CN108130121A - A kind of method of extractant in vacuum film dried recovered coal base oil slag extract remainder - Google Patents
A kind of method of extractant in vacuum film dried recovered coal base oil slag extract remainder Download PDFInfo
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- CN108130121A CN108130121A CN201810001316.0A CN201810001316A CN108130121A CN 108130121 A CN108130121 A CN 108130121A CN 201810001316 A CN201810001316 A CN 201810001316A CN 108130121 A CN108130121 A CN 108130121A
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- steam
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/28—Recovery of used solvent
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
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- Extraction Or Liquid Replacement (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The present invention relates to a kind of method of extractant in vacuum film dried recovered coal base oil slag extract remainder, this method includes the following steps：(1) the class pitch class dregs of fat containing washing oil, which are added in level-one film drier, carries out indirectly heat, respectively obtains the dregs of fat and naphtha steam that washing oil content is 5% ~ 20%；(2) the dregs of fat that washing oil content is 5% ~ 20%, which are added in two level film drier, carries out indirectly heat, respectively obtains the dregs of fat and heavy oil steam that washing oil content is 5% ~ 0.5%；Naphtha steam obtains non-condensing naphtha steam and a small amount of dust A through cooling, ejector action；(3) the dregs of fat that washing oil content is 5% ~ 0.5% cool down to obtain 30 DEG C ~ 100 DEG C of the dregs of fat；Heavy oil steam obtains non-condensing naphtha steam and a small amount of dust B through cooling, ejector action；(4) non-condensing naphtha steam and a small amount of dust A are mixed to form with non-condensing naphtha steam and a small amount of dust B and mix washing oil steam, the washing oil through being condensed；(5) the washing oil condensed cools down to obtain 30 DEG C ~ 100 DEG C of washing oil.The present invention invests small, easy to implement, high efficiency.
Description
Technical field
The present invention relates in technical field of coal chemical industry more particularly to a kind of vacuum film dried recovered coal base oil slag extract remainder
The method of extractant.
Background technology
With China's energy, the growth of chemical products demand, coal chemical industry has occupied an important position in the field, coalification industrial and commercial bank
The development of industry plays supplementary function for alleviating the high-grade energies disparities between supply and demand such as China's oil, natural gas.Coal liquefaction technology is
It solves above-mentioned contradiction and realizes an effective technical way of China's energy sustainable development.
Coal base oil slag is the solid-liquid mixing residue that Coal Liquefaction product obtains after vacuum distillation, is accounted for about always into coal
The 20% ~ 30% of amount.Containing heavy coal liquids, bitumen and unconverted coal in the residue, wherein, mink cell focus and pitch
Class content of material accounts for 50% or so of total dregs of fat.Generally use organic solvent extracts method, recycles the part oil product.And pass through extraction
Take can be remained in the dregs of fat after filtration treatment more than 20% extractant.The partial extraction agent is recycled, recycles extraction
Agent can save extractant usage amount, reduce dregs of fat post processing expense, avoid the pollution problem that subsequent technique is brought, moreover it is possible to
Improve the operability and economic feasibility of dregs of fat extraction and separation technology.General extractant is washing oil, is a kind of wide boiling range, height boiling
The sufficiently complex organic solvent of ingredient of point.
Invention content
The technical problems to be solved by the invention are to provide a kind of small, easy to implement, high efficiency vacuum film of investment and do
The method of extractant in dry recycling coal base oil slag extract remainder.
