CN202246573U - System used for processing coal directly-liquefied residue - Google Patents
System used for processing coal directly-liquefied residue Download PDFInfo
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- CN202246573U CN202246573U CN2011203724685U CN201120372468U CN202246573U CN 202246573 U CN202246573 U CN 202246573U CN 2011203724685 U CN2011203724685 U CN 2011203724685U CN 201120372468 U CN201120372468 U CN 201120372468U CN 202246573 U CN202246573 U CN 202246573U
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Abstract
The utility model provides a system used for processing coal directly-liquefied residue. The system comprises a residue extraction device, a first cyclone separator, a re-extraction device, a second cyclone separator, a forcing coarse filtration device, a secondary filter device and a distillation separating unit, wherein the residue extraction device is provided with a first solvent inlet, a liquefaction residue inlet and an extraction mixture outlet; the first cyclone separator is provided with an extraction mixture inlet, a bottom flow outlet and a clear liquid phase mixture outlet; the re-extraction device is provided with a bottom flow inlet, a second solvent inlet and a re-extraction mixture outlet; the second cyclone separator is provided with a re-extraction mixture inlet, a re-extraction bottom flow outlet and a re-extraction liquid phase mixture outlet; the forcing coarse filtration device is provided with a re-extraction bottom flow inlet and a coarse filtration filtrate outlet; the secondary filter device is provided with a liquid phase mixture inlet, a coarse filtration filtrate inlet, a re-extraction mixture outlet and a secondary filter filtrate outlet; and the distillation separating unit is provided with a secondary filter filtrate inlet, a weight quality fluidized oil outlet, an asphaltene outlet and a restoring extraction solvent outlet. The system solves a solid-liquid separation problem in a residue extraction technology, and farthest recovers an extraction solvent.
Description
Technical field
The utility model relates to a kind of system that handles coal directly-liquefied residue, especially relates to a kind of through cyclone separator and filtration unit being coupled extract the system of heavy liquefaction oil and bitumen.
Background technology
Coal direct liquefaction is the important supplement to the China's oil shortage of resources, and is significant to Chinese energy safety.No matter adopt which kind of coal direct liquefaction technology, like IGOR
+Technology, NEDOL technology and Shenhua liquefaction process (ZL200410070249.6 and ZL200610090484.9), the transformation efficiency of coal all can not reach 100%, and about 30% the liquefied residue by product that accounts for the liquefaction coal input quantity is always arranged at last.It is a kind of high-carbon, high ash and doctor positive material, and the unconverted coal, asphaltene and the heavy liquefaction oil that mainly exist by the mineral substance in the coal, catalyzer, with solid form are formed.Wherein the heavy liquefaction oil in the residue, bitumen content account for about 50% of level of residue, and unconverted coal accounts for about 30%, and ash content and catalyzer account for about 20%.
Reclaim the heavy oil product in the liquefied residue, to improving the oily yield of whole coal liquefaction craft, the economic benefit of factory improves efficiency of resource thereby raising is liquefied, and reduces energy dissipation and has very important significance.In addition, the bituminous matter in the coal directly-liquefied residue mainly is made up of the polycyclic condensed aromatics, has the aromaticity height; Carbon content is high, and polymerization or crosslinked characteristics have the unexistent characteristic of a lot of petroleum pitch matter easily; Be suitable as very much the raw material of preparation carbon materials; Be a kind of very valuable and unique resource, the bitum application of gelatin liquefaction receives people's attention day by day, is expected to prepare the carbon product of some high added values.It is the method that the prepared using plasma body prepares nano-carbon material with the coal direct liquefaction residue that Chinese patent ZL200510047800.X discloses a kind of.Chinese patent ZL200610012547.9 discloses a kind of with the method for coal liquefaction residue as road asphalt modifier.Chinese patent ZL200910087907.5 discloses a kind of method of utilizing coal directly-liquefied residue to prepare asphalt base carbon fiber.China ZL200910086158.4 discloses a kind of method for preparing mesophase pitch with coal liquefaction residue.These methods all are to be raw material with the bitumen in the coal liquefaction residue; But from residue, do not isolate the heavy liquefaction oil and be used; Caused the waste of oil product resource undoubtedly; And the extracting of residue medium pitch class material all is to be solvent with expensive pure chemistry reagent, and cost is higher relatively, and research at present is in the laboratory lab scale stage basically.
Current large approach that utilizes to coal liquefaction residue mainly contains methods such as burning, coking system oil, gasification hydrogen-producing.Coal liquefaction residue acts as a fuel and directly in boiler or kiln, burns, and will influence the economy of gelatin liquefaction undoubtedly, causes the waste of resource, and higher sulphur content will be brought the problem aspect the environment in the liquefied residue in combustion processes.Coking system oil is that the asphaltene in the liquefied residue is converted into BO and retortable oil; Though can increase the liquid oil yield of coal liquefaction craft to a certain extent; But semi-coke yield is high after the liquefied residue coking; The oil yield is low, and coking obtain the sulphur content of semicoke high with the ash content height, it utilizes approach also very not clear and definite.Patent CN101760220A discloses a kind of method for continuously coking and equipment of coal liquefied residue; Coking operation carries out under high temperature, condition of high vacuum degree; But because high, the polymerization easily of aromaticity content in the heavy liquefaction oil; It is coke that the heavy liquefaction oil polycondensation of significant proportion is arranged when thermal treatment, and therefore the actual BO ratio that obtains is not high.The method of liquefied residue being carried out gasification hydrogen-producing is a kind of effectively extensive approach that utilizes, but the high value added utilization potentiality of bitumen in the residue and BO are not obtained embodying.
About 50% BO, asphaltene etc. in the residue are had the separating substances of higher utility value to come out and carry out comprehensive processing and utilization respectively, make it produce bigger economic benefit, be a challenging subject in DCL/Direct coal liquefaction field always.One of difficult point wherein is the problem of solid-liquid separation and solvent recuperation.Why these problems are difficult to solve is because the characteristics decision of liquefied residue.The grain graininess of solids is very thin in the coal direct liquefaction residue, particle size distribution from less than 1 μ m to several microns, part is suspended in the raffinate, part is colloidal state; Because the existence of high viscosity materials such as asphaltene, asphaltene before in the liquefied residue, and effects such as therein swelling of unconverted coal, peptization can determine that all the viscosity of liquefied residue is very high; Because liquid phase is made up of heavy liquefaction oil and bituminous matter basically, so the density difference between liquid phase and the solid particulate is smaller.All these characteristics have caused the difficulty of liquefied residue solid-liquid separation.JP1304182 discloses a kind of method of from the direct liquefaction residue, isolating heavy liquefaction oil and bitumen.CN101885976A, CN101962560A and CN101962561A disclose a kind of heavy-fluid carburetion and bituminous matter and comprehensive utilization method in addition respectively of from coal directly-liquefied residue, extracting.The operational path that above patent provides has farthest been brought into play BO and the bitum potentiality of utilizing in the residue, but does not provide concrete solid-liquid separation and extraction solvent recovery scheme.
