CN101240192A - Method for producing high grade diesel oil by coal tar heavy fractioning hydrogenation - Google Patents
Method for producing high grade diesel oil by coal tar heavy fractioning hydrogenation Download PDFInfo
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- CN101240192A CN101240192A CNA2007100103826A CN200710010382A CN101240192A CN 101240192 A CN101240192 A CN 101240192A CN A2007100103826 A CNA2007100103826 A CN A2007100103826A CN 200710010382 A CN200710010382 A CN 200710010382A CN 101240192 A CN101240192 A CN 101240192A
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Abstract
The invention discloses a method for producing high quality diesel oil through hydrogenation of heavy coal tar distillate. The method is that technics of refining hydrogen-hydrocracking-upgrading portfolio is used, which includes: the heavy coal tar distillate and hydrogen mix and go into heydrogenation reaction zone, effluent after refining changes to diesel fuel cut fraction and tail oil through a segregation system, a part of the diesel fuel cut fraction and the tail oil go into the hydrocracking/upgrading reaction zone together, the part or the all of the effluent of the hydrocracking/the upgrading reaction circularly are acted as incoming stock of the refining hydrogen, and the left part goes into the segregation system. Compares to the prior art, the invention not only can produce production of high quality of low condensate diesel fuel through the hydrogenation of heavy coal tar distillates, and by-product of naphtha is acted as redintegration raw materials oil, but also provides a higher value-added application method for the heavy coal tar distillate, and relieves current situation of oil-based diesel supply and demand tension.
Description
Technical field
The present invention relates to a kind of method of producing high grade diesel oil by coal tar heavy fractioning hydrogenation, specifically, is raw material with the coal tar heavy fractioning, produces high-quality light Fuel oil product by the method for hydrofining-hydrocracking-hydro-upgrading.
Background technology
The scarcity day by day of world petroleum resource, the technology that makes various non-conventional oil resources processings produce light-weight fuel oils becomes focus, and one of technology wherein is to be producing clean fuel with the coal.
Coal tar heavy fractioning is one of cut of low temperature, middle temperature or coal-tar heavy oil distillation gained, its initial boiling point is at 180～260 ℃, final boiling point is at 400～600 ℃, the main mixture of forming by compounds such as anthracene, phenanthrene, carbazole, acenaphthenes, mostly be the above aromatic hydrocarbons of three rings and Fourth Ring greatly, density (20 ℃) is greater than 1.0g/m
3, and foreign matter content height, especially nitrogen content be about 1wt%, in addition higher, the oxygen level height is generally 1.0～2.0wt%, and coal tar heavy distillate is a kind of special material that is different from petroleum fractions.
At present the purposes of coal tar heavy fractioning is as carbon black raw material or is used for wood preserving oil, or separates and obtain products such as anthracene, acenaphthene, phenanthrene, carbazole, but the added value of aforesaid method is all lower.
With the method for hydrogenation handle coal tar or wherein the part cut produce the existing report of light-weight fuel oil.Introduced the method that a kind of coal tar hydrogenating is produced diesel oil as CN1351130A, this method is that the coal tar full distillate oil is distilled, to carry out hydrogenation less than 370 ℃ of cuts, its catalyst system therefor is Hydrobon catalyst and dearomatization catalyst, mainly is to make with extra care to remove impurity and aromatic hydrocarbons saturated reaction.This method is only applicable to handle lighter fraction in the coal tar, is not suitable for the processing coal tar heavy fractioning, the last running more than the diesel oil in the coal tar can not be converted into light-weight fuel oil.
It is the selective cracking catalyst of carrier with layer structure clay that US4640764 has introduced a kind of, thrcylic aromatic hydrocarbon (as anthracene), straight-chain paraffin, isomerization alkanes, naphthane and perhydronaphthalene are existed down, selective cracking is the higher component of cetane value, thereby improves the cetane value of diesel oil distillate.This patent catalyzer is not suitable for almost all, and component is the coal tar heavy fractioning of aromatic hydrocarbons.
