CN103146424B - The method of full cut preparing fuel oil by coal tar hydrogenation and lubricant base - Google Patents
The method of full cut preparing fuel oil by coal tar hydrogenation and lubricant base Download PDFInfo
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Abstract
The present invention relates to a kind of method of full cut preparing fuel oil by coal tar hydrogenation and lubricant base, it goes out lighter products and heavy product by after the process of full cut coal tar hydrogenating by flash separation after reducing valve step-down, the further isomerization dewaxing of heavy product, again with lighter products in succession through overheated, cold high score separator, cold low point of separator and separation column fractionation, thus it is good to obtain quality, be up to state standards the oil fuel and lubricant base that require, and technical process of the present invention is simple, easy to control, operating safety is stablized and full cut coal tar not only can be made to obtain scientific and reasonable utilization, further increase production economy benefit, and to the deficiency alleviating China's lubricant base, there is certain active effect.
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 the shortage of alleviation China's oil.
China has realized industrial coal tar hydrogenating technology at present and has mainly contained: benzoline (the < 370 DEG C) hydrogenation technique of coal tar, delay coking of coal tar hydrogenation combination technique, full cut coal tar hydrogenation process (Zhang Xiaojing. middle coalite tar hydrogen addition technology, coal journal, 2011, the 5th phase 840-844).But in actual production process, the coal tar hydrogenating tail oil of meeting by-product about 8%, normally by its export trade at a low price, does not have further Appropriate application, makes 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 being 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, find the full cut preparing fuel oil by coal tar hydrogenation of a kind of use and the method for coproduction lubricant base can also become the important topic of research.
Summary of the invention
For existing preparing fuel oil with coal oil hydrogenation technique existing for deficiency, the invention provides a kind of technical process simple, easy to control, good product quality, the method for the full cut preparing fuel oil by coal tar hydrogenation that safe operation is stable and lubricant base.
The present invention solves the problems of the technologies described above adopted technical scheme and is made up of following steps:
(1) according to a conventional method full cut coal tar is carried out de-slag aftertreatment of dewatering;
(2) send in the first hydrogenator after the full cut coal tar after the de-slag of dehydration mixes with hydrogen; the temperature in of hydrogenation protecting agent is 230 ~ 240 DEG C; the temperature of reaction of hydrodemetallation (HDM) agent is 240 ~ 260 DEG C, and pressure is 12 ~ 18MPa, and liquid air speed is 0.2 ~ 0.9h
-1, oily hydrogen volume, than 1:1500 ~ 2600, is sent in the second hydrogenator, and the temperature of reaction of hydrogen desulfurization agent is 310 ~ 350 DEG C, and the temperature of reaction of catalyst for hydro-upgrading is 380 ~ 420 DEG C, and pressure is 12 ~ 18MPa, and 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 by being separated lighter products with heavy product after reducing valve step-down in flashing tower, lighter products enters hot high score separator from the top exit of flashing tower by pipeline, heavy product to be entered in refining isomerization dewaxing reactor by pipeline by flashing tower outlet at bottom and reacts, temperature of reaction is 360 ~ 400 DEG C, pressure is 10 ~ 16.5MPa, and liquid air speed is 0.2 ~ 0.9h
-1, oily hydrogen volume is than being 1:1500 ~ 2600, and reaction product enters by pipeline the lighter products exported with flashing tower in hot high score separator and mixes, and in hot high score separator, isolate gas-phase product and liquid product;
(4) gas-phase product enters cold high score separator by pipeline, in cold high score separator, isolate hydrogen turns back in hydrogenator and isomerization dewaxing reactor by pipeline, the high score oil separated enters in cold low point of separator by pipeline, in cold low point of separator, isolate low point of oil be mixed in separation column in the duct with the isolated liquid product of hot high score separator and be separated, obtained 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); send in the first hydrogenator after full cut coal tar after the de-slag of dehydration mixes with hydrogen; optimum condition is: oily hydrogen volume compares 1:1500; the temperature in of hydrogenation protecting agent is 230 DEG C; the temperature of reaction of hydrodemetallation (HDM) agent is 250 DEG C; pressure is 14MPa, and liquid air speed is 0.2h
-1, send in the second hydrogenator, oily hydrogen volume is than 1:1500, and the temperature of reaction of hydrogen desulfurization agent is 320 DEG C, and the temperature of reaction of catalyst for hydro-upgrading is 390 DEG C, and pressure is 14MPa, and liquid air speed is 0.2h
-1, imurity-removal in hydrogenator, obtains hydrogenation products.