The utility model people finds through years of researches; Select suitable solvent can from liquefied residue, extract heavy liquefaction oil and bitumen, but in the residue extraction process, the residue solid substrate concentration is big; The concentration of common soluble solid particulate matter accounts for 10～40% of extraction system; And, bring very big difficulty for the solid-liquid separation of extraction system because the existence of high-viscosity materials such as bituminous matter makes extraction system viscosity relatively large.Therefore; How to realize extracting the efficient solid-liquid separation of mixture (extraction solvent, liquefaction BO and bituminous matter) and extract remainder (solid part in the residue); Farthest reclaim extraction solvent; Thereby improving the technical and economic feasibility of extraction process, is the main bottleneck of restriction residue abstraction technique development.The domestic and international research achievement does not address this problem effectively at present.Patent JP2289684 adopts the method for gravity settling that the extraction mixture is separated with extract remainder with patent JP61276889; But this method separation efficiency is relatively low; Precipitation apparatus is relatively heavier; The extract ash content that finally obtains is difficult to reach and is lower than 1% requirement, and the extraction solvent loss is bigger.Kerr-McGee company (U.S. Patent number 3607716, U.S. Patent number 3607717) adopts light aromatics solvent such as toluene etc., extraction liquefied residue under super critical condition; Solid-liquid separation still adopts the method for gravity settling; Although this technology can obtain ash less than 1% extraction product, solvent recovering rate is higher, and extraction temperature is than higher 325～340 ℃; The big 5.0MPa of pressure ratio; This technology extraction conditions is relatively harsh, and plant energy consumption is high, equipment requirements is high, and settlement separate efficient is not high yet.
The utility model content
The utility model provides a kind of system that handles the coal direct liquefaction residue; Purpose is to realize the solid-liquid high efficiency separation of liquefied residue extraction mixture and extract remainder; Obtain the residue extract (comprising heavy liquefaction oil and bitumen) that ash content is lower than 0.1wt%, this extract will become the high quality raw material of high value added product; Simultaneously, native system can farthest reclaim extraction solvent, improves solvent recovering rate, is beneficial to the long-term stability running of implement device, reduces running cost, thereby improves the Technological Economy property of technological process.
A kind of system that handles the coal direct liquefaction residue that the utility model provides; It is characterized in that liquefaction oil (being called first solvent) as extraction solvent, coal directly-liquefied residue is extracted extraction mixture (comprising solvent, extraction heavy liquefaction oil, extraction bituminous matter) and extract remainder to obtain liquefied residue with a kind of specific fraction section.
A kind of system that handles the coal direct liquefaction residue that the utility model provides is characterized in that cyclone separator and filtration unit are coupled, and is used for the solid-liquid separation of liquefied residue extract and extract remainder.Specifically; This system is at first low with cost of investment, safety is high and suitable continuous run in long period and the high cyclone separator of separation efficiency extract the solid-liquid roughing out of mixture and extract remainder; Be directed against the requirement of subsequent technique then; Overflow clear liquid to cyclone separator carries out secondary filter, obtains ash less than 0.1% liquefied residue extract (comprising heavy liquefaction oil and bitumen).
A kind of system that handles the coal direct liquefaction residue that the utility model provides; It is characterized in that; Big to solvent residual amount in the cyclone separator underflow, and in the residue extractable matter not by complete isolating problem, with the liquefaction oil (being called second solvent) of another kind of specific fraction section as extraction solvent; The rotational flow separation underflow is extracted again, and then reclaim solvent and residue extract.
A kind of system that handles the coal direct liquefaction residue that the utility model provides is characterized in that the underflow after second solvent extracts again at first carries out the pressurized raw filtration, reclaims residual solvent and extract; Then filter residue is used the heating agent blowback, carry out drying treatment, further reclaim and residue in the extraction solvent in the filter residue.
In one aspect; The utility model provides a kind of system that handles the coal direct liquefaction residue; It is characterized in that said system comprises: the residue extraction plant has coal directly-liquefied residue inlet, first colvent inlet and coal liquefaction residue extraction mixture outlet; First cyclone separator; Have: coal liquefaction residue extraction mixture inlet; The said coal liquefaction residue extraction mixture outlet of residue extraction plant is connected to the said coal liquefaction residue extraction mixture inlet of said first cyclone separator; Spissated underflow mixture outlet and the outlet of clear liquor phase mixture; Extraction plant again; Have spissated underflow mixture inlet, second colvent inlet and extract the solidliquid mixture outlet again, the said spissated underflow mixture inlet of said extraction plant again is connected to the said spissated underflow mixture outlet of said first cyclone separator; Second cyclone separator; Have: extract the solidliquid mixture inlet again; The said solidliquid mixture that extracts again of said extraction plant again exports the said solidliquid mixture inlet that extracts again that is connected to said second cyclone separator; Spissatedly extract the underflow mixture outlet again and extract clear liquor phase mixture outlet again; The pressurized raw filtration unit; Have spissated underflow mixture inlet and the coarse filtration filtrate outlet of extracting again, said pressurized raw filtration unit said spissated extracts the said spissated underflow mixture outlet that extracts again that the underflow mixture inlet is connected to said second cyclone separator again; The secondary filter device; Have clear liquor phase mixture inlet, the said clear liquor phase mixture inlet of said secondary filter device is connected to the said clear liquor phase mixture outlet of said first cyclone separator and the said clear liquor phase mixture that extracts again of said second cyclone separator exports; Coarse filtration filtrating inlet, said coarse filtration filtrating inlet is connected to the said coarse filtration filtrate outlet of said pressurized raw filtration unit; Export with the secondary filter clear filtrate; And fractionation by distillation device; Have secondary filter clear filtrate inlet, the outlet of heavy liquefaction oil, bituminous matter outlet, first solvent outlet that reclaims and second solvent outlet of recovery; Wherein, the said secondary filter clear filtrate outlet of said secondary filter device is connected to the said secondary filter clear filtrate inlet of said fractionation by distillation device.