CN1464031A discloses a kind of coal tar hydrotreating process and catalyzer, and this technology is to adopt hydrofining and hydro-upgrading one-stage serial, by coal tar production high-quality petroleum naphtha and fine-quality diesel oil.Though this technology is according to nitrogen in the coal tar, characteristics that iron level is high, selected titaniferous Hydrobon catalyst specially, the catalyst for hydro-upgrading that contains titanium oxide and molecular sieve, but the deactivation rate of catalyst for hydro-upgrading is fast in this technology, running period is short, more is not suitable for processing foreign matter content height, coal tar heavy fractioning that cut is heavier.And, can't satisfy in of the service requirements of north cold area condensation point less than-40 ℃ by the condensation point of diesel oil higher (4 ℃) that this technology is produced.
Summary of the invention
In order to overcome deficiency of the prior art, the invention provides a kind of method of coal tar heavy fractioning hydrogenation process for producing fine-quality diesel oil.This method not only can make coal tar heavy fractioning hydrogenation produce the high-grade low-freezing diesel product, the petroleum naphtha of by-product can be used as reforming raw oil simultaneously, and, alleviate the present situation of petroleum base diesel oil supply and demand anxiety simultaneously for coal tar heavy oil provides a kind of added value higher application approach.
The method of producing high grade diesel oil by coal tar heavy fractioning hydrogenation provided by the invention, comprise: coal tar heavy fractioning and hydrogen are mixed into the hydrofining reaction district, contact with Hydrobon catalyst, remove sulphur wherein, nitrogen, impurity such as oxygen, after separation system, obtain hydrogen-rich gas, petroleum naphtha, diesel oil, tail oil and water, wherein petroleum naphtha and a part of diesel oil can be used as the finished product and directly go out device, another part diesel oil and tail oil enter hydrocracking/upgrading reaction zone together, contact with catalyst for hydro-upgrading with hydrocracking catalyst successively and carry out hydrocracking and hydro-upgrading reaction, partly or entirely circulation is as hydrorefined charging for the hydrogenation reaction effluent of gained, and remainder enters above-mentioned separation system.The diesel oil distillate that wherein enters hydrocracking/upgrading reaction zone accounts for 20%～50% of total diesel oil distillate weight.
Among the present invention, the shared cover separation system of hydrofining effluent and hydrocracking/upgrading effluent can reduce facility investment like this.Hydrogen-rich gas by the separation system gained can be used as the recycle hydrogen use after purifying, water is discharged reactive system.
Tail oil of the present invention is as the criterion with diesel oil, counts lighting end than the component that diesel oil is lighter, and the cut that overweights diesel oil is counted tail oil.
Described hydrocracking reaction district can only adorn a kind of hydrocracking catalyst, also can be with two or more filling hydrocracking catalyst at different stages.
The hydro-upgrading reaction zone is in the downstream in hydrocracking reaction district, hydro-upgrading reaction zone and hydrocracking reaction district directly generate oil to hydrocracking and carry out the hydro-upgrading processing in same reactor, further improve the character of diesel product, especially improved diesel-fuel cetane number.
Used coal tar heavy fractioning is one of cut of coal tar distillation gained among the present invention, and its initial boiling point is at 180～260 ℃, and final boiling point is at 400～600 ℃.Mainly the mixture of being made up of compounds such as anthracene, phenanthrene, carbazole, acenaphthenes mostly is the above aromatic hydrocarbons of three rings and Fourth Ring greatly, and density (20 ℃) is greater than 1.0g/m
3, and foreign matter content height, especially nitrogen content be about 1wt%, in addition higher, and the oxygen level height is generally 1.0～2.0wt%.
