacuum distillation removing residue by obtaining the 3rd heavy distillate, the 3rd heavy end
Oil is not hydrogenated with circulation solvent whole return to step (1) and prepares slurry oil as first；
(4) first light fractions oil is with the second light fraction oil by weight 1:The 3rd hydrogenation upgrading is carried out after 5 mixing anti-
Should, reaction temperature is 370 DEG C, and pressure 15MPa obtains liquid fuel A, and experimental result and liquid fuel A properties are shown in Table 3.
Embodiment 2
High temperature coal-tar component and property in the present embodiment are shown in Table 1；The coal group of the inertinite content high in the present embodiment
It is divided into the para bituminous coal of Xinjiang region, its property is shown in Table 2.
The coal of the inertinite content a kind of high that one embodiment of the present of invention is proposed and the method for mink cell focus coprocessing, its bag
Include：
(1) the high temperature coal tar of table 1 and first circulation solvent is not hydrogenated with by 9：1 ratio is made slurry oil, in oil-soluble Mo
In the presence of catalyst, the first pre-hydrotreating reaction is carried out under the conditions of 390 DEG C of temperature, pressure 17MPa, gas liquid ratio 1000, obtain
One light fraction oil and the first heavy distillate, the addition of Mo catalyst is the 0.02% of slurry oil weight；
(2) the first heavy distillate and the metabituminous coal B of table 2 and second circulation solvent is not hydrogenated with by 0.7:1:0.8 ratio
Coal is made, the second hydrocracking reaction is carried out under the conditions of 450 DEG C of temperature, pressure 19MPa, gas liquid ratio 1500, obtain
Two lightweight distillates and the second matter heavy distillate；
(3) the 80% the second heavy distillates are not hydrogenated with circulation solvent as second and return to step (2) with liquefaction coal
Slurry, another 20% the second heavy distillate after vacuum distillation removing residue by obtaining the 3rd heavy distillate, the 3rd heavy end
Oil is not hydrogenated with circulation solvent whole return to step (1) and prepares slurry oil as first；
(4) first light fractions oil presses 1 with the second light fraction oil:The 3rd hydrogenation upgrading reaction is carried out after the mixing of 4 ratios,
Reaction temperature is 360 DEG C, and pressure 15MPa obtains liquid fuel B, and experimental result and liquid fuel B properties are shown in Table 3.
Comparative example 1
Using feed coal and mink cell focus in the same manner as in Example 1, using the technological process in Fig. 2, with coal：Circulation is molten
Agent：Residual oil=1:1.2:0.7 proportions coal, at 450 DEG C, carries out hydrocracking reaction, the light oil for obtaining under 19MPa
Hydrogenation upgrading is carried out under 370 DEG C, 17MPa, liquid fuel C is obtained, experimental result and liquid fuel C properties are shown in Table 3.
Wherein, the conversion ratio of coal is on the basis of moisture-and-ash-free basis coal；Products collection efficiency is as base with the charging of whole organic matters
It is accurate；Hydrogen utilization rate is oily yield/hydrogen consumption.
The heavy oil feed property of table 1
The property of the Xinjiang para bituminous coal of table 2
The coal-residual coprocessing long run test result of table 3 and material properties
The above, is only presently preferred embodiments of the present invention, and any formal limitation is not made to the present invention, according to
Any simple modification, equivalent variations and the modification made to above example according to technical spirit of the invention, still fall within this hair
In the range of bright technical scheme.
Claims (9)
1. a kind of method of coal of inertinite content high and mink cell focus coprocessing, it is characterised in that it includes：
1) mink cell focus, first are not hydrogenated with circulation solvent and catalyst mixes, slurry oil is obtained；Described slurry oil is carried out first
Hydrocracking is reacted, and obtains the first product；The first described product is separated, the first light fraction oil is obtained and the first heavy is evaporated
Divide oil；
2) the first described heavy distillate, second are not hydrogenated with circulation solvent and coal dust mixes, be made coal, will be described
Coal carry out the second hydrocracking reaction, obtain the second product, the second described product is separated, obtain second light
Matter distillate and the second heavy distillate；
3) the second heavy distillate described in is divided into two parts, a part of isolated residue and the 3rd heavy distillate, wherein
The 3rd described heavy distillate is not hydrogenated with circulation solvent as first, for preparing slurry oil；Another part does not add as second
Hydrogen circulates solvent, for preparing coal；
4) the 3rd hydrogenation upgrading is carried out with the second described light fraction oil by described first light fraction is oily, obtain tertiary industry
Thing, described third product is separated, and obtains naphtha, aviation kerosine and diesel oil.
2. the method for the coal of inertinite content high according to claim 1 and mink cell focus coprocessing, it is characterised in that described
Mink cell focus for coal tar, crude oil and/or by after working process low value-added product oil.
3. the method for the coal of inertinite content high according to claim 2 and mink cell focus coprocessing, it is characterised in that described
Coal tar include middle coalite tar, high temperature coal-tar and its processing after heavy distillate；
The low value-added product oil of the petroleum refining is catalytic cracked oil pulp, residual oil, solvent extraction are obtained aromatic hydrocarbons, cracking of ethylene
At least one in tar.
4. the method for the coal of inertinite content high according to claim 1 and mink cell focus coprocessing, it is characterised in that described
The metal active constituent of catalyst be at least one in Fe, Ni, Co, Mo, Ti, W；The matter of the active component of the catalyst
Measure the 0.002-2% for mink cell focus；It is 1 that described first is not hydrogenated with circulation solvent with the mass ratio of mink cell focus：10-6：4.