System according to the utility model; It is characterized in that; Said system further comprises: first storage tank, the said clear liquor phase mixture that extracts again of the said clear liquor phase mixture outlet of said first cyclone separator and said second cyclone separator exports the said clear liquor phase mixture inlet that is connected to said secondary filter device via said first storage tank.
System according to the utility model; It is characterized in that; Said system further comprises: second storage tank, the said secondary filter clear filtrate outlet of said secondary filter device are connected to the said secondary filter clear filtrate inlet of said fractionation by distillation device via said second storage tank.
System according to the utility model; It is characterized in that; Said pressurized raw filtration unit also has blowback heating agent inlet and gas-oil mixture outlet: said heating agent gets into said pressurized raw filtration unit via the said blowback heating agent inlet of said pressurized raw filtration unit, and the gas-oil mixture of the coarse filtration of discharging via the said gas-oil mixture outlet of said pressurized raw filtration unit is got into the said fractionation by distillation device with the secondary filter clear filtrate of discharging from the said secondary filter clear filtrate outlet of said secondary filter device.
System according to the utility model; It is characterized in that; Said system further comprises: heating agent heating unit and gas and oil separating plant; Said heating agent heating unit has heating agent inlet and the outlet of blowback heating agent; Heating agent gets in the said heating agent heating unit via the said heating agent inlet of said heating agent heating unit, and in heating after discharge by the said blowback heating agent outlet of said heating agent heating unit, the said blowback heating agent outlet of said heating agent heating unit is connected to the said blowback heating agent inlet of said pressurized raw filtration unit; Said gas and oil separating plant has gas-oil mixture inlet and oil content outlet; The said gas-oil mixture inlet of said gas and oil separating plant is connected to the said gas-oil mixture outlet of said pressurized raw filtration unit, and the said oil content outlet of said gas and oil separating plant is connected to the said secondary filter clear filtrate inlet of said fractionation by distillation device.
System according to the utility model is characterized in that, said residue extraction plant and again extraction plant be provided with whipping device and recycle pump.
System according to the utility model is characterized in that, said secondary filter device and pressurized raw filtration unit are provided with pressure equipment and blowback air system are provided.
System according to the utility model; It is characterized in that; Said residue extraction plant also has the residue extraction mixture inlet that is positioned at said residue extraction plant top; The said coal liquefaction residue extraction mixture outlet of said residue extraction plant is positioned at the bottom of said residue extraction plant, and the said coal liquefaction residue extraction mixture outlet of said residue extraction plant also is connected to the said residue extraction mixture inlet on said residue extraction plant top.
System according to the utility model; It is characterized in that; Said residue extraction plant also has first colvent inlet of recovery; Be positioned at the top or the top of said residue extraction plant, first solvent outlet of the said recovery of said fractionation by distillation device is connected to the said recovery and first colvent inlet of said residue extraction plant.
System according to the utility model; It is characterized in that; Said extraction plant more also has second colvent inlet of recovery; Be positioned at the top or the top of said extraction plant again, second solvent outlet of the said recovery of said fractionation by distillation device is connected to second colvent inlet of the said recovery of said extraction plant again.
System according to the utility model; It is characterized in that; Said extraction plant more also has the solidliquid mixture of the extraction again inlet that is positioned at said extraction plant again top; The said of said extraction plant again extracts the bottom that the solidliquid mixture outlet is positioned at said extraction plant more again, and the said solidliquid mixture that extracts again of said extraction plant again exports the said solidliquid mixture inlet that extracts again that also is connected to said extraction plant again top.
System according to the utility model is characterized in that, said gas and oil separating plant also has the outlet of circulation heating agent, is positioned at the top or the top of said gas and oil separating plant.
System according to the utility model is characterized in that, the said circulation heating agent outlet of said gas and oil separating plant is connected to the said heating agent inlet of said gas and oil separating plant.
System according to the utility model is characterized in that, said first storage tank has liquid inlet and liquid exit at least.
System according to the utility model is characterized in that, said second storage tank has liquid inlet and liquid exit at least.
System according to the utility model; It is characterized in that; Between the said coal liquefaction residue extraction mixture inlet of the said coal liquefaction residue extraction mixture outlet of said residue extraction plant and said first cyclone separator, be provided with topping-up pump, and be provided with topping-up pump between entering the mouth at the said solidliquid mixture that extracts again that said extraction plant again said extracts solidliquid mixture outlet and said second cyclone separator again.
System according to the utility model is characterized in that, the pore size filter of said secondary filter device is 0.5～3 μ m.
System according to the utility model is characterized in that, the pore size filter of said pressurized raw filtration unit is 10～50 μ m.
System according to the utility model is characterized in that, said fractionation by distillation device is the combination of atmospheric distillation tower, vacuum still or atmospheric distillation tower and vacuum still.
The system of heavy liquefaction oil and bitumen in the processing coal directly-liquefied residue that the utility model provides; Adopt that separation efficiency is high, equipment volume is little, flexible operation, realize that the cyclone separator of long-term operation extracts the solid-liquid separation of mixture and extract remainder easily, and coupling obtains high quality, hangs down the extract (heavy liquefaction oil and bitumen) of ash with secondary filter; Adopt lightweight solvent method of extraction again, improved the percentage extraction and first solvent recovering yield of liquefied residue to greatest extent; Blowback exsiccant method has improved second solvent recovering yield to greatest extent after adopting coarse filtration.This system has solved the difficult problem of solid-liquid separation in the residue abstraction technique, has farthest reclaimed extraction solvent simultaneously, has reduced solvent loss, has realized solvent recycling.This system makes technological process simple, workable; Be easy to realize long-term operation; Improved the oily yield of whole liquefaction process; And, avoided the waste of liquefied residue resource for the preparation of carbon materials provides the fine raw material, the whole economic efficiency that improves liquefaction factory is had very important realistic meaning.
Description of drawings
With reference to the accompanying drawings, can be more readily understood the technical scheme of the utility model.In the accompanying drawing:
Fig. 1 shows a kind of synoptic diagram of handling the system of coal directly-liquefied residue.
Embodiment
In the utility model, for the emphasis of outstanding the utility model, the omission that some conventional operations and unit, parts are carried out, or only do simple description.
In the utility model, " with ... link to each other " or " being connected to " or " connections ", both can be that the two directly links to each other, also can across common parts or device (for example valve, pump, interchanger etc.) links to each other or connection.
In the utility model, " coal directly-liquefied residue " and " coal liquefaction residue " interchangeable use all refers to the coal liquefaction residue that the solid-liquid separation process of gelatin liquefaction product utilization vacuum flashing (underpressure distillation) obtains.
