CN103146424A - Method for producing fuel oil and lubricant base oil by hydrogenating all fractions of coal tar - Google Patents
Method for producing fuel oil and lubricant base oil by hydrogenating all fractions of coal tar Download PDFInfo
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Abstract
The invention relates to a method for producing fuel oil and lubricant base oil by hydrogenating all fractions of coal tar. The method comprises the following steps of: performing pressure reduction on the all fractions of coal tar by virtue of a pressure reduction valve after hydroprocessing on the all fractions of coal tar is finished, and flashing to separate out a light product and a heavy product; performing isodewaxing on the heavy product; and fractioning the heavy product, successively together with the light product, through a heat high fraction separator, a cold high fraction separator, a cold low fraction separator and a fraction tower to obtain the fuel oil and the lubricant base oil which are good in quality and meet a state standard request. The method is simple in process procedures, easy to control, and safe and stable in operation; and the all fractions of coal tar can be scientifically and reasonably utilized, the production economic benefit is further improved, and a certain active function in overcoming the defect of the fuel oil and the lubricant base oil in China is achieved.
Description
Technical field
The invention belongs to coal chemical technology, be specifically related to a kind of method of full cut preparing fuel oil by coal tar hydrogenation and lubricant base.
Background technology
In the last few years, the fast development of China's preparing fuel oil by coal tar hydrogenation industry had certain meaning to alleviating the China's oil shortage.
China has realized that at present industrial coal tar hydrogenating technology mainly contains: and the benzoline of coal tar (＜370 ℃) hydrogenation technique, delay coking of coal tar hydrogenation combination technique, full cut coal tar hydrogenation process (Zhang Xiaojing. middle coalite tar hydrogen addition technology, the coal journal, 2011, the 5th phase 840-844).But in actual production process, can by-product the coal tar hydrogenating tail oil of 8% left and right, normally with its export trade at a low price, further rationally do not utilize, do not make its production economy benefit be difficult to further raising.In addition along with the fast development of the industries such as China's automobile, machinery, communications and transportation, China has now become the second-biggest-in-the-world lubricating oil country of consumption that is only second to the U.S., and the main body of lubricating oil is lubricant base, but the raw material of production basis oil is oil, due to the shortage of China's oil resource, cause China's base oil under-supply.Therefore, seek the important topic that method that the full cut preparing fuel oil by coal tar hydrogenation of a kind of use can also the coproduction lubricant base becomes research.
Summary of the invention
The existing deficiency of technique for existing preparing fuel oil with coal oil hydrogenation the invention provides a kind of technical process simple, and is easy to control, good product quality, the full cut preparing fuel oil by coal tar hydrogenation that safe operation is stable and the method for lubricant base.
The present invention solves the problems of the technologies described above the technical scheme that adopts and is comprised of following steps:
(1) the slag aftertreatment of according to a conventional method full cut coal tar being dewatered;
(2) take off after slag full cut coal tar with send in the first hydrogenator after hydrogen mixes; the temperature in of hydrogenation protecting agent is 230～240 ℃; the temperature of reaction of hydrodemetallation (HDM) agent is 240～260 ℃, and pressure is 12～18MPa, and the liquid air speed is 0.2～0.9h
-1, oily hydrogen volume is sent in the second hydrogenator than 1:1500～2600, and the temperature of reaction of hydrogen desulfurization agent is 310～350 ℃, and the temperature of reaction of catalyst for hydro-upgrading is 380～420 ℃, and pressure is 12～18MPa, the liquid air speed is 0.2～0.9h
-1, oily hydrogen volume is than 1:1500～2600, and imurity-removal in hydrogenator obtains hydrogenation products;
(3) hydrogenation products separates lighter products in flashing tower after by the reducing valve step-down with heavy product, lighter products enters hot high score separator by pipeline from the top exit of flashing tower, heavy product is entered in refining isomerization dewaxing reactor by pipeline by the flashing tower outlet at bottom and reacts, temperature of reaction is 360～400 ℃, pressure is 10～16.5MPa, and the liquid air speed is 0.2～0.9h
-1, oily hydrogen volume is than being 1:1500～2600, reaction product enters in hot high score separator by pipeline mixes with the lighter products of flashing tower output, and isolates gas-phase product and liquid product in hot high score separator;
(4) gas-phase product enters cold high score separator by pipeline, isolating hydrogen in cold high score separator turns back to by pipeline in hydrogenator and isomerization dewaxing reactor, the high score oil of separating enters in cold low minute separator by pipeline, isolating low minute oil in separator in cold low minute and separating the isolated liquid product of hot high score separator is mixed into separation column in pipeline in, make oil fuel and lubricant base.