In above-mentioned steps (3), hydrogenation products by after reducing valve step-down in flashing tower lighter products be separated with heavy product, lighter products enters hot high score separator from the top exit of flashing tower by pipeline, heavy product to be entered in refining isomerization dewaxing reactor by pipeline by flashing tower outlet at bottom and reacts, optimum condition is: oily hydrogen volume is than being 1:1700, temperature of reaction is 370 DEG C, and pressure is 12MPa, and liquid air speed is 0.4h
-1, reaction product enters by pipeline the lighter products exported with flashing tower in hot high score separator and mixes, 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 goes out lighter products and heavy product by after the process of full cut coal tar hydrogenating by flash separation after reducing valve step-down, the further isomerization dewaxing of heavy product, again with lighter products in succession through overheated, cold high score separator, cold low point of separator and separation column fractionation, thus it is good to obtain quality, be up to state standards the oil fuel and lubricant base that require, and technical process of the present invention is simple, easy to control, operating safety is stablized and full cut coal tar not only can be made to obtain scientific and reasonable utilization, further increase production economy benefit, and to the deficiency alleviating China's lubricant base, there is certain active effect.
Accompanying drawing explanation
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 described, but the present invention is not limited only to following embodiment.
Embodiment 1
Now for full cut coalite tar 1, see Fig. 1, the method for Hydrogenation oil fuel and lubricant base is made up of following steps:
(1) according to a conventional method full cut coalite tar 1 is carried out de-slag aftertreatment of dewatering;
(2) coalite tar 1 after the de-slag of dehydration mixes in rear feeding first hydrogenator 3 with hydrogen 2; TK-10 hydrogenation protecting agent (Topsoe company), RN-5030 hydrodemetallation (HDM) agent (Criterion company) is loaded in first hydrogenator 3; the temperature in of TK-10 hydrogenation protecting agent is 230 DEG C; the temperature of reaction of RN-5030 hydrodemetallation (HDM) agent is 240 DEG C; pressure is 12MPa, and liquid air speed is 0.3h
-1oil hydrogen volume compares 1:1500, send into after having reacted in the second hydrogenator 4, dress ICR-137 hydrogen desulfurization agent (Chevron company), TK-555 catalyst for hydro-upgrading (Topsoe company) is added in second hydrogenator 4, the temperature of reaction of ICR-137 hydrogen desulfurization agent is 310 DEG C, the temperature of reaction of TK-555 catalyst for hydro-upgrading is 380 DEG C, and pressure is 12MPa, and liquid air speed is 0.3h
-1, oily hydrogen volume, than 1:1500, removes the impurity such as metal, sulphur, nitrogen, obtains hydrogenation products;
(3) hydrogenation products is by sending in flashing tower 6 after reducing valve 5 step-down, 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 from the outlet at flashing tower 6 top by pipeline, heavy product is entered in refining isomerization dewaxing reactor 7 in isomerization dewaxing catalyst ICR-142(Chevron company by pipeline by the outlet bottom flashing tower 6) katalysis under carry out isocracking reaction, temperature of reaction is 360 DEG C, pressure is 10MPa, and liquid air speed is 0.2h
-1, oily hydrogen volume is than being 1:1500, and reaction product enters by pipeline the lighter products exported with flashing tower 6 in hot high score separator 8 and mixes, and in hot high score separator 8, isolate gas-phase product and liquid product;
(4) gas-phase product enters cold high score separator 9 by pipeline, in cold high score separator 9, isolate hydrogen 2 turn back to first by pipeline, second hydrogenator 3, 4 and isomerization dewaxing reactor 7 in, carry out recycle, the high score oil separated at cold high score separator 9 enters in cold low point of separator 10 by pipeline, low point of gas 11 is isolated by recycling in pipeline feeding device for producing hydrogen in cold low point of separator 10, the isolated low point of oil of cold low point of separator 10 is mixed in the duct in separation column 10 with the isolated liquid product of hot high score separator 8 and is separated, obtained oil fuel and lubricant base 14.This oil fuel is gasoline fraction 12 and diesel oil distillate 13 mainly, and cold high score separator 9 enters device for producing hydrogen with the saline sewage 15 bottom cold low point of separator 10 by pipeline and recycles.