An aspect of the utility model provides a kind of system that handles the coal direct liquefaction residue, it is characterized in that said system comprises: the residue extraction plant has coal directly-liquefied residue inlet, first colvent inlet and coal liquefaction residue extraction mixture outlet; First cyclone separator; Have: coal liquefaction residue extraction mixture inlet; The said coal liquefaction residue extraction mixture outlet of residue extraction plant is connected to the said coal liquefaction residue extraction mixture inlet of said first cyclone separator; Spissated underflow mixture outlet and the outlet of clear liquor phase mixture; Extraction plant again; Have spissated underflow mixture inlet, second colvent inlet and extract the solidliquid mixture outlet again, the said spissated underflow mixture inlet of said extraction plant again is connected to the said spissated underflow mixture outlet of said first cyclone separator; Second cyclone separator; Have: extract the solidliquid mixture inlet again; The said solidliquid mixture that extracts again of said extraction plant again exports the said solidliquid mixture inlet that extracts again that is connected to said second cyclone separator; Spissatedly extract the underflow mixture outlet again and extract clear liquor phase mixture outlet again; The pressurized raw filtration unit; Have spissated underflow mixture inlet and the coarse filtration filtrate outlet of extracting again, said pressurized raw filtration unit said spissated extracts the said spissated underflow mixture outlet that extracts again that the underflow mixture inlet is connected to said second cyclone separator again; The secondary filter device has clear liquor phase mixture inlet, and the said clear liquor phase mixture inlet of said secondary filter device is connected to the said clear liquor phase mixture outlet of said first cyclone separator; Coarse filtration filtrating inlet, said coarse filtration filtrating inlet is connected to the said coarse filtration filtrate outlet of said pressurized raw filtration unit; Export with the secondary filter clear filtrate; And fractionation by distillation device; Have secondary filter clear filtrate inlet, the outlet of heavy liquefaction oil, bituminous matter outlet, first solvent outlet that reclaims and second solvent outlet of recovery; Wherein, the said secondary filter clear filtrate outlet of said secondary filter device is connected to the said secondary filter clear filtrate inlet of said fractionation by distillation device.
Preferably; The system of the utility model further comprises: first storage tank, the said clear liquor phase mixture that extracts again of the said clear liquor phase mixture outlet of said first cyclone separator and said second cyclone separator exports the said clear liquor phase mixture inlet that is connected to said secondary filter device via said first storage tank.
Preferably, the system of the utility model further comprises: second storage tank, the said secondary filter clear filtrate outlet of said secondary filter device are connected to the said secondary filter clear filtrate inlet of said fractionation by distillation device via said second storage tank.
Preferably; Wherein, Said pressurized raw filtration unit also has blowback heating agent inlet and gas-oil mixture outlet: said heating agent gets into said pressurized raw filtration unit via the said blowback heating agent inlet of said pressurized raw filtration unit, and the gas-oil mixture of the coarse filtration of discharging via the said gas-oil mixture outlet of said pressurized raw filtration unit is got into the said fractionation by distillation device with the secondary filter clear filtrate of discharging from the said secondary filter clear filtrate outlet of said secondary filter device.
Preferably; Wherein, Said system further comprises: heating agent heating unit and gas and oil separating plant, said heating agent heating unit have heating agent inlet and the outlet of blowback heating agent, and heating agent gets in the said heating agent heating unit via the said heating agent inlet of said heating agent heating unit; And in heating after discharge by the said blowback heating agent outlet of said heating agent heating unit, the said blowback heating agent outlet of said heating agent heating unit is connected to the said blowback heating agent inlet of said pressurized raw filtration unit; Said gas and oil separating plant has gas-oil mixture inlet and oil content outlet; The said gas-oil mixture inlet of said gas and oil separating plant is connected to the said gas-oil mixture outlet of said pressurized raw filtration unit, and the said oil content outlet of said gas and oil separating plant is connected to the said secondary filter clear filtrate inlet of said fractionation by distillation device.
Preferably, wherein, said residue extraction plant is provided with whipping device and recycle pump.
Preferably, wherein, said secondary filter device and pressurized raw filtration unit are provided with pressure equipment and blowback air system are provided.
Preferably; Wherein, Said residue extraction plant also has the residue extraction mixture inlet that is positioned at said residue extraction plant top; The said coal liquefaction residue extraction mixture outlet of said residue extraction plant is positioned at the bottom of said residue extraction plant, and the said coal liquefaction residue extraction mixture outlet of said residue extraction plant also is connected to the said residue extraction mixture inlet on said residue extraction plant top.
Preferably; Wherein, Said residue extraction plant also has first colvent inlet of recovery, is positioned at the top or the top of said residue extraction plant, and first solvent outlet of the said recovery of said fractionation by distillation device is connected to first colvent inlet of the said recovery of said residue extraction plant.
Preferably; Wherein, Said extraction plant more also has second colvent inlet of recovery, is positioned at the top or the top of said extraction plant again, and second solvent outlet of the said recovery of said fractionation by distillation device is connected to second colvent inlet of the said recovery of said extraction plant again.
Preferably; Wherein, Said extraction plant more also has the solidliquid mixture of the extraction again inlet that is positioned at said extraction plant again top; The said of said extraction plant again extracts the bottom that the solidliquid mixture outlet is positioned at said extraction plant more again, and the said solidliquid mixture that extracts again of said extraction plant again exports the said solidliquid mixture inlet that extracts again that also is connected to said extraction plant again top.
Preferably, wherein, said gas and oil separating plant also has the outlet of circulation heating agent, is positioned at the top or the top of said gas and oil separating plant.
Preferably, wherein, the said circulation heating agent outlet of said gas and oil separating plant is connected to the said heating agent inlet of said gas and oil separating plant.
Preferably, wherein, said first storage tank has liquid inlet and liquid exit at least.
Preferably, wherein, said second storage tank has liquid inlet and liquid exit at least.
Preferably; Wherein, Between the said coal liquefaction residue extraction mixture inlet of the said coal liquefaction residue extraction mixture outlet of said residue extraction plant and said first cyclone separator, be provided with topping-up pump, and be provided with topping-up pump between entering the mouth at the said solidliquid mixture that extracts again that said extraction plant again said extracts solidliquid mixture outlet and said second cyclone separator again.
Preferably, wherein, the pore size filter of said secondary filter device is 0.5～3 μ m.
Preferably, wherein, the pore size filter of said pressurized raw filtration unit is 10～50 μ m.