Above-mentioned full cut coal tar is coalite tar, coal-tar middle oil or coal-tar heavy oil.
In above-mentioned steps (2); take off after slag full cut coal tar with send in the first hydrogenator after hydrogen mixes; optimum condition is: oily hydrogen volume compares 1:1500; the temperature in of hydrogenation protecting agent is 230 ℃; the temperature of reaction of hydrodemetallation (HDM) agent is 250 ℃; pressure is 14MPa, and the liquid air speed is 0.2h
-1, to send in the second hydrogenator, oily hydrogen volume is than 1:1500, and the temperature of reaction of hydrogen desulfurization agent is 320 ℃, and the temperature of reaction of catalyst for hydro-upgrading is 390 ℃, and pressure is 14MPa, the liquid air speed is 0.2h
-1, imurity-removal in hydrogenator obtains hydrogenation products.
In above-mentioned steps (3), hydrogenation products by the reducing valve step-down after in flashing tower lighter products separate with heavy product, lighter products enters hot high score separator by pipeline from the top exit of flashing tower, heavy product is entered in refining isomerization dewaxing reactor by pipeline by the flashing tower outlet at bottom and reacts, optimum condition is: oily hydrogen volume is than being 1:1700, temperature of reaction is 370 ℃, and pressure is 12MPa, and the liquid air speed is 0.4h
-1, reaction product enters in hot high score separator by pipeline mixes with the lighter products of flashing tower output, and isolates gas-phase product and liquid product in hot high score separator.
the method of full cut preparing fuel oil by coal tar hydrogenation of the present invention and lubricant base is to go out lighter products and heavy product by flash separation after the reducing valve step-down after full cut coal tar hydrogenating is processed, the further isomerization dewaxing of heavy product, again with lighter products in succession through overheated, cold high score separator, cold low minute separator and separation column fractionation, thereby it is good to obtain quality, the oil fuel and the lubricant base that are up to state standards and require, and technical process of the present invention is simple, easy to control, operating safety is stable and not only can make full cut coal tar obtain scientific and reasonable utilization, further improved the production economy benefit, and the deficiency of alleviating China's lubricant base had certain active effect.
Description of drawings
Fig. 1 is the process flow sheet of embodiment 1.
Embodiment
Now by reference to the accompanying drawings technical scheme of the present invention is further illustrated, but the present invention is not limited only to following embodiment.