Embodiment 2
Now for full cut coalite tar 1, the method for Hydrogenation oil fuel and lubricant base is made up of following steps:
(1) according to a conventional method full cut coalite tar 1 is carried out de-slag aftertreatment of dewatering;
(2) coalite tar 1 after the de-slag of dehydration mixes in rear feeding first hydrogenator 3 with hydrogen 2; hydrogenation protecting agent, hydrodemetallation (HDM) agent is loaded in first hydrogenator 3; the temperature in of hydrogenation protecting agent is 230 DEG C; the temperature of reaction of hydrodemetallation (HDM) agent is 250 DEG C; pressure is 14MPa, and liquid air speed is 0.2h
-1oil hydrogen volume compares 1:1500, send into after having reacted in the second hydrogenator 4, dress hydrogen desulfurization agent, catalyst for hydro-upgrading is added in second hydrogenator 4, the temperature of reaction of hydrogen desulfurization agent is 320 DEG C, the temperature of reaction of catalyst for hydro-upgrading is 390 DEG C, and pressure is 14MPa, and liquid air speed is 0.2h
-1, oily hydrogen volume, than 1:1500, removes the impurity such as metal, sulphur, nitrogen, obtains hydrogenation products;
(3) hydrogenation products is by sending in flashing tower 6 after reducing valve 5 step-down, in flashing tower 6, the lighter products that water, ammonia and lighter hydrocarbons etc. form is separated with heavy product, lighter products enters hot high score separator 8 from the outlet at flashing tower 6 top by pipeline, heavy product to be entered in refining isomerization dewaxing reactor 7 by pipeline by the outlet bottom flashing tower 6 and carry out isocracking reaction under the katalysis of isomerization dewaxing catalyst, temperature of reaction is 370 DEG C, pressure is 12MPa, and liquid air speed is 0.4h
-1, oily hydrogen volume is than being 1:1700, and reaction product enters by pipeline the lighter products exported with flashing tower 6 in hot high score separator 8 and mixes, and in hot high score separator 8, isolate gas-phase product and liquid product;
Step (4) is identical with embodiment 1, obtained oil fuel and lubricant base.
Embodiment 3
Now for full cut coalite tar 1, the method for Hydrogenation oil fuel and lubricant base is made up of following steps:
(1) according to a conventional method full cut coalite tar 1 is carried out de-slag aftertreatment of dewatering;
(2) coalite tar 1 after the de-slag of dehydration mixes in rear feeding first hydrogenator 3 with hydrogen 2; hydrogenation protecting agent, hydrodemetallation (HDM) agent is loaded in first hydrogenator 3; the temperature in of hydrogenation protecting agent is 240 DEG C; the temperature of reaction of hydrodemetallation (HDM) agent is 260 DEG C; pressure is 16MPa, and liquid air speed is 0.5h
-1oil hydrogen volume compares 1:1800, send into after having reacted in the second hydrogenator 4, dress hydrogen desulfurization agent, catalyst for hydro-upgrading is added in second hydrogenator 4, the temperature of reaction of hydrogen desulfurization agent is 330 DEG C, the temperature of reaction of catalyst for hydro-upgrading is 400 DEG C, and pressure is 16MPa, and liquid air speed is 0.5h
-1, oily hydrogen volume, than 1:1800, removes the impurity such as metal, sulphur, nitrogen, obtains hydrogenation products;
(3) hydrogenation products is by sending in flashing tower 6 after reducing valve 5 step-down, in flashing tower 6, the lighter products that water, ammonia and lighter hydrocarbons etc. form is separated with heavy product, lighter products enters hot high score separator 8 from the outlet at flashing tower 6 top by pipeline, heavy product to be entered in refining isomerization dewaxing reactor 7 by pipeline by the outlet bottom flashing tower 6 and carry out isocracking reaction under the katalysis of isomerization dewaxing catalyst, temperature of reaction is 420 DEG C, pressure is 14MPa, and liquid air speed is 0.6h
-1, oily hydrogen volume is than being 1:2200, and reaction product enters by pipeline the lighter products exported with flashing tower 6 in hot high score separator 8 and mixes, and in hot high score separator 8, isolate gas-phase product and liquid product;
Step (4) is identical with embodiment 1, obtained oil fuel and lubricant base.