According to the system of the utility model, wherein, said fractionation by distillation device is the combination of atmospheric distillation tower, vacuum still or atmospheric distillation tower and vacuum still.
According to another aspect of the utility model, a kind of method that from the coal direct liquefaction residue, extracts heavy liquefaction oil and bitumen is provided, said method comprising the steps of:
A) coal liquefaction residual powder is joined with first solvent carry out thorough mixing extraction in the residue extraction plant, so that comprise heavy liquefaction oil and bitum extractable matter in the liquefied residue are extracted in first solvent;
B) utilize first cyclone separator that comprise first solvent, heavy liquefaction oil, bitum extraction mixture and the residue extract remainder that obtains in the step a) carried out solid-liquid separation, obtain the spissated underflow mixture of clear liquor phase mixture and bottom of upper strata overflow respectively;
C) the spissated underflow mixture in the bottom in the step b) is sent to second solvent again carries out extraction treatment again in the extraction plant, first solvent of carrying secretly in the underflow mixture and extractable matter are extracted in second solvent again, to obtain to extract again mixture;
D) utilize second cyclone separator to comprise first solvent, second solvent, heavy liquefaction oil, bitumly extract mixture again and the residue extract remainder carries out the solid-liquid separation second time, obtain the spissated underflow mixture that extracts again of clear liquor phase mixture of extraction again and bottom of upper strata overflow respectively what obtain in the step c);
E) clear liquor phase mixture in the step b) and the clear liquor of the extraction again phase mixture in the step e) are carried out secondary filter in the secondary filter device, and filtrating is sent in the fractionation by distillation device;
F) the spissated underflow mixture that extracts again in the bottom in the step d) is carried out pressurized raw and filters in the pressurized raw filtration unit, the filtrating part with extract the clear liquor phase mixture again through secondary filter, send into the fractionation by distillation device;
G) in the fractionation by distillation device, the extraction mixture is separated, supply to recycle, and obtain heavy liquefaction oil and ash less than 0.1% bitumen to reclaim first solvent, second solvent.
Preferably, said method also comprises step h between step f) and step g)): remaining filter residue carried out drying treatment with the heating agent blowback after pressurized raw was filtered in to step f), reclaimed residual solvent, sent into the fractionation by distillation device.
Preferably, said first solvent and second solvent are in the DCL/Direct coal liquefaction process liquefaction oil product that directly produces, and said first solvent is 160～260 ℃ a fraction, and said second solvent is the fraction of over point (IBP)～110 ℃.
Preferably, the extracting operation condition in said step a) is: the mass ratio of coal liquefaction residue and said first solvent is 1: 1～10, be preferably 1: 2～and 8; N
2And/or H
2Atmosphere, pressure is 0.1～3.0MPa, is preferably 0.2～2.5MPa; Extraction temperature is 60～300 ℃, is preferably 80～250 ℃; The extraction time is 5～120min, and stir speed (S.S.) is 50～400r/min; The solid concentration of extraction back system is 5～30%, and system density is 0.95～1.5g/ml.
Preferably, at said step b) and d) in extraction mixture and the solid concentration that extracts the clear liquor phase mixture of the upper strata overflow that mixture obtains again after rotational flow separation be 1%～5%, the solid concentration of the spissated underflow mixture in bottom is 40～60%.
Preferably, the condition of extracting operation again of second solvent is in said step c): the mass ratio of coal liquefaction residue and said second solvent is 1: 1～10, be preferably 1: 1～and 6; N
2And/or H
2Atmosphere, pressure is 0.2～3.5MPa, is preferably 0.5～2.5MPa; Extraction temperature is 30～250 ℃, is preferably 40～150 ℃; The extraction time is 5～120min, and stir speed (S.S.) is 50～400r/min.
The clear liquor phase mixture of the upper strata overflow that preferably, rotational flow separation obtains in said step e) obtains solid concentration and is not more than 0.01% filtrating after secondary filter.
The pore size filter of the secondary filter device that preferably, in said step e), uses is 0.5～3 μ m.
Preferably, the spissated underflow mixture that extracts again obtains solid concentration and is not more than 5% filtrating after pressurized raw is filtered in said step f).
The pore size filter of the pressurized raw filtration unit that preferably, in said step f), uses is 10～50 μ m.
Preferably, the solid concentration of pressurized raw filtered filtration residue is 70～90% in said step f).
Preferably, at said step h) in heating agent be meant nitrogen, helium rare gas element and water vapor or their mixture, said heating agent is heated to 100～300 ℃ in heating unit, be used for the blowback drying treatment of coarse filtration filter residue.
Preferably, in said step d), reclaim residual solvent and at least one oil-gas separator, carry out.
Preferably, in said step g), the fractionation by distillation device is air distillation tripping device, underpressure distillation tripping device or both combinations, preferably both combinations.
Preferably, the particle diameter of said coal directly-liquefied residue powder is 0.05～2mm.
Preferably, said residue extraction plant and again extraction plant be provided with whipping device and recycle pump.
Preferably, said secondary filter device and pressurized raw filtration unit are provided with pressure equipment and blowback air system are provided.
Preferably, according to heavy liquefaction oil and bitumen that the method for the utility model is extracted, wherein, the boiling range of said heavy liquefaction oil is 260～450 ℃, and the ash of said bitumen is less than 0.1%.
Wherein, the particle diameter of said coal directly-liquefied residue powder is 0.05～2mm, the ash content of coal 10～30%.
Preferably, the pressure-losses of said cyclone separator is 0.1～1.0MPa.
Preferably, be 260～450 ℃ by the boiling range of the heavy liquefaction oil that extracts according to the method for the utility model, be particularly suitable for solvent as coal direct liquefaction technology, also be that further unifining becomes other processed oil, like the high quality raw material of diesel oil, solvent oil.
Preferably, less than 0.1%, it is the high quality raw material of preparation carbon materials by the ash of the bitumen that extracts according to the method for the utility model.
Below in conjunction with Fig. 1 the method that the utility model provided is at length explained, but the utility model is not limited to this.