Now take full cut coalite tar 1 as example, referring to Fig. 1, the method for Hydrogenation oil fuel and lubricant base is comprised of following steps:
(1) the slag aftertreatment of according to a conventional method full cut coalite tar 1 being dewatered;
(2) take off after slag coalite tar 1 with send in the first hydrogenator 3 after hydrogen 2 mixes; filling TK-10 hydrogenation protecting agent (Topsoe company), RN-5030 hydrodemetallation (HDM) agent (Criterion company) in the first hydrogenator 3; the temperature in of TK-10 hydrogenation protecting agent is 230 ℃; the temperature of reaction of RN-5030 hydrodemetallation (HDM) agent is 240 ℃; pressure is 12MPa, and the liquid air speed is 0.3h
-1The oil hydrogen volume compares 1:1500, send in the second hydrogenator 4 after having reacted, add dress ICR-137 hydrogen desulfurization agent (Chevron company), TK-555 catalyst for hydro-upgrading (Topsoe company) in the second hydrogenator 4, the temperature of reaction of ICR-137 hydrogen desulfurization agent is 310 ℃, the temperature of reaction of TK-555 catalyst for hydro-upgrading is 380 ℃, and pressure is 12MPa, and the liquid air speed is 0.3h
-1, oily hydrogen volume removes the impurity such as metal, sulphur, nitrogen than 1:1500, obtains hydrogenation products;
(3) hydrogenation products is sent in flashing tower 6 after by reducing valve 5 step-downs, in flashing tower 6, the lighter products such as water, ammonia and lighter hydrocarbons are separated with heavy product, lighter products enters hot high score separator 8 by pipeline from the outlet at flashing tower 6 tops, heavy product is entered in refining isomerization dewaxing reactor 7 in isomerization dewaxing catalyst ICR-142(Chevron company by pipeline by the outlet of flashing tower 6 bottoms) katalysis under carry out the isocracking reaction, temperature of reaction is 360 ℃, pressure is 10MPa, and the liquid air speed is 0.2h
-1, oily hydrogen volume is than being 1:1500, reaction product enters in hot high score separator 8 by pipeline mixes with the lighter products of flashing tower 6 outputs, and isolates gas-phase product and liquid product in hot high score separator 8;
(4) gas-phase product enters cold high score separator 9 by pipeline, isolate hydrogen 2 and turn back to first by pipeline in cold high score separator 9, the second hydrogenator 3, 4 and isomerization dewaxing reactor 7 in, carry out recycle, enter by pipeline in cold low minute separator 10 at the high score oil that cold high score separator 9 is separated, recycle in sending into device for producing hydrogen by pipeline isolating low minute gas 11 in cold low minute in separator 10, isolated low minute oil of cold low minute separator 10 is mixed in pipeline in separation column 10 with the isolated liquid product of hot high score separator 8 and separates, make oil fuel and lubricant base 14.This oil fuel is mainly gasoline fraction 12 and diesel oil distillate 13, and the saline sewage 15 of cold high score separator 9 and cold low minute separator 10 bottoms enters device for producing hydrogen by pipeline and recycles.
Now take full cut coalite tar 1 as example, the method for Hydrogenation oil fuel and lubricant base is comprised of following steps:
(1) the slag aftertreatment of according to a conventional method full cut coalite tar 1 being dewatered;
(2) take off after slag coalite tar 1 with send in the first hydrogenator 3 after hydrogen 2 mixes; the agent of filling hydrogenation protecting, hydrodemetallation (HDM) agent in the first hydrogenator 3; the temperature in of hydrogenation protecting agent is 230 ℃; the temperature of reaction of hydrodemetallation (HDM) agent is 250 ℃; pressure is 14MPa, and the liquid air speed is 0.2h
-1The oil hydrogen volume compares 1:1500, send in the second hydrogenator 4 after having reacted, add dress hydrogen desulfurization agent, catalyst for hydro-upgrading in the second hydrogenator 4, the temperature of reaction of hydrogen desulfurization agent is 320 ℃, the temperature of reaction of catalyst for hydro-upgrading is 390 ℃, and pressure is 14MPa, and the liquid air speed is 0.2h
-1, oily hydrogen volume removes the impurity such as metal, sulphur, nitrogen than 1:1500, obtains hydrogenation products;
(3) hydrogenation products is sent in flashing tower 6 after by reducing valve 5 step-downs, in flashing tower 6, the lighter products of the compositions such as water, ammonia and lighter hydrocarbons is separated with heavy product, lighter products enters hot high score separator 8 by pipeline from the outlet at flashing tower 6 tops, heavy product is entered by pipeline by the outlet of flashing tower 6 bottoms and carry out the isocracking reaction in refining isomerization dewaxing reactor 7 under the katalysis of isomerization dewaxing catalyst, temperature of reaction is 370 ℃, pressure is 12MPa, and the liquid air speed is 0.4h
-1, oily hydrogen volume is than being 1:1700, reaction product enters in hot high score separator 8 by pipeline mixes with the lighter products of flashing tower 6 outputs, and isolates gas-phase product and liquid product in hot high score separator 8;
Step (4) is identical with embodiment 1, makes oil fuel and lubricant base.