The present invention has determined hydrogenation combination technique process of the present invention according to the character of coal tar heavy fractioning.Because oxygen level is higher in the coal tar heavy fractioning, so the separation system after refining can in time have been discharged and may dysgenic water have been arranged to hydro-upgrading and cracking catalyst, has reduced the possibility of the catalyst activity reduction that causes owing to the temporary absorption of water molecules and catalyst active center.Because aromaticity content height in the coal tar heavy fractioning, even after hydrofining and cracking step, generate in the oil and still have polycyclic aromatic hydrocarbonss such as higher dihydroanthracene of content and alkylnaphthalene, this is the major cause that causes the diesel oil distillate cetane value low, therefore present method is seated in modifying catalyst and cracking catalyst in the reactor, make hydrocracking generate polycyclic aromatic hydrocarbonss such as higher dihydroanthracene of content in the oil and alkylnaphthalene further through the upgrading catalyzed reaction, be converted into the ideal composition of diesel oil, help reducing plant investment and energy expenditure.Cracking/upgrading generates oil and partly or entirely circulates as hydrorefined charging, can alleviate on the one hand because the charging insulation that the existence of high melting compound such as anthracene, carbazole etc. causes requires height, easily stop up the problem of feeding line, available on the other hand back purified method, further make the further hydrogenation of polynuclear compound that reacts of not having enough time in the raw material saturated, promptly help lighting more, can make simultaneously the alkene that generates few part saturated is alkane, and this is favourable to the quality that improves light-end products.
The present invention is directed to oxygen and nitrogen content height in the coal tar heavy fractioning, aromaticity content height, characteristics that cut is heavier, select the hydrocracking catalyst that contains amorphous aluminum silicide and molecular sieve that anti-nitrogen and water resistance are good, cracking performance is suitable, not only anti-nitrogen of hydrocracking catalyst and anti-outlet capacity are strong, the running period of device is long, and can produce the qualified high-grade low-freezing diesel oil that uses at cold district of being suitable for, diesel cetane-number is greater than 45, and condensation point is less than-40 ℃.
In addition, the present invention also has following advantage:
1, the present invention advances hydrocracking/upgrading reaction zone with part of fraction of fuel-oil with tail oil, can solve the low problem of diesel oil distillate cetane value, make further saturated and open loop selective cracking of the higher double ring arene of content in the diesel oil distillate through aromatic hydrocarbons, generate the ideal composition of diesel oil---the mononuclear aromatics of band side chain, thereby improve the cetane value of diesel oil distillate, do not need again diesel oil distillate to be carried out aftertreatment and can satisfy the diesel oil specification, help making full use of hydroeracking unit, simplify Production Flow Chart, reduce production costs, improve the ton appreciation rate of raw material.
2, because the present invention has adopted lighter diesel oil distillate and tail oil to be mixed into the method for cracking case, can alleviate the problem (higher 40 ℃ of tail oil condensation point) of cracking case difficult feed on the one hand, improve the charging situation of cracking case simultaneously, helped the long-term operation of cracking unit.
3, this method is directly handled the last running of coal tar distillation gained, does not need raw material is carried out as pre-treatment such as cuttings, and the step that simplifies the operation reduces production costs.
4, the present invention provides a kind of processing means that improves its economy for the lower coal tar heavy fractioning of added value; Under the crude supply present situation of growing tension, for low-coagulation diesel oil production provides new raw material sources.
5, the present invention goes back by-product part reforming raw oil except obtaining qualified low-coagulation diesel oil product.
Description of drawings
Fig. 1 is a schematic flow sheet of the present invention.