Embodiment 4
In the present embodiment; coalite tar 1 after the de-slag of step (2) dehydration mixes in rear feeding first hydrogenator 3 with hydrogen 2; hydrogenation protecting agent, hydrodemetallation (HDM) agent is loaded in first hydrogenator 3; the temperature in of hydrogenation protecting agent is 230 DEG C; the temperature of reaction of hydrodemetallation (HDM) agent is 250 DEG C; pressure is 18MPa, and liquid air speed is 0.9h
-1oil hydrogen volume compares 1:2600, send into after having reacted in the second hydrogenator 4, dress hydrogen desulfurization agent, catalyst for hydro-upgrading is added in second hydrogenator 4, the temperature of reaction of hydrogen desulfurization agent is 350 DEG C, the temperature of reaction of catalyst for hydro-upgrading is 420 DEG C, and pressure is 18MPa, and liquid air speed is 0.9h
-1, oily hydrogen volume, than 1:2600, removes the impurity such as metal, sulphur, nitrogen, obtains hydrogenation products;
(3) hydrogenation products is by sending in flashing tower 6 after reducing valve 5 step-down, in flashing tower 6, the lighter products that water, ammonia and lighter hydrocarbons etc. form is separated with heavy product, lighter products enters hot high score separator 8 from the outlet at flashing tower 6 top by pipeline, heavy product to be entered in refining isomerization dewaxing reactor 7 by pipeline by the outlet bottom flashing tower 6 and reacts under the katalysis of isomerization dewaxing catalyst, temperature of reaction is 400 DEG C, pressure is 16.5MPa, and liquid air speed is 0.9h
-1, oily hydrogen volume is than being 1:2600, and reaction product enters by pipeline the lighter products exported with flashing tower 6 in hot high score separator 8 and mixes, and in hot high score separator 8, isolate gas-phase product and liquid product;
Other step is identical with embodiment 1, obtained oil fuel and lubricant base.
Embodiment 5
In the present embodiment; coalite tar 1 after the de-slag of step (2) dehydration mixes in rear feeding first hydrogenator 3 with hydrogen 2; hydrogenation protecting agent, hydrodemetallation (HDM) agent is loaded in first hydrogenator 3; the temperature in of hydrogenation protecting agent is 230 DEG C; the temperature of reaction of hydrodemetallation (HDM) agent is 240 DEG C; pressure is 15MPa, and liquid air speed is 0.7h
-1oil hydrogen volume compares 1:2200, send into after having reacted in the second hydrogenator 4, dress hydrogen desulfurization agent, catalyst for hydro-upgrading is added in second hydrogenator 4, the temperature of reaction of hydrogen desulfurization agent is 330 DEG C, the temperature of reaction of catalyst for hydro-upgrading is 410 DEG C, and pressure is 15MPa, and liquid air speed is 0.7h
-1, oily hydrogen volume, than 1:2200, removes the impurity such as metal, sulphur, nitrogen, obtains hydrogenation products;
(3) hydrogenation products is by sending in flashing tower 6 after reducing valve 5 step-down, in flashing tower 6, the lighter products that water, ammonia and lighter hydrocarbons etc. form is separated with heavy product, lighter products enters hot high score separator 8 from the outlet at flashing tower 6 top by pipeline, heavy product to be entered in refining isomerization dewaxing reactor 7 by pipeline by the outlet bottom flashing tower 6 and carry out isocracking reaction under the katalysis of isomerization dewaxing catalyst, temperature of reaction is 395 DEG C, pressure is 14MPa, and liquid air speed is 0.6h
-1, oily hydrogen volume is than being 1:2000, and reaction product enters by pipeline the lighter products exported with flashing tower 6 in hot high score separator 8 and mixes, and in hot high score separator 8, isolate gas-phase product and liquid product;
Other step is identical with embodiment 1, obtained oil fuel and lubricant base.
Embodiment 6
In the present embodiment; coalite tar 1 after the de-slag of step (2) dehydration mixes in rear feeding first hydrogenator 3 with hydrogen 2; hydrogenation protecting agent, hydrodemetallation (HDM) agent is loaded in first hydrogenator 3; the temperature in of hydrogenation protecting agent is 230 DEG C; the temperature of reaction of hydrodemetallation (HDM) agent is 240 DEG C; pressure is 13MPa, and liquid air speed is 0.4h
-1oil hydrogen volume compares 1:1700, send into after having reacted in the second hydrogenator 4, dress hydrogen desulfurization agent, catalyst for hydro-upgrading is added in second hydrogenator 4, the temperature of reaction of hydrogen desulfurization agent is 310 DEG C, the temperature of reaction of catalyst for hydro-upgrading is 380 DEG C, and pressure is 13MPa, and liquid air speed is 0.4h
-1, oily hydrogen volume, than 1:1700, removes the impurity such as metal, sulphur, nitrogen, obtains hydrogenation products;
(3) hydrogenation products is by sending in flashing tower 6 after reducing valve 5 step-down, in flashing tower 6, the lighter products that water, ammonia and lighter hydrocarbons etc. form is separated with heavy product, lighter products enters hot high score separator 8 from the outlet at flashing tower 6 top by pipeline, heavy product to be entered in refining isomerization dewaxing reactor 7 by pipeline by the outlet bottom flashing tower 6 and carry out isocracking reaction under the katalysis of isomerization dewaxing catalyst, temperature of reaction is 360 DEG C, pressure is 11MPa, and liquid air speed is 0.2h
-1, oily hydrogen volume is than being 1:1500, and reaction product enters by pipeline the lighter products exported with flashing tower 6 in hot high score separator 8 and mixes, and in hot high score separator 8, isolate gas-phase product and liquid product;
Other step is identical with embodiment 1, obtained oil fuel and lubricant base.