To solve the above problems, extractant in a kind of vacuum film dried recovered coal base oil slag extract remainder of the present invention
Method, include the following steps：
(1) the class pitch class dregs of fat containing washing oil are added to by charging system I in level-one film drier, meanwhile, the level-one is thin
Conduction oil is passed through in the central shaft and housing of film drying machine and carries out indirectly heat；Under vacuum, by the light oil group in the dregs of fat
Divide and be evaporated, respectively obtain the dregs of fat and naphtha steam that washing oil content is 5% ~ 20%；
(2) the dregs of fat that the washing oil content is 5% ~ 20% are added to by charging system II in two level film drier, meanwhile, it is described
Conduction oil is passed through in the central shaft and housing of two level film drier and carries out indirectly heat；It under vacuum, will be in the dregs of fat
Heavy oil component is evaporated, and respectively obtains the dregs of fat and heavy oil steam that washing oil content is 5% ~ 0.5%；
Pipeline A with spray of the naphtha steam through being obliquely installed is sent in light oil scrubbing tower, meanwhile, cooling water A warps
Heat exchanger I, light oil washing pump are passed through in the light oil scrubbing tower and the naphtha steam are cooled down, and pass through tower inner venturi tube
Ejector action, remove a large amount of dust, respectively obtain non-condensing naphtha steam and a small amount of dust A and light oil liquid；It is described not
Condensation naphtha steam and a small amount of dust A are then entered by bottom of towe in spray column under the swabbing action of vacuum pump；The light oil liquid
By light oil washing pumped by heat exchanger I cooling, 30 DEG C ~ 100 DEG C of light oil is obtained, this 30 DEG C ~ 100 DEG C light
Tower top spray liquid of the part as the light oil scrubbing tower in oil, another part are sent to described in heavy oil washing column overhead conduct
The spray liquid of heavy oil scrubbing tower；
(3) the dregs of fat that the washing oil content is 5% ~ 0.5% are directly discharged in intermediate storage bin, and cold through the feeding film of blocking valve I
But in machine；Meanwhile cooling water B is passed through in the film cooling machine and the dregs of fat that the washing oil content is 5% ~ 0.5% is cooled down,
30 DEG C ~ 100 DEG C of the dregs of fat are obtained, this 30 DEG C ~ 100 DEG C of the dregs of fat are discharged into subsequent technique by blocking valve II；
Pipeline B with spray of the heavy oil steam through being obliquely installed is sent in the heavy oil scrubbing tower, meanwhile, cooling water
C is passed through in the heavy oil scrubbing tower through heat exchanger II, heavy oil washing pump and the heavy oil steam is cooled down, and passes through Ta Neiwenqiu
In pipe ejector action, remove a large amount of dust, respectively obtain non-condensing naphtha steam and a small amount of dust B and heavy oil liquid；Institute
It states non-condensing naphtha steam and a small amount of dust B is then entered by bottom of towe in spray column under the swabbing action of the vacuum pump；It is described
Heavy oil liquid washs pumped through the heavy oil and cools down by the heat exchanger II, obtains 30 DEG C ~ 100 DEG C of heavy oil, this 30 DEG C ~
Tower top spray liquid of the part as the heavy oil scrubbing tower in 100 DEG C of heavy oil, another part are discharged as washing oil production
Product are sent to follow-up workshop section；
(4) the non-condensing naphtha steam and a small amount of dust A and the non-condensing naphtha steam and a small amount of dust B are in the spray
Mixing washing oil steam is formed after being mixed in tower, meanwhile, cooling water D is entered by the tower top of the spray column, through mixing steaming with described
After vapour is in direct contact, the washing oil and fixed gas of condensation are respectively obtained；The fixed gas is emptied through the vacuum pump；
(5) the washing oil of the condensation is sent by spray pumped through the spray column bottom of towe and further cooled down into heat exchanger III, is obtained
30 DEG C ~ 100 DEG C of washing oil, the part in this 30 DEG C ~ 100 DEG C of washing oil are sent to the spray column overhead and do spray liquid, separately
A part is discharged as washing oil product and send to follow-up workshop section.
The operating pressure of the level-one film drier is -10 ~ -90KPa, operation temperature is 120 ~ 240 DEG C.
The operating pressure of the two level film drier is -15 ~ -95KPa, operation temperature is 120 ~ 270 DEG C.
The heat medium of the level-one film drier and the two level film drier is steam or conduction oil.
The light oil scrubbing tower is single spraying leaching or more spray venturi spray towers with the heavy oil scrubbing tower.
The spray column refers to one kind in perforated plate tower, packed tower or spray column.
The heat exchanger I, the heat exchanger II and the heat exchanger III are spiral heat exchanger or floating head type tubular
Heat exchanger.
：The light oil scrubbing tower, the heavy oil scrubbing tower, the spray column operating pressure be -10 ~ -95KPa.