Embodiment
Hydrobon catalyst in the inventive method is conventional hydrocracking pretreatment catalyst, be active ingredient generally with group vib and/or group VIII metal, with aluminum oxide or siliceous aluminum oxide is carrier, the group vib metal is generally Mo and/or W, and the group VIII metal is generally Co and/or Ni.In the weight of catalyzer, the group vib metal content is counted 10wt%～35wt% with oxide compound, and the group VIII metal content is counted 3wt%～15wt% with oxide compound, and its character is as follows: specific surface is 100～350m
2/ g, pore volume are 0.15～0.60ml/g.Main catalyzer have that China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute develops 3936,3996, Hydrobon catalysts such as FF-16, FF-26, the function class that also can be external catalyst Co. exploitation is like catalyzer, HC-K, HC-P catalyzer as Uop Inc., KF-847, the KF-848 etc. of the TK-555 of Topsor company, TK-565 catalyzer and AKZO company.The used reactor of hydrofining system is conventional hydrogenator.The operational condition of hydrofining system adopts conventional operational condition, is generally stagnation pressure 5.0MPa～19.0MPa, and average reaction temperature is 300 ℃～440 ℃, volume space velocity 0.1h during liquid
-1～4.0h
-1, hydrogen to oil volume ratio is 500: 1～5000: 1, and organic sulfur content is less than 500 μ g/g in the generation oil, and organonitrogen content is less than 300 μ g/g.
Hydrocracking process catalyst system therefor in the inventive method is conventional hydrocracking catalyst, is active ingredient with group vib and/or group VIII metal generally, and the group vib metal is generally Mo and/or W, and the group VIII metal is generally Co and/or Ni.The carrier of this catalyzer is one or more in aluminum oxide, siliceous aluminum oxide and the molecular sieve.Main catalyzer has FC-28, FC-14 that China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute develops, ZHC-01, ZHC-02, ZHC-04, single-stage hydrocracking catalyzer such as 3974, and DHC39, the DHC-8 of Uop Inc. of offshore company's exploitation, the hydrocracking catalysts such as ICR126 of CHERON company.The used reactor of hydrocracking system is conventional hydrogenator.Because oxygen level is than higher in the coal tar heavy fractioning, and the composition more complicated of oxygenatedchemicals in oil, therefore still containing the nitrogen and the oxygen of some amount in the tail oil that process hydrofining and fractionation obtain, is the hydrocracking catalyst of carrier so hydrocracking catalyst of the present invention is preferably with amorphous aluminum silicide and molecular sieve.Weight in catalyzer, the group vib metal content is counted 10wt%～35wt% with oxide compound, the group VIII metal content is counted 3wt%～15wt% with oxide compound, Y and/or beta-molecular sieve content are 5wt%-40wt%, amorphous aluminum silicide content is 10wt%～80wt%, alumina content is 10wt%～80wt%, and its specific surface is 100m
2/ g～650m
2/ g, pore volume are 0.15ml/g～0.50ml/g.Wherein 3974, FC-14 is for being the hydrocracking catalyst of cracking component with amorphous aluminum silicide and molecular sieve, is more suitable for process of the present invention.The operational condition of hydrocracking process can adopt conventional operational condition, and be generally: stagnation pressure 5.0MPa～18.0MPa, average reaction temperature is 300 ℃～440 ℃, volume space velocity 0.2h during liquid
-1～4.0h
-1, hydrogen to oil volume ratio is 500: 1～5000: 1.
In the inventive method, used catalyst for hydro-upgrading is for having optionally catalyzer of the saturated and higher open loop of good aromatic hydrocarbons, be active ingredient with group vib and/or group VIII metal generally, the group vib metal is generally Mo and/or W, and the group VIII metal is generally Co and/or Ni.The carrier of this catalyzer be in aluminum oxide, siliceous aluminum oxide and the molecular sieve one or more.Weight in catalyzer, the group vib metal content is counted 10wt%～35wt% with oxide compound, and the group VIII metal content is counted 3wt%～15wt% with oxide compound, and molecular sieve content is 5wt%-40wt%, alumina content is 10wt%～80wt%, and its specific surface is 100m
2/ g～650m
2/ g, pore volume are 0.15ml/g～0.50ml/g.Molecular sieve can be Y zeolite and/or beta molecular sieve etc.3963 and FC-18 as China Petroleum and Chemical Corporation Fushun Petrochemical Research Institute's development.Described hydro-upgrading condition is: pressure 3.0MPa～18.0MPa, average reaction temperature is 300 ℃～440 ℃, volume space velocity 0.3h during liquid
-1～4.0h
-1, hydrogen to oil volume ratio is 500: 1～5000: 1.
