CN106701176B - A kind of process for handling high temperature coal-tar - Google Patents
A kind of process for handling high temperature coal-tar Download PDFInfo
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- CN106701176B CN106701176B CN201510769230.9A CN201510769230A CN106701176B CN 106701176 B CN106701176 B CN 106701176B CN 201510769230 A CN201510769230 A CN 201510769230A CN 106701176 B CN106701176 B CN 106701176B
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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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/205—Metal content
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Abstract
The present invention provides a kind of process for handling high temperature coal-tar, methods described is that high temperature coal-tar is fractionated to obtain light fraction and heavy distillat, heavy distillat, the line distillate that subtracts three of naphthene base crude enter preatreating reactors after being mixed with demulsifier, stirring standing separation obtains liquid phase and insoluble matter, enter demetalization reactor after liquid phase, solvent naphtha, alcohols material mixing, with filler haptoreaction, reaction effluent enters water scrubber, the mixture for contacting to obtain with fresh water enters dehydrating tower, the isolated high temperature coal-tar and water removed after metal.The inventive method can purify coal tar raw material in the metal during high temperature coal-tar is removed under relaxing process conditions, slow down metal inactivation and the rising of bed pressure drop of catalyst in hydrogenation reactor.
Description
Technical field
The invention belongs to field of coal tar deep processing, and in particular to the processing method of high temperature coal-tar.
Background technology
Coal tar is the fluid product that coal obtains during destructive distillation and gasification.Can according to the difference of pyrolysis temperature and method
Obtain following several tar：Low temperature (450 DEG C~650 DEG C) retort tar；(600 DEG C~800 DEG C) generation oven cokes of low temperature and medium temperature
Oil；Medium temperature (900 DEG C~1000 DEG C) vertical coke oven tar；High temperature (1000 DEG C) coking tar.No matter which kind of tar is to have thorn
Swash the black of property stink or the thick liquid of dark brown.Density at 20 DEG C is between 0.98~1.2g/cm3, and its value is with temperature
Rise and reduce.Coal tar is the organic mixture based on aromatic hydrocarbon, containing 10,000 multiple compounds, extractible about 500
Kind.At present, there is value and extractable and economical rationality about 50 kinds, light oil that its deep processing is obtained, phenol, naphthalene, wash
The series of products such as oil, anthracene, carbazole, indoles, pitch be synthetic plastic, synthetic fibers, agricultural chemicals, dyestuff, medicine, coating, auxiliary agent and
The basic material of fine chemical product, and the base stock of the industry such as metallurgy, synthesis, construction, weaving, papermaking, traffic, it is many
Product is unavailable in petrochemical industry, and therefore, coal tar processing can promote the development of these industries.And improve the utilization of resources
Rate, be advantageous to environmental protection and develop a circular economy.
Because processing temperature is different, the composition and property of corresponding coal tar have very big difference, especially high temperature coal-tar
Matter is the most inferior, and middle coalite tar and high temperature coal-tar are two kinds of completely different tar, and composition does not have to, and water content is different,
Also difference is very big for tenor, and high temperature coal-tar is a kind of material of dark oil, there is special odor, with middle coalite tar phase
Than high temperature coal-tar density is big, carbon residue is high, condensed-nuclei aromatics content is high, especially high with the heavy constituent such as colloid, asphalitine content, gold
It is high to belong to content.Containing 10%~30% moisture content in high temperature coal-tar, and the state of Water-In-Oil is presented.In at coalite tar
Reason method is not appropriate for handling high temperature coal-tar, it is necessary to finds new process route and process conditions.