Embodiment 3
Now take full cut coalite tar 1 as example, the method for Hydrogenation oil fuel and lubricant base is comprised of following steps:
(1) the slag aftertreatment of according to a conventional method full cut coalite tar 1 being dewatered;
(2) take off after slag coalite tar 1 with send in the first hydrogenator 3 after hydrogen 2 mixes; the agent of filling hydrogenation protecting, hydrodemetallation (HDM) agent in the first hydrogenator 3; the temperature in of hydrogenation protecting agent is 240 ℃; the temperature of reaction of hydrodemetallation (HDM) agent is 260 ℃; pressure is 16MPa, and the liquid air speed is 0.5h
-1The oil hydrogen volume compares 1:1800, send in the second hydrogenator 4 after having reacted, add dress hydrogen desulfurization agent, catalyst for hydro-upgrading in the second hydrogenator 4, the temperature of reaction of hydrogen desulfurization agent is 330 ℃, the temperature of reaction of catalyst for hydro-upgrading is 400 ℃, and pressure is 16MPa, and the liquid air speed is 0.5h
-1, oily hydrogen volume removes the impurity such as metal, sulphur, nitrogen than 1:1800, obtains hydrogenation products;
(3) hydrogenation products is sent in flashing tower 6 after by reducing valve 5 step-downs, in flashing tower 6, the lighter products of the compositions such as water, ammonia and lighter hydrocarbons is separated with heavy product, lighter products enters hot high score separator 8 by pipeline from the outlet at flashing tower 6 tops, heavy product is entered by pipeline by the outlet of flashing tower 6 bottoms and carry out the isocracking reaction in refining isomerization dewaxing reactor 7 under the katalysis of isomerization dewaxing catalyst, temperature of reaction is 420 ℃, pressure is 14MPa, and the liquid air speed is 0.6h
-1, oily hydrogen volume is than being 1:2200, reaction product enters in hot high score separator 8 by pipeline mixes with the lighter products of flashing tower 6 outputs, and isolates gas-phase product and liquid product in hot high score separator 8;
Step (4) is identical with embodiment 1, makes oil fuel and lubricant base.
Embodiment 4
In the present embodiment; step (2) take off after slag coalite tar 1 with send in the first hydrogenator 3 after hydrogen 2 mixes; the agent of filling hydrogenation protecting, hydrodemetallation (HDM) agent in the first hydrogenator 3; the temperature in of hydrogenation protecting agent is 230 ℃; the temperature of reaction of hydrodemetallation (HDM) agent is 250 ℃; pressure is 18MPa, and the liquid air speed is 0.9h
-1The oil hydrogen volume compares 1:2600, send in the second hydrogenator 4 after having reacted, add dress hydrogen desulfurization agent, catalyst for hydro-upgrading in the second hydrogenator 4, the temperature of reaction of hydrogen desulfurization agent is 350 ℃, the temperature of reaction of catalyst for hydro-upgrading is 420 ℃, and pressure is 18MPa, and the liquid air speed is 0.9h
-1, oily hydrogen volume removes the impurity such as metal, sulphur, nitrogen than 1:2600, obtains hydrogenation products;
(3) hydrogenation products is sent in flashing tower 6 after by reducing valve 5 step-downs, in flashing tower 6, the lighter products of the compositions such as water, ammonia and lighter hydrocarbons is separated with heavy product, lighter products enters hot high score separator 8 by pipeline from the outlet at flashing tower 6 tops, heavy product is entered in refining isomerization dewaxing reactor 7 by pipeline by the outlet of flashing tower 6 bottoms and reacts under the katalysis of isomerization dewaxing catalyst, temperature of reaction is 400 ℃, pressure is 16.5MPa, and the liquid air speed is 0.9h
-1, oily hydrogen volume is than being 1:2600, reaction product enters in hot high score separator 8 by pipeline mixes with the lighter products of flashing tower 6 outputs, and isolates gas-phase product and liquid product in hot high score separator 8;
Other step is identical with embodiment 1, makes oil fuel and lubricant base.