Figure 1 shows that a schematic flow sheet of the present invention, coal tar heavy fractioning 1 is mixed into the hydrofining reactor 3 that Hydrobon catalyst is housed with hydrogen 2, obtain hydrofining and generate oil 4, the generation oil 4 that obtains enters high-pressure separator 5 subsequently and carries out gas-liquid separation, the hydrogen-rich gas 9 that obtains, water 6 and liquid oil 7, hydrogen-rich gas 9 enters circulating hydrogen compressor, can be used as recycle hydrogen uses, water 6 direct extraction systems, liquid oil 7 enters separation column 8, fractionation obtains petroleum naphtha 10, diesel oil 11, and tail oil 12, the diesel oil 11 of 20wt%～50wt% and tail oil 12 are mixed into hydrocracking/reforming reactor 13 with hydrogen 2 and carry out hydrocracking and hydro-upgrading reaction, obtain hydrocracking/upgrading and generate oil 14, hydrocracking/upgrading generates oil 14 and partly or entirely returns hydro-refining unit, and remainder enters high-pressure separator 5.
Below by embodiment the present invention program and effect are described, it is described that Fig. 1 is pressed in concrete technical process.
The stock oil character that embodiment uses sees Table 1.(wherein wt% is weight percentage)
Table 1 stock oil character
| |
1# | 2# |
| Density, g/cm 3 | 1.10 | 1.16 |
| Boiling range/℃ | 190～420 | 250～600 |
| Carbon residue, wt% | 0.2 | 2.6 |
| Sulphur content, wt% | 0.48 | 0.53 |
| Nitrogen content, wt% | 0.96 | 1.12 |
| Metal content, μ gg -1 | 31.0 | 22.0 |
| Oxygen level, wt% | 1.1 | 1.9 |
| Aromaticity content, wt% | 100.0 | 100.0 |
At first coal tar heavy fractioning and hydrogen are mixed into hydrofining reactor, obtaining hydrofining generation oil separates, part diesel oil distillate and tail oil enter hydrocracking/reforming reactor, cracking/upgrading generates oil and all returns hydrofining reactor, obtain hydrofining generation oil and carry out fractionation, processing condition and product property see Table 2.
Table 2 processing condition and product property-hydrofining operational condition
| |
Embodiment 2 | |
|
|
|
| |
1# | 1# | 2# | 2# | 2# |
| Catalyzer | 3936 | 3936 | FF-26 | FF-26 | FF-26 |
| Pressure, MPa | 16.0 | 12.0 | 8.0 | 16.0 | 10.0 |
| Medial temperature, ℃ | 380 | 385 | 390 | 375 | 390 |
| Volume space velocity, h -1 | 0.4 | 0.8 | 0.5 | 0.2 | 0.6 |
| Hydrogen to oil volume ratio | 1500∶1 | 1000∶1 | 1500∶1 | 800∶1 | 2000∶1 |
Continuous table 2 processing condition and product property-hydrotreated product character
| |
Embodiment 2 | |
|
|
|
| Hydrofining mink cell focus nitrogen content, μ g/g | 240 | 300 | 280 | 250 | 260 |
| Diesel yield, wt% (accounting for total raw material) | 85.8 | 72.5 | 69.4 | 72.6 | 80.5 |
| The hydrofining diesel oil cetane value | 37.5 | 32.4 | 35.5 | 36.4 | 35.6 |
Continuous table 2 processing condition and product property-hydrocracking/upgrading operational condition
| |
Embodiment 2 | |
|
|
|
| Diesel feed accounts for the weight percent of total diesel oil distillate | 20％ | 50％ | 45％ | 35％ | 25％ |
| Hydrocracking/upgraded condition | |||||
| Catalyzer | FC-14/ 3963 | FC-14/ 3963 | ZHC-02/ FC-18 | ZHC-02/ FC-18 | 3974/ FC-14/ FC-18 |
| Pressure, MPa | 16.0 | 12.0 | 6.0 | 16.0 | 10.0 |
| Medial temperature, ℃ | 390/365 | 400/370 | 405/360 | 395/380 | 405/350 |
| Volume space velocity, h -1 | 0.80 | 0.60 | 0.60 | 0.35 | 0.20 |
| Hydrogen to oil volume ratio | 1500∶1 | 1000∶1 | 800∶1 | 1200∶1 | 1500∶1 |