The charging system I and the charging system II refer to one kind in plunger pump, screw pump or screw conveyor or
It is several.
Compared with the prior art, the present invention has the following advantages：
1st, the material that the present invention enters film drier enhances heat transfer and biography under the rotation stirring action of the hot axis of drying machine
Matter is easily dried material, and fugitive constituent is easy to volatilize, and drying time is short.
2nd, the dynamic equipment such as drying machine of the present invention is negative-pressure operation, effectively prevent letting out for dust and toxic gas
Dew.
3rd, contained dust is tiny in dry light steam and viscosity is big, easily blocks naphtha steam conveyance conduit, therefore, this hair
Bright middle naphtha steam conveyance conduit is obliquely installed and is equipped with pipeline spray, effectively prevent the blocking of pipeline.
4th, the film drier that the present invention uses can make material be mixed, dried to greatest extent, and thermal medium passes in and out
Smoothness will not generate dead zone, be uniformly mixed, and shaft power is small, greatly improve the thermal efficiency of drying machine.
5th, the present invention invests small, easy to implement, high efficiency.
Description of the drawings
The specific embodiment of the present invention is described in further detail below in conjunction with the accompanying drawings.
Fig. 1 is the process flow chart of the present invention.
In figure：1- charging systems I；2- level-one film driers；3- charging systems II；4- two level film driers；In 5-
Between storage bin；6- blocking valves I；7- film cooling machines；8- blocking valves II；9- light oil scrubbing towers；10- heat exchanger Is；11- light oil is washed
Wash pump；12- heavy oil scrubbing towers；13- heat exchanger IIs；14- heavy oil washing pumps；15- vacuum pumps；16- heat exchangers III；17- spray columns；
18- spray pumps.
Specific embodiment
As shown in Figure 1, in a kind of vacuum film dried recovered coal base oil slag extract remainder extractant method, including following step
Suddenly：
(1) the class pitch class dregs of fat containing washing oil are added to by charging system I 1 in level-one film drier 2, meanwhile, level-one film
Conduction oil is passed through in the central shaft and housing of drying machine 2 and carries out indirectly heat；Under the conditions of vacuum degree is -60 KPa, by the dregs of fat
In light oil constituents be evaporated, respectively obtain washing oil content be 5% ~ 20% the dregs of fat and naphtha steam.
Wherein：Level-one film drier 2（The patent No.：201420010597.3）Operating pressure for -10 ~ -90KPa, behaviour
It is 120 ~ 240 DEG C to make temperature, and heat medium is steam or conduction oil.
Charging system I 1 refers to one or more of plunger pump, screw pump or screw conveyor.
(2) the dregs of fat that washing oil content is 5% ~ 20% are added to by charging system II 3 in two level film drier 4, meanwhile, two
Conduction oil, which is passed through, in the central shaft and housing of grade film drier 4 carries out indirectly heat；Under the conditions of vacuum degree is -60 KPa,
Heavy oil component in the dregs of fat is evaporated, respectively obtains the dregs of fat and heavy oil steam that washing oil content is 5% ~ 0.5%.Wherein：Two
Grade film drier 4（The patent No.：201420010597.3）Operating pressure be -15 ~ -95KPa, operation temperature for 120 ~
270 DEG C, heat medium is steam or conduction oil.Charging system II 3 refers to one in plunger pump, screw pump or screw conveyor
Kind is several.
Pipeline A with spray of the naphtha steam through being obliquely installed is sent in light oil scrubbing tower 9, meanwhile, cooling water A warps
Heat exchanger I 10, light oil washing pump 11 are passed through in light oil scrubbing tower 9 and naphtha steam are cooled down, and pass through tower inner venturi tube
Ejector action removes a large amount of dust, respectively obtains non-condensing naphtha steam and a small amount of dust A and light oil liquid；It is non-condensing light
Oil vapour and a small amount of dust A are then entered by bottom of towe in spray column 17 under the swabbing action of vacuum pump 15；Light oil liquid is by light oil
The extraction of washing pump 11 cools down by heat exchanger I 10, obtains 30 DEG C ~ 100 DEG C of light oil, a part of in this 30 DEG C ~ 100 DEG C of light oil
As the tower top spray liquid of light oil scrubbing tower 9, another part is sent to 12 tower top of heavy oil scrubbing tower as heavy oil scrubbing tower 12
Spray liquid.