In the present embodiment; step (2) take off after slag coalite tar 1 with send in the first hydrogenator 3 after hydrogen 2 mixes; the agent of filling hydrogenation protecting, hydrodemetallation (HDM) agent in the first hydrogenator 3; the temperature in of hydrogenation protecting agent is 230 ℃; the temperature of reaction of hydrodemetallation (HDM) agent is 240 ℃; pressure is 15MPa, and the liquid air speed is 0.7h
-1The oil hydrogen volume compares 1:2200, send in the second hydrogenator 4 after having reacted, add dress hydrogen desulfurization agent, catalyst for hydro-upgrading in the second hydrogenator 4, the temperature of reaction of hydrogen desulfurization agent is 330 ℃, the temperature of reaction of catalyst for hydro-upgrading is 410 ℃, and pressure is 15MPa, and the liquid air speed is 0.7h
-1, oily hydrogen volume removes the impurity such as metal, sulphur, nitrogen than 1:2200, obtains hydrogenation products;
(3) hydrogenation products is sent in flashing tower 6 after by reducing valve 5 step-downs, in flashing tower 6, the lighter products of the compositions such as water, ammonia and lighter hydrocarbons is separated with heavy product, lighter products enters hot high score separator 8 by pipeline from the outlet at flashing tower 6 tops, heavy product is entered by pipeline by the outlet of flashing tower 6 bottoms and carry out the isocracking reaction in refining isomerization dewaxing reactor 7 under the katalysis of isomerization dewaxing catalyst, temperature of reaction is 395 ℃, pressure is 14MPa, and the liquid air speed is 0.6h
-1, oily hydrogen volume is than being 1:2000, reaction product enters in hot high score separator 8 by pipeline mixes with the lighter products of flashing tower 6 outputs, and isolates gas-phase product and liquid product in hot high score separator 8;
Other step is identical with embodiment 1, makes oil fuel and lubricant base.
In the present embodiment; step (2) take off after slag coalite tar 1 with send in the first hydrogenator 3 after hydrogen 2 mixes; the agent of filling hydrogenation protecting, hydrodemetallation (HDM) agent in the first hydrogenator 3; the temperature in of hydrogenation protecting agent is 230 ℃; the temperature of reaction of hydrodemetallation (HDM) agent is 240 ℃; pressure is 13MPa, and the liquid air speed is 0.4h
-1The oil hydrogen volume compares 1:1700, send in the second hydrogenator 4 after having reacted, add dress hydrogen desulfurization agent, catalyst for hydro-upgrading in the second hydrogenator 4, the temperature of reaction of hydrogen desulfurization agent is 310 ℃, the temperature of reaction of catalyst for hydro-upgrading is 380 ℃, and pressure is 13MPa, and the liquid air speed is 0.4h
-1, oily hydrogen volume removes the impurity such as metal, sulphur, nitrogen than 1:1700, obtains hydrogenation products;
(3) hydrogenation products is sent in flashing tower 6 after by reducing valve 5 step-downs, in flashing tower 6, the lighter products of the compositions such as water, ammonia and lighter hydrocarbons is separated with heavy product, lighter products enters hot high score separator 8 by pipeline from the outlet at flashing tower 6 tops, heavy product is entered by pipeline by the outlet of flashing tower 6 bottoms and carry out the isocracking reaction in refining isomerization dewaxing reactor 7 under the katalysis of isomerization dewaxing catalyst, temperature of reaction is 360 ℃, pressure is 11MPa, and the liquid air speed is 0.2h
-1, oily hydrogen volume is than being 1:1500, reaction product enters in hot high score separator 8 by pipeline mixes with the lighter products of flashing tower 6 outputs, and isolates gas-phase product and liquid product in hot high score separator 8;
Other step is identical with embodiment 1, makes oil fuel and lubricant base.