Embodiment 7
In above-described embodiment 1 ~ 6, replaced by the coal-tar heavy oil of complete for raw material cut coalite tar 1 with the full cut coal-tar middle oil of equivalent or full cut, other step is identical with corresponding embodiment, obtained 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 relevant regulations to the specification of quality of corresponding motor spirit, derv fuel oil and lubricant base, contriver is according to detecting according to standard relevant regulations respectively the gasoline fraction obtained by 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
As can be seen from upper table 1, table 2, table 3, above-mentioned every detection of the gasoline fraction prepared by embodiment 1, diesel oil distillate and lubricant base all meets the regulation of relevant national standard.The oil fuel that embodiment 1 is obtained thus, the quality of lubricant base are good.
Claims (4)
1. a method for full cut preparing fuel oil by coal tar hydrogenation and lubricant base, is characterized in that being made up of following steps:
(1) according to a conventional method full cut coal tar is carried out de-slag aftertreatment of dewatering;
(2) send in the first hydrogenator after the full cut coal tar after the de-slag of dehydration mixes with hydrogen; oil hydrogen volume is than 1:1500 ~ 2600; the temperature in of TK-10 hydrogenation protecting agent is 230 ~ 240 DEG C; the temperature of reaction of RN-5030 hydrodemetallation (HDM) agent is 240 ~ 260 DEG C; pressure is 12 ~ 18MPa, and liquid volume air speed is 0.2 ~ 0.9h
-1, send in the second hydrogenator, oily hydrogen volume is than 1:1500 ~ 2600, the temperature of reaction of ICR-137 hydrogen desulfurization agent is 310 ~ 350 DEG C, the temperature of reaction of TK-555 catalyst for hydro-upgrading is 380 ~ 420 DEG C, and pressure is 12 ~ 18MPa, and liquid volume air speed is 0.2 ~ 0.9h
-1, imurity-removal in hydrogenator, obtains hydrogenation products;
(3) hydrogenation products by after reducing valve step-down in flashing tower lighter products be separated with heavy product, lighter products enters hot high score separator from the top exit of flashing tower by pipeline, heavy product to be entered in refining isomerization dewaxing reactor by pipeline by flashing tower outlet at bottom and reacts under the katalysis of ICR-142 isomerization dewaxing catalyst, temperature of reaction is 360 ~ 400 DEG C, pressure is 10 ~ 16.5MPa, and liquid volume air speed is 0.2 ~ 0.9h
-1, oily hydrogen volume is than being 1:1500 ~ 2600, and reaction product enters by pipeline the lighter products exported with flashing tower in hot high score separator and mixes, and in hot high score separator, isolate gas-phase product and liquid product;
(4) gas-phase product enters cold high score separator by pipeline, in cold high score separator, isolate hydrogen turns back in hydrogenator and isomerization dewaxing reactor by pipeline, the high score oil separated enters in cold low point of separator by pipeline, in cold low point of separator, isolate low point of oil be mixed in separation column in the duct with the isolated liquid product of hot high score separator and be separated, obtained 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, 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); send in the first hydrogenator after full cut coal tar after the de-slag of dehydration mixes with hydrogen; oil hydrogen volume compares 1:1500; the temperature in of hydrogenation protecting agent is 230 DEG C; the temperature of reaction of hydrodemetallation (HDM) agent is 250 DEG C, and pressure is 14MPa, and liquid volume air speed is 0.2h
-1, send in the second hydrogenator, oily hydrogen volume is than 1:1500, and the temperature of reaction of hydrogen desulfurization agent is 320 DEG C, and the temperature of reaction of catalyst for hydro-upgrading is 390 DEG C, and pressure is 14MPa, and liquid volume 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 after reducing valve step-down in flashing tower lighter products be separated with heavy product, lighter products enters hot high score separator from the top exit of flashing tower by pipeline, heavy product to be entered in refining isomerization dewaxing reactor by pipeline by flashing tower outlet at bottom and reacts, oil hydrogen volume is than being 1:1700, temperature of reaction is 370 DEG C, pressure is 12MPa, and liquid volume air speed is 0.4h
-1, reaction product enters by pipeline the lighter products exported with flashing tower in hot high score separator and mixes, and isolates gas-phase product and liquid product in hot high score separator.
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| 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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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
|---|---|---|---|---|
| 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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