As shown in Figure 1, the coal directly-liquefied residue powder 1 after the fragmentation and first solvent 2 are joined in the residue extraction plant 3 via first colvent inlet 32 and coal directly-liquefied residue inlet 31 respectively by a certain percentage, under certain extraction conditions, carry out extracting operation.Then; To preferably be pumped into first cyclone separator 4 carrying out solid-liquid separation from the coal liquefaction residue extraction mixture outlet 41 of cyclone separator 4 through the solidliquid mixture of extraction from what the coal liquefaction residue of residue extraction plant 3 extraction mixture outlet 33 was discharged, thereby the height of realizing the gelatin liquefaction solid residue concentrates via topping-up pump.Wherein, Said residue extraction plant 3 also has the residue extraction mixture inlet 34 that is positioned at said residue extraction plant 3 tops; The said coal liquefaction residue extraction mixture outlet 34 of said residue extraction plant 3 is positioned at the bottom of said residue extraction plant 3, and the said coal liquefaction residue extraction mixture outlet 33 of said residue extraction plant 3 also is connected to the said residue extraction mixture inlet 34 on said residue extraction plant 3 tops.Preferably, the clear liquor phase mixture of the upper strata overflow of discharging from the clear liquor phase mixture of first cyclone separator 4 outlet 43 is flow into first storage tank 6, so that regime flow via the liquid inlet of first storage tank 6.Then, will be pressed into the secondary filter device 7 via the clear liquor phase mixture inlet 71 of secondary filter device 7 from the liquid that the liquid exit of first storage tank 6 is discharged.Preferably, the filtrating of discharging from the secondary filter clear filtrate outlet 73 of secondary filter device 7 is flow into second storage tank 8.The spissated underflow mixture in bottom of discharging from the spissated underflow mixture outlet of first cyclone separator 4 42 is flow into the extraction plant 5 via the spissated underflow mixture inlet 51 of extraction plant 5 more again; And by a certain percentage second solvent 19 is joined in the extraction plant 5 via second colvent inlet 52 again, carry out extracting operation more under certain condition.
Then; To preferably be pumped into from the solidliquid mixture of the extraction again inlet 121 of second cyclone separator 12 second cyclone separator 12 carrying out solid-liquid separation from the solidliquid mixture that extracts the extraction again that solidliquid mixture outlet 53 discharges again of extraction plant 5 again, thereby the height of realizing the gelatin liquefaction solid residue concentrates via topping-up pump.Wherein, Said extraction plant again 5 also has the solidliquid mixture of the extraction again inlet 54 that is positioned at said extraction plant again 5 tops; Said extraction plant again 5 said extracts the bottom that solidliquid mixture outlet 53 is positioned at said extraction plant again 5 again, and said extraction plant again 5 said extracts the said solidliquid mixture inlet 54 that extracts again that solidliquid mixture outlet 53 also is connected to said extraction plant again 5 tops again.Preferably; Make from the clear liquor phase mixture that extracts again that extracts upper strata overflow that clear liquor phase mixture outlet 123 discharges again of second cyclone separator 12 to flow into first storage tank 6 via the liquid inlet of first storage tank 6, so that regime flow with the clear liquor phase mixture of the upper strata overflow of discharging from the clear liquor phase mixture outlet 43 of first cyclone separator 4.Then; To be pressed into the secondary filter device 7 via the clear liquor phase mixture inlet 71 of secondary filter device 7 from the liquid that the liquid exit of first storage tank 6 is discharged, the filtrating of discharging from the secondary filter clear filtrate outlet of secondary filter device 7 is flow into second storage tank 8.To extract the spissated underflow mixture that extracts again in bottom that underflow mixture outlet 122 discharges again from second cyclone separator 12 spissated and extract underflow mixture inlet 131 again via pressurized raw filtration unit 13 spissated and flow into the pressurized raw filtration unit 13, and carry out hot pressurized raw and filter.After the filtrating of gained is discharged from the coarse filtration filtrate outlet 132 of pressurized raw filtration unit 13; Get in the secondary filter device 7 via the coarse filtration filtrating inlet 72 of secondary filter device 7; Filtrate filtered flow in second storage tank 8 via the secondary filter clear filtrate outlet 73 of secondary filter device 7, so that regime flow.
Preferably; After the heating agent of introducing via the heating agent of heating agent heating unit 15 inlet 151 18 heats in heating agent heating unit 15; After heating agent outlet 152 discharges through heating agent heating unit 15; Blowback heating agent inlet 133 via pressurized raw filtration unit 13 gets in the pressurized raw filtration unit 13, in pressurized raw filtration unit 13, carries out blowback, drying treatment.The gas-oil mixture that to discharge from the gas-oil mixture of pressurized raw filtration unit 13 outlet 134 is incorporated into the gas and oil separating plant 14 via the gas-oil mixture inlet 141 of gas and oil separating plant 14, and this gas-oil mixture separates through gas and oil separating plant 14.Then, the heating agent that makes gained is discharged from the blowback heating agent outlet 143 of gas and oil separating plant 14, is incorporated into the heating agent heating unit 15 from the heating agent inlet 151 of heating agent heating unit 15, supplies to recycle.To be sent in the fractionation by distillation device 9 via the extraction mixture of oil content in second storage tank 8 that the oil content outlet 142 of gas and oil separating plant 14 is discharged, first solvent 2 of recovery and second solvent 19 are discharged with second solvent outlet 95 that reclaims via first solvent outlet 94 of the recovery of fractionation by distillation device 9.First solvent that reclaims is fed in the residue extraction plant 3 through first colvent inlet 35 of the recovery of residue extraction plant 3, supplies to recycle.Second solvent 19 that reclaims is fed in the extraction plant 5 via second colvent inlet 55 of the recovery of extraction plant 5 more again, supplies to recycle.And obtain the extraction product heavy liquefaction oil 16 and high-quality asphalt matter 17 of coal liquefaction residue.
The system of the processing coal directly-liquefied residue that the utility model provides; Its characteristics are; Cyclone separator and filtration unit separation efficiency is high, that be fit to long-term operation are coupled; The solid-liquid separation that is used for liquefied residue extract and extract remainder, the whole process flow process is simple, easy and safe to operate, separation efficiency is high, facility investment is little, be fit to long-term operation.
The system of the processing coal directly-liquefied residue that the utility model provides; Its characteristics are; The spissated extraction mixture of eddy flow underflow is extracted with second solvent again, and carry out coarse filtration, hot blowback drying treatment, thereby improve solvent recovering yield extracting the underflow mixture again; Increase the percentage extraction of liquefied residue, thereby improve the economy of extraction process.
The system of the processing coal directly-liquefied residue that the utility model provides, its characteristics are that two kinds of extraction solvents are all from the gelatin liquefaction process, and are from the horse's mouth, with low cost for the liquefaction oil product of different fractions section, and easy recovery can supply to recycle for a long time.