Embodiment 7
In above-described embodiment 1～6, the full cut coal-tar middle oil of the full cut coalite tar 1 use equivalent of raw material or the coal-tar heavy oil of full cut to be replaced, other step is identical with corresponding embodiment, makes oil fuel and lubricant base.
According to national standard " motor spirit " (GB/T17930-2006), " derv fuel oil " (GB/T19147-2003) and " all-purpose engine oil base oil " Q/SY44-2009(HVI-400) in to the relevant regulations of the specification of quality of corresponding motor spirit, derv fuel oil and lubricant base, the contriver is according to detecting according to the standard relevant regulations respectively the prepared gasoline fraction of embodiment 1, diesel oil distillate, lubricant base, and result is respectively as following table 1, table 2, table 3:
The main character of gasoline fraction in table 1 embodiment 1
The main character of diesel oil distillate in table 2 embodiment 1
The main character of lubricant base in table 3 embodiment 1
Can be found out by upper table 1, table 2, table 3, above-mentioned every detection of gasoline fraction, diesel oil distillate and lubricant base that embodiment 1 is prepared all meets the regulation of relevant national standard.The quality of the oil fuel that makes of embodiment 1, lubricant base is good thus.
Claims (4)
1. the method for a full cut preparing fuel oil by coal tar hydrogenation and lubricant base is characterized in that being comprised of following steps:
(1) the slag aftertreatment of according to a conventional method full cut coal tar being dewatered;
(2) take off after slag full cut coal tar with send in the first hydrogenator after hydrogen mixes; the oil hydrogen volume is than 1:1500～2600; the temperature in of hydrogenation protecting agent is 230～240 ℃; the temperature of reaction of hydrodemetallation (HDM) agent is 240～260 ℃; pressure is 12～18MPa, and the liquid air speed is 0.2～0.9h
-1, to send in the second hydrogenator, oily hydrogen volume is than 1:1500～2600, and the temperature of reaction of hydrogen desulfurization agent is 310～350 ℃, and the temperature of reaction of catalyst for hydro-upgrading is 380～420 ℃, and pressure is 12～18MPa, the liquid air speed is 0.2～0.9h
-1, imurity-removal in hydrogenator obtains hydrogenation products;
(3) hydrogenation products by the reducing valve step-down after in flashing tower lighter products separate with heavy product, lighter products enters hot high score separator by pipeline from the top exit of flashing tower, heavy product is entered in refining isomerization dewaxing reactor by pipeline by the flashing tower outlet at bottom and reacts, temperature of reaction is 360～400 ℃, pressure is 10～16.5MPa, and the liquid air speed is 0.2～0.9h
-1, oily hydrogen volume is than being 1:1500～2600, reaction product enters in hot high score separator by pipeline mixes with the lighter products of flashing tower output, and isolates gas-phase product and liquid product in hot high score separator;
(4) gas-phase product enters cold high score separator by pipeline, isolating hydrogen in cold high score separator turns back to by pipeline in hydrogenator and isomerization dewaxing reactor, the high score oil of separating enters in cold low minute separator by pipeline, isolating low minute oil in separator in cold low minute and separating the isolated liquid product of hot high score separator is mixed into separation column in pipeline in, make oil fuel and lubricant base.
2. the method for full cut preparing fuel oil by coal tar hydrogenation according to claim 1 and lubricant base, it is characterized in that: described full cut coal tar is coalite tar, coal-tar middle oil or coal-tar heavy oil.