As economic development and light-weight fuel oil demand constantly increase, coal tar hydrogenating is produced into light-weight fuel oil increasingly
The favor of tar producer is obtained, middle coalite tar hydrogenation production light Fuel oil tech is relatively ripe, in the industry cycle promotes
It is more.But middle coalite tar and high temperature coal-tar are two kinds of completely different tar, and nature difference is very big, high temperature coal-tar mesh
The industrialized device of front-end hydrogenation is relatively fewer, it is reported that industrialized device has Qitaihe treasured ACE Semi coal chemical industry limited at present
100,000 tons of industrialized units of company, it uses high temperature coal-tar back-end crop technology, by the colloid in coal tar, asphalitine and machinery
Impurity removal, light component is subjected to hydrotreating, in addition, not yet document report has industrialized plant running.Cause height
Warm coal tar fails extensive industrialized reason and its property composition much relations, and wherein one of reason is high temperature coal-tar restructuring
Divide content high, especially the condensed-nuclei aromatics such as colloid, asphalitine content is high, and the tenor such as wherein corresponding Fe, Ca, Na is special
Height, in using traditional fixed bed hydrogenation processing procedure, these metals can be deposited on catalyst surface or bed after being removed
In layer space, catalyst inactivation or bed pressure drop is caused to raise, especially Hydrodemetalation catalyst superficial metal deposition amount is big,
Catalyst inactivation speed and pressure drop rise speed especially cause device shortening service cycle soon.
Patent CN1676583A describes a kind of high temperature coal tar hydrocracking technique, and wherein high temperature coal tar introduces
Heating furnace is mixed with hydrogen, and hydrofining reactor, then the hydrogen isolated through exchanging heat into high-pressure separator are entered after mixing
Hydrofining reactor is returned to through circulating hydrogen compressor, generation oil enters low pressure separator, entered after low point of fuel oil of sub-department
Deoxidation tower, enter fractionating column after further taking off fuel gas, gasoline, diesel oil and lubricating oil are obtained after fractionation, tail oil enters to be hydrocracked
Reactor.A large amount of metals of content etc. are easily caused what catalyst inactivation and bed pressure drop rose in high temperature coal tar in this patent
Component, directly handled in the case where not anticipated to raw material using traditional hydrofining reactor, can cause to urge
Agent deactivation rate is accelerated and bed pressure drop rises, and then causes device shortening service cycle.
At present, there are a variety of drawbacks in domestic existing coal tar processing, and many enterprises are directly using coal tar as combustion
Material is sold, and so does that poor product quality, added value are low, and the pollution to environment is also extremely serious.With market competition not
Disconnected intensification and national specification increasingly strict in terms of environmental protection and requirement, adequately and reasonably become people using tar resource
The hot issue increasingly paid close attention to.Hydrogenation of tar technology can haul out the thing of the post-combustion pollution environment such as sulphur in coal tar, nitrogen
Matter, improve smell, color and the stability of oil product, improve oil quality, be a kind of important means of coal tar comprehensive utilization.Coal
Tar has to pass through and handled before hydrogenation plant is entered, and removes the components such as water therein, impurity, asphalitine, metal, ability
It is normally carried out hydrogenation process.Therefore, to the research of coal tar preprocessing process, improving energy utilization rate, reduce energy consumption and
It is significant to increase enterprise profit aspect.
The content of the invention
It is big for current high temperature coal-tar studies on asphaltene, tenor, carry out hydrogenation reactor Nei Tuojin during hydrogenation reaction
The shortcomings that metal catalyst metal deposition capability is big, deactivation rate is fast, the present invention provide a kind of process for handling high temperature coal-tar,
The existence form and actual tests result of metal in the coal tar that Binding experiment research is found, are removed high in the case where relaxing process conditions
Metal in warm coal tar, coal tar raw material is purified, slow down the metal inactivation and bed pressure drop of catalyst in hydrogenation reactor
Rise, a kind of feasible processing method is provided for high temperature coal-tar.