(3) the dregs of fat that washing oil content is 5% ~ 0.5% are directly discharged in intermediate storage bin 5, and be sent into film through blocking valve I 6
In cooler 7；Meanwhile cooling water B is passed through in film cooling machine 7 and the dregs of fat that washing oil content is 5% ~ 0.5% is cooled down, and obtains
30 DEG C ~ 100 DEG C of the dregs of fat, this 30 DEG C ~ 100 DEG C of the dregs of fat are discharged into subsequent technique by blocking valve II 8.Wherein：Film is cold
But machine 7（The patent No.：201420010597.3）.
Pipeline B with spray of the heavy oil steam through being obliquely installed is sent in heavy oil scrubbing tower 12, meanwhile, cooling water C
Counterweight oil vapour in heavy oil scrubbing tower 12 is passed through through heat exchanger II 13, heavy oil washing pump 14 to be cooled down, and passes through venturi in tower
The ejector action of pipe removes a large amount of dust, respectively obtains non-condensing naphtha steam and a small amount of dust B and heavy oil liquid；It does not coagulate
Knot naphtha steam and a small amount of dust B are then entered by bottom of towe in spray column 17 under the swabbing action of vacuum pump 15；Heavy oil liquid passes through
The extraction of heavy oil washing pump 14 cools down by heat exchanger II 13,30 DEG C ~ 100 DEG C of heavy oil is obtained, in this 30 DEG C ~ 100 DEG C of heavy oil
Tower top spray liquid of the part as heavy oil scrubbing tower 12, another part is discharged as washing oil product and send to follow-up workshop section.
(4) non-condensing naphtha steam and a small amount of dust A are mixed with non-condensing naphtha steam and a small amount of dust B in spray column 17
Mixing washing oil steam is formed after conjunction, meanwhile, cooling water D is entered by the tower top of spray column 17, after being in direct contact with mixed vapour,
Respectively obtain the washing oil and fixed gas of condensation；Fixed gas is emptied through vacuum pump 15；
(5) the washing oil condensed is sent through 17 bottom of towe of spray column by the extraction of spray pump 18 further to cool down into heat exchanger III 16, obtains 30
DEG C ~ 100 DEG C of washing oil, the part in this 30 DEG C ~ 100 DEG C of washing oil is sent to 17 tower top of spray column and does spray liquid, another portion
Point being discharged as washing oil product send to follow-up workshop section.
Light oil scrubbing tower 9 and heavy oil scrubbing tower 12 are single spraying leaching or more spray venturi spray towers in the present invention.
Spray column 17 refers to one kind in perforated plate tower, packed tower or spray column.
Light oil scrubbing tower 9, heavy oil scrubbing tower 12, spray column 17 operating pressure be -10 ~ -95KPa.
Heat exchanger I 10, heat exchanger II 13 and heat exchanger III 16 are spiral heat exchanger or float head heat-exchanger.