5. the method for the coal of inertinite content high according to claim 1 and mink cell focus coprocessing, it is characterised in that described
The reaction temperature of the first hydrocracking reaction be 370-430 DEG C, hydrogen dividing potential drop is 12-20MPa, and gas liquid ratio is 400-1500, empty
Speed is 0.5-1.5h-1；
The reaction temperature of the second hydrocracking reaction is 430-470 DEG C, and hydrogen dividing potential drop is 15-22MPa, and gas liquid ratio is 600-
1800, air speed is 0.3-0.8h-1；
The reaction temperature of the 3rd described hydrogenation upgrading is 320-420 DEG C.Hydrogen dividing potential drop is 10-20MPa, and air speed is 0.5-4.0h-1。
6. the method for the coal of inertinite content high according to claim 1 and mink cell focus coprocessing, it is characterised in that described
The first product separated by high-temperature separator and cold catch pot, the separation temperature of described high-temperature separator is 250-
370 DEG C, the separation temperature of the cold catch pot is room temperature；
The second described product is separated by high-temperature separator and cold catch pot；
Described residue and the 3rd heavy distillate are separated by vacuum distillation.
7. the method for the coal of inertinite content high according to claim 1 and mink cell focus coprocessing, it is characterised in that described
The first light fraction oil boiling range be that the end point of distillation is less than 370 DEG C, the cutting temperature of the first heavy end is more than 350 DEG C；
Described the second light fraction oil boiling range is that the end point of distillation is less than 370 DEG C, and the cutting temperature of the second heavy distillate is more than 350
℃；
The separation of described the 3rd mink cell focus and residue realizes that the end point of distillation of the 3rd mink cell focus is less than or equal to by vacuum distillation
520℃。
8. the method for the coal of inertinite content high according to claim 1 and mink cell focus coprocessing, it is characterised in that described
Coal in the weight/mass percentage composition of coal dust be 40-50%, the particle diameter of described coal dust is less than 0.3mm, and moisture is less than
Equal to 4.0%.
9. the method for the coal of inertinite content high according to claim 1 and mink cell focus coprocessing, it is characterised in that described
Second not to be hydrogenated with the mass ratio that accounts in the second heavy distillate of circulation solvent be 50-90%.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108277037A (en) * | 2017-12-26 | 2018-07-13 | 北京三聚环保新材料股份有限公司 | A kind of method of coal and biomass liquefying production light oil |
| CN110144249A (en) * | 2019-05-16 | 2019-08-20 | 煤炭科学技术研究院有限公司 | The preparation method of high matching coal |
| CN112708485A (en) * | 2020-12-27 | 2021-04-27 | 陕西延长石油（集团）有限责任公司 | Method for preparing high-calorific-value high-density jet fuel from kerosene mixed raw material |
| CN113046129A (en) * | 2021-03-22 | 2021-06-29 | 邢彩虹 | Energy-saving kerosene co-refining method and device |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4541916A (en) * | 1984-10-18 | 1985-09-17 | Gulf Research & Development Corporation | Coal liquefaction process using low grade crude oil |
| CN102115674A (en) * | 2009-12-30 | 2011-07-06 | 中国石油化工股份有限公司 | Coal liquefaction and petroleum refining combined method |
| CN104531197A (en) * | 2014-12-19 | 2015-04-22 | 神华集团有限责任公司 | Preparation method of liquid fuel |
| CN106433775A (en) * | 2016-12-20 | 2017-02-22 | 煤炭科学技术研究院有限公司 | Coal and oil coprocessing method and device |
-
2017
- 2017-04-26 CN CN201710280841.6A patent/CN106906001B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4541916A (en) * | 1984-10-18 | 1985-09-17 | Gulf Research & Development Corporation | Coal liquefaction process using low grade crude oil |
| CN102115674A (en) * | 2009-12-30 | 2011-07-06 | 中国石油化工股份有限公司 | Coal liquefaction and petroleum refining combined method |
| CN104531197A (en) * | 2014-12-19 | 2015-04-22 | 神华集团有限责任公司 | Preparation method of liquid fuel |
| CN106433775A (en) * | 2016-12-20 | 2017-02-22 | 煤炭科学技术研究院有限公司 | Coal and oil coprocessing method and device |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108277037A (en) * | 2017-12-26 | 2018-07-13 | 北京三聚环保新材料股份有限公司 | A kind of method of coal and biomass liquefying production light oil |
| CN108277037B (en) * | 2017-12-26 | 2020-04-07 | 北京三聚环保新材料股份有限公司 | Method for producing light oil by coal and biomass liquefaction |
| CN110144249A (en) * | 2019-05-16 | 2019-08-20 | 煤炭科学技术研究院有限公司 | The preparation method of high matching coal |
| CN112708485A (en) * | 2020-12-27 | 2021-04-27 | 陕西延长石油（集团）有限责任公司 | Method for preparing high-calorific-value high-density jet fuel from kerosene mixed raw material |
| CN112708485B (en) * | 2020-12-27 | 2023-04-11 | 陕西延长石油（集团）有限责任公司 | Method for preparing high-calorific-value high-density jet fuel from kerosene mixed raw material |
| CN113046129A (en) * | 2021-03-22 | 2021-06-29 | 邢彩虹 | Energy-saving kerosene co-refining method and device |
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