The system of the processing coal directly-liquefied residue that the utility model provides, its characteristics are, from liquefied residue, extract the heavy liquefaction oil, not only can improve the overall oily yield of gelatin liquefaction process, avoid the residue wasting of resources, thereby improve the economy of liquefaction factory; And be the coal liquefaction solvent that suits, can improve the degree of heaviness of coal liquefaction solvent, help the gelatin liquefaction reaction.
What the utility model provided is a kind of from coal directly-liquefied residue extraction heavy liquefaction oil and bitum method, and its characteristics are that the condensation degree of the bitumen aromatic ring that from liquefied residue, extracts is high; The C/H atomic ratio is high; Quinoline insolubles is low, and ash content is low, is the high quality raw material of preparation carbon materials.
Further specify the utility model through the following example, but the protection domain of the utility model is not limited to the following example.
Embodiment
The fundamental test flow process is following:
The coal direct liquefaction residue that produces in a kind of 0.1t/d coal direct liquefaction of this experiment selected device, residue character sees attached list 1.At first residue is crushed to below the 2mm with jaw crusher.As shown in Figure 1, coal directly-liquefied residue powder after the 100Kg fragmentation 1 and 300Kg first solvent 2 are joined in the residue extraction plant 3, by carrying out extracting operation under the extraction conditions shown in the subordinate list 2; Extraction have stir and the pump circulation condition under carry out, will extract solidliquid mixture then and be pumped into cyclone separator 4 and carry out solid-liquid separation, obtain the clear liquor phase mixture 301.5Kg of upper strata overflow; Solid concentration is 2.1%; Flow into first storage tank 6, be pressed into secondary filter device 7 then, the filter pore size is 1 μ m; The solid concentration that obtains filtrating is 0.005%, flows in second storage tank 8.Cyclone separator 4 bottoms spissated underflow mixture 98.5Kg, solid concentration 47.1% flows in the extraction plant 5 again, adds 200Kg second solvent 19 again, by carrying out extracting operation again under the extraction conditions again shown in the table 2.Extraction have stir and the pump circulation condition under carry out; To extract solidliquid mixture again is pumped into cyclone separator 12 and carries out solid-liquid separation; Obtain the clear liquor of the extraction again phase mixture 210.1Kg of upper strata overflow, solid concentration is 1.9%, flows into first storage tank 6; After secondary filter device 7 filters, flow into second storage tank 8 then.The spissated underflow mixture 88.4Kg that extracts again in cyclone separator 12 bottoms, solid concentration 50.1% is sent into pressurized raw filtration unit 13, carries out the hot pressing coarse filtration.The filter pore size is 50 μ m, and the 25.8Kg that must filtrate again through secondary filter device 7, flows into second storage tank 8.
The character data of table 1 coal directly-liquefied residue
* oil content refers to the normal hexane soluble part in the residue in the soxhlet extraction, the bituminous matter insoluble THF soluble part of hexane of making a comment or criticism, and insolubles refers to the insoluble part of THF.
* comprises asphaltene and the preceding asphaltene in the residue.
The main extraction process condition of table 2 embodiment
Table 3 utilizes the experimental result of coal directly-liquefied residue of the system handles of the utility model
Comparative example
Technique effect for the system that further specifies the utility model; Comparative example 1 adopts coal directly-liquefied residue, first extraction solvent, extraction conditions and identical distillating method same as the previously described embodiments; Adopt conventional thermal air pressure filtration method to carry out solid-liquid separation, main experimental result is seen table 4.
Comparative example 2 adopts coal directly-liquefied residue, first extraction solvent, extraction conditions and identical distillating method same as the previously described embodiments, adopts conventional settling methods to carry out solid-liquid separation, and main experimental result is seen table 4.
Table 4 is according to the experimental result of the coal directly-liquefied residue of system in the traditional method
Data from table 3 and table 4 can be found out; Compare with experimental result according to the coal directly-liquefied residue of system in the traditional method; According to the described system of the utility model, the percentage extraction of coal directly-liquefied residue, heavy liquefaction oil and bitum yield are high, and the recovery of extraction solvent is high; The continuous long-term operation that helps the residue extraction process, the economy of raising DCL/Direct coal liquefaction technology.
The utility model is described with reference to embodiment and embodiment.Yet, the aspect that the utility model is not limited to describe in the above-described embodiment and examples, and can carry out various distortion.But should be appreciated that for a person skilled in the art, under the situation of spirit that does not deviate from the utility model and scope, can carry out various modifications and be equal to replacement the utility model.Therefore, the utility model specific embodiment of being not limited to describe in this article.More properly, the protection domain of the utility model is limited by the accompanying claims.
Claims (19)
1. a system that handles the coal direct liquefaction residue is characterized in that, said system comprises:
Residue extraction plant (3) has coal directly-liquefied residue inlet (31), first colvent inlet (32) and coal liquefaction residue extraction mixture outlet (33);
First cyclone separator (4) has:
Coal liquefaction residue extraction mixture inlet (41), the said coal liquefaction residue extraction mixture outlet (33) of residue extraction plant (3) are connected to the said coal liquefaction residue extraction mixture inlet (41) of said first cyclone separator (4),
Spissated underflow mixture outlet (42) and
Clear liquor phase mixture outlet (43);
Extraction plant (5) again; Have spissated underflow mixture inlet (51), second colvent inlet (52) and extract solidliquid mixture outlet (53) again, the said spissated underflow mixture inlet (51) of said extraction plant again (5) is connected to the said spissated underflow mixture outlet (42) of said first cyclone separator (4);
Second cyclone separator (12) has:
Extract solidliquid mixture inlet (121) again, the said solidliquid mixture that extracts again of said extraction plant again (5) exports the said solidliquid mixture inlet (121) that extracts again that (53) are connected to said second cyclone separator (12),
Spissated extract again underflow mixture outlet (122) and
Extract clear liquor phase mixture outlet (123) again;
Pressurized raw filtration unit (13); Have spissated underflow mixture inlet (131) and the coarse filtration filtrate outlet (132) of extracting again, said pressurized raw filtration unit (13) said spissated extracts the said spissated underflow mixture outlet (122) that extracts again that underflow mixture inlet (131) is connected to said second cyclone separator (12) again;
Secondary filter device (7); Have clear liquor phase mixture inlet (71), the said clear liquor phase mixture inlet (71) of said secondary filter device (7) is connected to the said clear liquor phase mixture outlet (43) of said first cyclone separator (4) and the said clear liquor phase mixture that extracts again of said second cyclone separator (12) exports (123); Coarse filtration filtrating inlet (72), said coarse filtration filtrating inlet (72) is connected to the said coarse filtration filtrate outlet (132) of said pressurized raw filtration unit (13); With secondary filter clear filtrate outlet (73); And
Fractionation by distillation device (9); Second solvent outlet (95) that has secondary filter clear filtrate inlet (91), heavy liquefaction oil outlet (92), bituminous matter outlet (93), first solvent outlet (94) that reclaims and reclaim; Wherein, the said secondary filter clear filtrate outlet (73) of said secondary filter device (7) is connected to the said secondary filter clear filtrate inlet (91) of said fractionation by distillation device (9).