Found by studying, the existence form of metal and the existence form of metal in traditional residual oil have very in high temperature coal-tar
Big difference, metal is mainly the metals such as Ni, V in residual oil, and is existed more in the form of porphyrin metal complex, due to these metals
Be embedded in heavy constituent colloid and the asphalitine in residual oil, it is necessary in the presence of catalyst and hydrogen high temperature removal；And high temperature
Metal in coal tar mainly exists with metal oxide forms such as Fe, Ca, Na, and Ni, V tenor are seldom, this and its shape
Relevant into process, coal steam needs Water spray to cool down during High T-emperature Carbonization, and the salt such as Ca, Mg in water can enter in coal tar, together
When the dry distillation of coal during have substantial amounts of coal ash, furnace wall breakage thing and some mineral matters（Calcite, albite）Deng doping wherein,
These materials can carry substantial amounts of alkaline metal oxide（CaO, Na2O、MgO、Fe2O3）Into in high temperature coal-tar, at the same it is high
In warm coal tar storage and transportation, enter coal tar because the reasons such as corrosive pipeline also result in the part metals such as Fe ion
Oil, as the above analysis, the metal in high temperature coal-tar have be greatly with existing for mineral form, so if
It is clearly contretemps to be applied to again using traditional demetallated mode of residual oil on coal tar metal removal.But due to high temperature
Coal tar contains 10%~30% moisture, and the state that Water-In-Oil is presented more, a certain degree of emulsification be present, is sent out during experiment
Now it is difficult to be demulsified to coal tar and remove metal therein using traditional in general demulsifier.
Based on above-mentioned discovery, the present invention provides a kind of process for handling high temperature coal-tar, and methods described includes as follows
Content：
（1）High temperature coal-tar is segmented to obtain light fraction and heavy distillat, and the cut-point is 330~400 DEG C, is preferably
360~380 DEG C；
（2）Step（1）The line distillate that subtracts three of obtained heavy distillat and naphthene base crude enters pretreatment reaction after mixing
Device, stood after being sufficiently stirred, isolated liquid phase and insoluble matter；
（3）Step（2）Enter after obtained liquid phase, solvent naphtha, alcohols material mixing and preheated to 150~250 DEG C de-
Metallic reactors, contact and reacted with the filler loaded in demetalization reactor；
（4）Step（3）Obtained reaction effluent enters water scrubber, fully contacts with fresh water, is solved in reaction effluent
The metal inorganic substance come is separated out to be dissolved into aqueous phase；
（5）Step（4）Obtained mixture enters dehydrating tower, carries out water-oil separating, obtains removing the high-temperature coal after metal
Tar and water；
（6）Step（1）Obtained insoluble matter mixes with aromatic solvent, isolated aromatic hydrocarbons DDGS and aromatic hydrocarbons insoluble matter；
（7）By step（6）Aromatic hydrocarbons in obtained aromatic hydrocarbons DDGS is distilled off, and obtains steaming excess；
（8）By step（1）Obtained light fraction, step（5）Obtained high temperature coal-tar and step（7）Obtained steaming excess
It is well mixed to obtain pretreated high temperature coal-tar.
In the inventive method, the high temperature coal-tar is that heating final temperature obtains more than 900 DEG C through destructive distillation or coking
High temperature coal-tar.
In the inventive method, the line distillate that subtracts three of the naphthene base crude and the weight ratio of high temperature coal-tar are 1：50~
1:10。
In the inventive method, step（2）In can also add demulsifier.
In the inventive method, step（2）In can also add auxiliary agent, the auxiliary agent is 1- butyl -3- methylimidazole tetrafluoros
Borate and/or 1- butyl -3- methylimidazole hexafluoro borates, the dosage are the 1/50000~1/ of high temperature coal-tar weight
15000。
In the inventive method, the boiling range of the solvent naphtha is 65~450 DEG C, preferably 120~400 DEG C, more preferably 150
~320 DEG C, can be specifically hydrofining diesel oil, hydrofinishing naphtha, hydrofinishing washing oil, hydrofinishing light oil, hydrogenation
One or several kinds of mixtures in refined carbolic oil.
In the inventive method, step（3）Described in the weight of solvent naphtha and high temperature coal-tar ratio be 1:20~1:3, preferably
For 1:10~1:5.
In the inventive method, the alcohols material can be the one or more in methanol, ethanol, isopropanol, sec-butyl alcohol.
The addition of the alcohols material is the 1/10000~1/100 of high temperature coal-tar weight；It is preferred that 1/5000~1/500.
In the inventive method, in the demetalization reactor filler of filling can be ceramic ring, quartz sand, activated carbon,
One or several kinds in diatomite, silica, aluminum oxide, zeolite, preferably ceramic ring, diatomite, activated carbon and titanium dioxide
Silicon；The aperture of the filler is 200nm~50 μm, preferably 300nm~10 μm.