3. the method for full cut preparing fuel oil by coal tar hydrogenation according to claim 1 and lubricant base; it is characterized in that: in step (2); take off after slag full cut coal tar with send in the first hydrogenator after hydrogen mixes; the oil hydrogen volume compares 1:1500; the temperature in of hydrogenation protecting agent is 230 ℃; the temperature of reaction of hydrodemetallation (HDM) agent is 250 ℃, and pressure is 14MPa, and the liquid air speed is 0.2h
-1, to send in the second hydrogenator, oily hydrogen volume is than 1:1500, and the temperature of reaction of hydrogen desulfurization agent is 320 ℃, and the temperature of reaction of catalyst for hydro-upgrading is 390 ℃, and pressure is 14MPa, the liquid air speed is 0.2h
-1, imurity-removal in hydrogenator obtains hydrogenation products.
4. the method for full cut preparing fuel oil by coal tar hydrogenation according to claim 1 and lubricant base, it is characterized in that: in step (3), hydrogenation products by the reducing valve step-down after in flashing tower lighter products separate with heavy product, lighter products enters hot high score separator by pipeline from the top exit of flashing tower, heavy product is entered in refining isomerization dewaxing reactor by pipeline by the flashing tower outlet at bottom and reacts, the oil hydrogen volume is than being 1:1700, temperature of reaction is 370 ℃, pressure is 12MPa, and the liquid air speed is 0.4h
-1, reaction product enters in hot high score separator by pipeline mixes with the lighter products of flashing tower output, and isolates gas-phase product and liquid product in hot high score separator.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103436290A (en) * | 2013-09-13 | 2013-12-11 | 王树宽 | Method for producing naphthenic base refrigerating machine oil base oil by using coal tar oil |
| CN107090307A (en) * | 2017-06-13 | 2017-08-25 | 邯郸鑫盛能源科技有限公司 | A kind of method of hydrogenation of high temperature coal tar |
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| US4855037A (en) * | 1984-09-12 | 1989-08-08 | Nippon Kokan Kabushiki Kaisha | Hydrogenation catalyst for coal tar, a method of hydrogenation of coal tar with use of such catalyst, and a method of producing super needle coke from the hydrogenation product of coal tar |
| CN1952070A (en) * | 2005-10-19 | 2007-04-25 | 中国石油化工股份有限公司 | Method for producing cleaning oil from coal-tar oil |
| CN101781577A (en) * | 2009-12-21 | 2010-07-21 | 曲靖众一精细化工股份有限公司 | Method for producing lightweight fuel oil by utilizing mixed coal tar |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US4855037A (en) * | 1984-09-12 | 1989-08-08 | Nippon Kokan Kabushiki Kaisha | Hydrogenation catalyst for coal tar, a method of hydrogenation of coal tar with use of such catalyst, and a method of producing super needle coke from the hydrogenation product of coal tar |
| CN1952070A (en) * | 2005-10-19 | 2007-04-25 | 中国石油化工股份有限公司 | Method for producing cleaning oil from coal-tar oil |
| CN101781577A (en) * | 2009-12-21 | 2010-07-21 | 曲靖众一精细化工股份有限公司 | Method for producing lightweight fuel oil by utilizing mixed coal tar |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103436290A (en) * | 2013-09-13 | 2013-12-11 | 王树宽 | Method for producing naphthenic base refrigerating machine oil base oil by using coal tar oil |
| CN103436290B (en) * | 2013-09-13 | 2015-05-27 | 王树宽 | Method for producing naphthenic base refrigerating machine oil base oil by using coal tar oil |
| CN107090307A (en) * | 2017-06-13 | 2017-08-25 | 邯郸鑫盛能源科技有限公司 | A kind of method of hydrogenation of high temperature coal tar |
| CN107090307B (en) * | 2017-06-13 | 2019-10-11 | 邯郸鑫盛能源科技有限公司 | A kind of method of hydrogenation of high temperature coal tar |
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Effective date of registration: 20200421 Address after: 719319 Jinyuan South Road, Jinjie Industrial Park, Shenmu City, Yulin City, Shaanxi Province Patentee after: SHENMUFUYOU ENERGY TECHNOLOGY Co.,Ltd. Address before: 719319 Shenmu oil rich energy technology Co., Ltd., Shenmu Industrial Zone, Shenmu, Shaanxi, Yulin Patentee before: Wang Shukuan |