Continuous table 2 processing condition and product property-hydrofining/cracking/upgrading product characteristics
| |
Embodiment 2 | |
|
|
|
| Hydrocracking generates oily nitrogen content, μ g/g | 2.1 | 3.0 | 4.0 | 2.0 | 2.2 |
| Diesel yield, wt% (accounting for total raw material) | 89.8 | 80.5 | 78.4 | 81.6 | 87.5 |
| The hydrogenated diesel oil cetane value | 45.5 | 46.4 | 47.5 | 46.4 | 48.6 |
Continuous table 2 processing condition and product property-whole flow process product yield and character
By embodiment as can be seen, by technology of the present invention, can be under hydro condition, adopt existing catalytic hydroprocessing technology and equipment, coal tar heavy fractioning is converted into the high-quality clean fuel to greatest extent, and especially low-coagulation diesel oil meets stricter specification requirement.
Can find out that from embodiment 1～5 quality of diesel oil obtains very fast lifting behind process hydrocracking/upgrading, especially the amplitude of cetane value raising is bigger, and foreign matter contents such as sulphur, nitrogen reduce significantly, can meet the requirement of harsh more automotive fuel specification.
Claims (10)
1. the method for a producing high grade diesel oil by coal tar heavy fractioning hydrogenation, comprise: coal tar heavy fractioning and hydrogen are mixed into the hydrofining reaction district, contact with Hydrobon catalyst and to carry out hydrofining reaction, the hydrofining reaction effluent of gained is after separation system, obtain hydrogen-rich gas, petroleum naphtha, diesel oil, tail oil and water, wherein petroleum naphtha and a part of diesel oil directly go out device as product, another part diesel oil enters hydrocracking/upgrading reaction zone with tail oil, contact with catalyst for hydro-upgrading with hydrocracking catalyst successively and carry out hydrocracking and hydro-upgrading reaction, partly or entirely circulation is as hydrorefined charging for the hydrocracking of gained/upgrading reaction effluent, and remainder enters above-mentioned separation system.
2. in accordance with the method for claim 1, it is characterized in that described coal tar heavy fractioning, its character is: 20 ℃ of density are 1.0～1.2g/m
3, more than the aromaticity content 90wt%, initial boiling point is 180～260 ℃, and doing is 400～600 ℃, and nitrogen content is 0.9～1.2wt%, and oxygen level is 1.0～2.0wt%.
3. in accordance with the method for claim 1, it is characterized in that a diesel oil distillate part with the separation system gained enters hydrocracking/reforming reactor with tail oil and carries out hydrotreatment, wherein to account for the ratio of total diesel oil distillate weight of separation system gained be 20%～50% to this part diesel oil distillate.
4. in accordance with the method for claim 1, it is characterized in that described hydrocracking catalyst is to contain amorphous aluminum silicide and molecular sieve is the hydrocracking catalyst of acid cracking component.
5. in accordance with the method for claim 1, it is characterized in that described hydrocracking reaction district loads a kind of hydrocracking catalyst, or adopt two or more filling hydrocracking catalyst at different stages.
6. in accordance with the method for claim 1, it is characterized in that described tail oil is as the criterion with diesel oil, the cut that overweights diesel oil is counted tail oil.