Claims (9)
1. the method for extractant, includes the following steps in a kind of vacuum film dried recovered coal base oil slag extract remainder：
(1) the class pitch class dregs of fat containing washing oil are by charging system I（1）It is added to level-one film drier（2）In, meanwhile, it is described
Level-one film drier（2）Central shaft and housing in be passed through conduction oil carry out indirectly heat；It under vacuum, will be in the dregs of fat
Light oil constituents be evaporated, respectively obtain washing oil content be 5% ~ 20% the dregs of fat and naphtha steam；
(2) the dregs of fat that the washing oil content is 5% ~ 20% are by charging system II（3）It is added to two level film drier（4）In, together
When, the two level film drier（4）Central shaft and housing in be passed through conduction oil carry out indirectly heat；Under vacuum,
Heavy oil component in the dregs of fat is evaporated, respectively obtains the dregs of fat and heavy oil steam that washing oil content is 5% ~ 0.5%；
Pipeline A with spray of the naphtha steam through being obliquely installed is sent to light oil scrubbing tower（9）In, meanwhile, cooling water A
Through heat exchanger I（10）, light oil washing pump（11）It is passed through the light oil scrubbing tower（9）In the naphtha steam is cooled down, lead to
The ejector action of tower inner venturi tube is crossed, removes a large amount of dust, respectively obtains non-condensing naphtha steam and a small amount of dust A and light
Fluid body；The non-condensing naphtha steam and a small amount of dust A are then in vacuum pump（15）Swabbing action under spray entered by bottom of towe
Tower（17）In；The light oil liquid is by the light oil washing pump（11）The heat exchanger I is passed through in extraction（10）Cooling, obtains 30 DEG C
~ 100 DEG C of light oil, a part is used as the light oil scrubbing tower in this 30 DEG C ~ 100 DEG C of light oil（9）Tower top spray liquid, it is another
Part is sent to heavy oil scrubbing tower（12）Tower top is as the heavy oil scrubbing tower（12）Spray liquid；
(3) the dregs of fat that the washing oil content is 5% ~ 0.5% are directly discharged to intermediate storage bin（5）In, and through blocking valve I（6）It is sent into
Film cooling machine（7）In；Meanwhile cooling water B is passed through the film cooling machine（7）In be 5% ~ 0.5% to the washing oil content
The dregs of fat are cooled down, and obtain 30 DEG C ~ 100 DEG C of the dregs of fat, this 30 DEG C ~ 100 DEG C of the dregs of fat pass through blocking valve II（8）After being discharged into
Continuous technique；
Pipeline B with spray of the heavy oil steam through being obliquely installed is sent to the heavy oil scrubbing tower（12）In, meanwhile, it is cold
But water C is through heat exchanger II（13）, heavy oil washing pump（14）It is passed through the heavy oil scrubbing tower（12）In to the heavy oil steam carry out
Cooling, by the ejector action of tower inner venturi tube, removes a large amount of dust, respectively obtains non-condensing naphtha steam and a small amount of powder
Dirt B and heavy oil liquid；The non-condensing naphtha steam and a small amount of dust B are then in the vacuum pump（15）Swabbing action under by tower
Bottom enters spray column（17）In；The heavy oil liquid is through the heavy oil washing pump（14）The heat exchanger II is passed through in extraction（13）Drop
Temperature obtains 30 DEG C ~ 100 DEG C of heavy oil, and the part in this 30 DEG C ~ 100 DEG C of heavy oil is as the heavy oil scrubbing tower（12）'s
Tower top spray liquid, another part are discharged as washing oil product and send to follow-up workshop section；
(4) the non-condensing naphtha steam and a small amount of dust A and the non-condensing naphtha steam and a small amount of dust B are in the spray
Tower（17）Mixing washing oil steam is formed after middle mixing, meanwhile, cooling water D is by the spray column（17）Tower top enter, through with institute
It states after mixed vapour is in direct contact, respectively obtains the washing oil and fixed gas of condensation；The fixed gas is through the vacuum pump（15）Row
It is empty；
(5) the washing oil of the condensation is through the spray column（17）Bottom of towe is by spray pump（18）Extraction is sent to heat exchanger III（16）In into
One step cools down, and obtains 30 DEG C ~ 100 DEG C of washing oil, the part in this 30 DEG C ~ 100 DEG C of washing oil is sent to the spray column
（17）Tower top does spray liquid, and another part is discharged as washing oil product and send to follow-up workshop section.
2. the method for extractant, special in a kind of vacuum film dried recovered coal base oil slag extract remainder as described in claim 1
Sign is：The level-one film drier（2）Operating pressure be -10 ~ -90KPa, operation temperature be 120 ~ 240 DEG C.
3. the method for extractant, special in a kind of vacuum film dried recovered coal base oil slag extract remainder as described in claim 1
Sign is：The two level film drier（4）Operating pressure be -15 ~ -95KPa, operation temperature be 120 ~ 270 DEG C.
4. the method for extractant, special in a kind of vacuum film dried recovered coal base oil slag extract remainder as described in claim 1
Sign is：The level-one film drier（2）With the two level film drier（4）Heat medium be steam or heat conduction
Oil.