2. system according to claim 1; It is characterized in that; Said system further comprises: first storage tank (6), the said clear liquor phase mixture that extracts again of the said clear liquor phase mixture outlet (43) of said first cyclone separator (4) and said second cyclone separator (12) exports (123) are connected to said secondary filter device (7) via said first storage tank (6) said clear liquor phase mixture inlet (71).
3. system according to claim 1; It is characterized in that; Said system further comprises: second storage tank (8), the said secondary filter clear filtrate outlet (73) of said secondary filter device (7) are connected to the said secondary filter clear filtrate inlet (91) of said fractionation by distillation device (9) via said second storage tank (8).
4. system according to claim 1; It is characterized in that; Said pressurized raw filtration unit (13) also has blowback heating agent inlet (133) and gas-oil mixture outlet (134): said heating agent gets into said pressurized raw filtration unit (13) via the said blowback heating agent inlet (133) of said pressurized raw filtration unit (13), and the gas-oil mixture of the coarse filtration of discharging via the said gas-oil mixture outlet (134) of said pressurized raw filtration unit (13) is got into the said fractionation by distillation device (9) with the secondary filter clear filtrate of discharging from the said secondary filter clear filtrate outlet (73) of said secondary filter device (7).
5. system according to claim 4; It is characterized in that; Said system further comprises: heating agent heating unit (15) and gas and oil separating plant (14); Said heating agent heating unit (15) has heating agent inlet (151) and blowback heating agent outlet (152); Heating agent gets in the said heating agent heating units (15) via the said heating agent inlet (151) of said heating agent heating unit (15), and in heating after discharge by the said blowback heating agent outlet (152) of said heating agent heating unit (15), the said blowback heating agent outlet (152) of said heating agent heating unit (15) is connected to the said blowback heating agent inlet (133) of said pressurized raw filtration unit (13); Said gas and oil separating plant (14) has gas-oil mixture inlet (141) and oil content outlet (142); The said gas-oil mixture inlet (141) of said gas and oil separating plant (14) is connected to the said gas-oil mixture outlet (134) of said pressurized raw filtration unit (13), and the said oil content outlet (142) of said gas and oil separating plant (14) is connected to the said secondary filter clear filtrate inlet (91) of said fractionation by distillation device (9).
6. system according to claim 1 is characterized in that, said residue extraction plant (3) and again extraction plant (5) be provided with whipping device and recycle pump.
7. system according to claim 1 is characterized in that, said secondary filter device (7) and pressurized raw filtration unit (13) are provided with pressure equipment and blowback air system are provided.
8. system according to claim 1; It is characterized in that; Said residue extraction plant (3) also has the residue extraction mixture inlet (34) that is positioned at said residue extraction plant (3) top; The said coal liquefaction residue extraction mixture outlet (33) of said residue extraction plant (3) is positioned at the bottom of said residue extraction plant (3), and the said coal liquefaction residue extraction mixture outlet (33) of said residue extraction plant (3) also is connected to the said residue extraction mixture inlet (34) on said residue extraction plant (3) top.
9. system according to claim 1; It is characterized in that; Said residue extraction plant (3) also has first colvent inlet (35) of recovery; Be positioned at the top or the top of said residue extraction plant (3), first solvent outlet (94) of the said recovery of said fractionation by distillation device (9) is connected to first colvent inlet (35) of the said recovery of said residue extraction plant (3).
10. system according to claim 1; It is characterized in that; Said extraction plant again (5) also has second colvent inlet (55) of recovery; Be positioned at the top or the top of said extraction plant again (5), second solvent outlet (95) of the said recovery of said fractionation by distillation device (9) is connected to second colvent inlet (55) of the said recovery of said extraction plant again (5).
11. system according to claim 1; It is characterized in that; Said extraction plant again (5) also has the solidliquid mixture of the extraction again inlet (54) that is positioned at said extraction plant again (5) top; The said of said extraction plant again (5) extracts the bottom that solidliquid mixture outlet (53) is positioned at said extraction plant again (5) again, and the said solidliquid mixture that extracts again of said extraction plant again (5) exports the said solidliquid mixture inlet (54) that extracts again that (53) also are connected to said extraction plant again (5) top.
12. system according to claim 5 is characterized in that, said gas and oil separating plant (14) also has circulation heating agent outlet (143), is positioned at the top or the top of said gas and oil separating plant (14).
13. system according to claim 5 is characterized in that, the said circulation heating agent outlet (143) of said gas and oil separating plant (14) is connected to the said heating agent inlet (151) of said gas and oil separating plant (14).
14. system according to claim 2 is characterized in that, said first storage tank (6) has liquid inlet and liquid exit at least.
15. system according to claim 3 is characterized in that, said second storage tank (8) has liquid inlet and liquid exit at least.
16. according to each described system among the claim 1-4; It is characterized in that; Between the said coal liquefaction residue extraction mixture inlet (41) of the said coal liquefaction residue extraction mixture outlet (33) of said residue extraction plant (3) and said first cyclone separator (4), be provided with topping-up pump, and enter the mouth and be provided with topping-up pump between (121) at the said solidliquid mixture that extracts again that said extraction plant again (5) said extracts solidliquid mixture outlet (53) and said second cyclone separator (12) again.
17., it is characterized in that the pore size filter of said secondary filter device (7) is 0.5～3 μ m according to each described system among the claim 1-4.
18., it is characterized in that the pore size filter of said pressurized raw filtration unit (13) is 10～50 μ m according to each described system among the claim 1-4.
19., it is characterized in that said fractionation by distillation device (9) is the combination of atmospheric distillation tower, vacuum still or atmospheric distillation tower and vacuum still according to each described system among the claim 1-4.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011203724685U CN202246573U (en) | 2011-09-30 | 2011-09-30 | System used for processing coal directly-liquefied residue |
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011203724685U CN202246573U (en) | 2011-09-30 | 2011-09-30 | System used for processing coal directly-liquefied residue |
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