7. in accordance with the method for claim 1, the condition when it is characterized in that described raw material by the hydrofining bed is: stagnation pressure 5.0MPa～18.0MPa, average reaction temperature is 300 ℃～440 ℃, volume space velocity 0.1h during liquid
-1～4.0h
-1, hydrogen to oil volume ratio is 500: 1～5000: 1; Described hydrocracking condition is: stagnation pressure 5.0MPa～18.0MPa, average reaction temperature is 300 ℃～440 ℃, volume space velocity 0.2h during liquid
-1～4.0h
-1, hydrogen to oil volume ratio is 500: 1～5000: 1.
8. in accordance with the method for claim 1, it is characterized in that the hydro-upgrading reaction zone is positioned at the downstream in hydrocracking reaction district, described hydro-upgrading reaction zone and hydrocracking reaction district directly generate oil to hydrocracking and carry out the hydro-upgrading processing in same reactor.
9. according to claim 1 or 8 described methods, the catalyst for hydro-upgrading that it is characterized in that described hydro-upgrading process employing is for having optionally catalyst for hydro-upgrading of the saturated and higher open loop of good aromatic hydrocarbons.
10. according to claim 1 or 8 described methods, it is characterized in that described hydro-upgrading condition is, pressure 3.0MPa～18.0MPa, average reaction temperature is 300 ℃～440 ℃, volume space velocity 0.3h during liquid
-1～4.0h
-1, hydrogen to oil volume ratio is 500: 1～5000: 1.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101760237A (en) * | 2008-10-17 | 2010-06-30 | 何巨堂 | Hydrofining transform method of heavy fraction-containing coal tar |
| CN102021028A (en) * | 2010-12-09 | 2011-04-20 | 何巨堂 | Hydro-conversion method of two-stage method aromatic oil |
| CN101629103B (en) * | 2008-10-15 | 2013-07-17 | 何巨堂 | Hydro-conversion combination method for coal tar fraction with different boiling ranges |
| CN103756724A (en) * | 2014-01-26 | 2014-04-30 | 陈恒顺 | Production method of high-cetane-number anthracene oil and wash oil hydrogenated diesel oil |
| CN104498090A (en) * | 2014-12-17 | 2015-04-08 | 王树宽 | System and method for preparing naphthenic base oil and low freezing point diesel oil through all-hydrogen coal tar |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4640764A (en) * | 1986-02-24 | 1987-02-03 | Shell Oil Company | Selective tricyclic hydrogenation and cracking process and catalyst suitable for such hydroconversion |
| CN100412168C (en) * | 2002-06-07 | 2008-08-20 | 上海博申工程技术有限公司 | Coal tar hydrogenation process and catalyst therefor |
-
2007
- 2007-02-09 CN CN 200710010382 patent/CN101240192B/en active Active
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101629103B (en) * | 2008-10-15 | 2013-07-17 | 何巨堂 | Hydro-conversion combination method for coal tar fraction with different boiling ranges |
| CN101760237A (en) * | 2008-10-17 | 2010-06-30 | 何巨堂 | Hydrofining transform method of heavy fraction-containing coal tar |
| CN101760237B (en) * | 2008-10-17 | 2013-08-28 | 何巨堂 | Hydrofining transform method of heavy fraction-containing coal tar |
| CN102021028A (en) * | 2010-12-09 | 2011-04-20 | 何巨堂 | Hydro-conversion method of two-stage method aromatic oil |
| CN103756724A (en) * | 2014-01-26 | 2014-04-30 | 陈恒顺 | Production method of high-cetane-number anthracene oil and wash oil hydrogenated diesel oil |
| CN104498090A (en) * | 2014-12-17 | 2015-04-08 | 王树宽 | System and method for preparing naphthenic base oil and low freezing point diesel oil through all-hydrogen coal tar |
| CN104498090B (en) * | 2014-12-17 | 2017-03-08 | 王树宽 | Perhydro moulded coal tar naphthenic base oils and the system and method for low-coagulation diesel oil |
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| CN101240192B (en) | 2011-08-24 |
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