5. the method for extractant, special in a kind of vacuum film dried recovered coal base oil slag extract remainder as described in claim 1
Sign is：The light oil scrubbing tower（9）With the heavy oil scrubbing tower（12）It is single spraying leaching or more spray venturi spray towers.
6. the method for extractant, special in a kind of vacuum film dried recovered coal base oil slag extract remainder as described in claim 1
Sign is：The spray column（17）Refer to one kind in perforated plate tower, packed tower or spray column.
7. the method for extractant, special in a kind of vacuum film dried recovered coal base oil slag extract remainder as described in claim 1
Sign is：The heat exchanger I（10）, the heat exchanger II（13）With the heat exchanger III（16）Be spiral heat exchanger or
Float head heat-exchanger.
8. the method for extractant, special in a kind of vacuum film dried recovered coal base oil slag extract remainder as described in claim 1
Sign is：The light oil scrubbing tower（9）, the heavy oil scrubbing tower（12）, the spray column（17）Operating pressure be -10
~-95KPa。
9. the method for extractant, special in a kind of vacuum film dried recovered coal base oil slag extract remainder as described in claim 1
Sign is：The charging system I（1）With the charging system II（3）Refer to one in plunger pump, screw pump or screw conveyor
Kind is several.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810001316.0A CN108130121B (en) | 2018-01-02 | 2018-01-02 | Method for recovering extractant from coal-based oil residue extraction residues through vacuum film drying |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810001316.0A CN108130121B (en) | 2018-01-02 | 2018-01-02 | Method for recovering extractant from coal-based oil residue extraction residues through vacuum film drying |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108130121A true CN108130121A (en) | 2018-06-08 |
| CN108130121B CN108130121B (en) | 2020-04-21 |
Family
ID=62399478
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810001316.0A Active CN108130121B (en) | 2018-01-02 | 2018-01-02 | Method for recovering extractant from coal-based oil residue extraction residues through vacuum film drying |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110229688A (en) * | 2019-04-21 | 2019-09-13 | 宁波市化工研究设计院有限公司 | The device and recovery method of spraying expansion drying recycling oil product or solvent are carried out containing solid oil product |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1492033A (en) * | 2002-10-24 | 2004-04-28 | 皇冠制铁公司 | Two stage device for removing solvent from food granular powder |
| CN103242881A (en) * | 2013-05-30 | 2013-08-14 | 神华集团有限责任公司 | Method for separating bituminous substances from coal direct liquefaction residues |
| CN104560121A (en) * | 2013-10-10 | 2015-04-29 | 天华化工机械及自动化研究设计院有限公司 | Method and device for recovering extractant in coal-based oil dreg extraction residue |
| CN205925038U (en) * | 2016-08-19 | 2017-02-08 | 河南省亚临界生物技术有限公司 | Continuous vaporization system of subcritical extract |
-
2018
- 2018-01-02 CN CN201810001316.0A patent/CN108130121B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1492033A (en) * | 2002-10-24 | 2004-04-28 | 皇冠制铁公司 | Two stage device for removing solvent from food granular powder |
| CN103242881A (en) * | 2013-05-30 | 2013-08-14 | 神华集团有限责任公司 | Method for separating bituminous substances from coal direct liquefaction residues |
| CN104560121A (en) * | 2013-10-10 | 2015-04-29 | 天华化工机械及自动化研究设计院有限公司 | Method and device for recovering extractant in coal-based oil dreg extraction residue |
| CN205925038U (en) * | 2016-08-19 | 2017-02-08 | 河南省亚临界生物技术有限公司 | Continuous vaporization system of subcritical extract |
Non-Patent Citations (2)
| Title |
|---|
| 王晓伟等: "真空薄膜干燥机回收煤液化残渣萃余物中萃取剂的应用研究", 《煤化工》 * |
| 高妍等: "煤直接液化残渣萃余物中萃取剂回收技术研究", 《洁净煤技术》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110229688A (en) * | 2019-04-21 | 2019-09-13 | 宁波市化工研究设计院有限公司 | The device and recovery method of spraying expansion drying recycling oil product or solvent are carried out containing solid oil product |
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| Publication number | Publication date |
|---|---|
| CN108130121B (en) | 2020-04-21 |
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