In the inventive method, 2~5 layers of filling of filler point in the demetalization reactor, preferably divide 3~4 layers of filling,
And along the aperture of Flow of Goods and Materials direction filler from large to small, while bed voidage is also from large to small, adjacent two layers filling
The pore size difference of thing is 50nm~1000nm, to those skilled in the art, when dividing multilayer filling filler, multilayer
The ratio of filler is that those skilled in the art can determine by existing knowledge.
In the inventive method, the demetalization reactor can be two and be arranged in parallel, when wherein a reactor reaches
During processing limit, switch another demetalization reactor.
In the inventive method, the filler of filling is different from traditional Hydrodemetalation catalyst in demetalization reactor, this
Filler has very strong appearance dirt and interception capacity in text, but does not have catalytic activity substantially；Therefore tradition can be avoided de-
Metallic catalyst is when high-temperature hydrogenation caused by aromatic hydrocarbons polycondensation the problems such as catalyst coking.
Compared with prior art, the inventive method has the following advantages that：
1st, in the inventive method, high temperature coal-tar is fractionated to obtain light fraction and heavy distillat, impurity, metal, pitch first
Matter etc. is concentrated mainly in heavy distillat, can so reduce treating capacity, viable economically, by obtained heavy distillat and cycloalkanes base
Precipitation is had after the line distillate that subtracts three of oil is well mixed, impurity, part in the mainly coal tar through analysis precipitation
Resin and asphalt, meanwhile, a part of metal is also deposited and is carried out.
2nd, in the inventive method, it is found that the metal in high temperature coal-tar exists with inorganic salt form, using the inventive method
Metal impurities therein can be removed under the relative operating condition relaxed, avoid conventional method using hydrogenation high temperature removal into
The problem of this is high.
3rd, the inventive method operates the metal in removing coal tar at a lower temperature, can avoid alkadienes in coal tar
The problem of easy polycondensation causes catalyst inactivation at high temperature Deng unsaturated hydrocarbons.
4th, in the inventive method, the demetalization reactor inner stuffing is without carried metal, and aperture is big, retention and appearance dirt
Ability is strong, and cost is less than the catalyst for demetalation of the carried metal in conventional method, at the same can effectively catching remove
Metallic salt.
5th, in the inventive method, by using solvent naphtha as dilution precipitating reagent, body can be destroyed by adding solvent naphtha
The colloidal stability of system, the viscous force between original component is on the one hand reduced, on the other hand by the asphalitine in glue core center
Parsed etc. heavy constituent, the components precipitate such as toluene insolubles and mechanical admixture for most being suspended at last in system gets off, while companion
As most precipitated metals get off.
6th, in the inventive method, auxiliary agent alcohols material is added, it is and oxygen-containing in coal tar because alcohols material contains hydroxyl
Compound aldehydes matter property is similar, can reach and dissolve each other, and the metal inorganic salt hydrophily dissociateed in such coal tar is strong,
It can be dissolved into alcohols, in follow-up water scrubber, alcohols material carries salt and can mixed with the water of excess, forms new mixing
Thing, and new mixture and coal tar intersolubility are poor, and then realize the separation of coal tar and alcohol-water mixture.
Embodiment
Technical scheme is further illustrated below by specific embodiment, but is not limited to the embodiment.
High temperature coal-tar raw material, naphthene base crude subtract three line distillate, solvent oil nature used by the embodiment of the present invention
Table 1 is listed in respectively, and demetalization processor process conditions are shown in Table 2.Direction is loaded respectively from top to bottom in the demetalization processor
Four kinds of ceramic ring, diatomite, activated carbon and silica fillers, the apertures of four kinds of fillers is respectively 5~10 μm, 1~3
μm, 500nm~900nm, 300~500nm, the admission space ratios of four kinds of fillers is 30:25:25:20, solvent naphtha is
The naphtha and diesel fuel mixtures that hydrotreating obtains, the demulsifier are the SLD-G031 model demulsifiers of triumph chemical industry.
The feedstock property of table 1
Embodiment 1
Test raw material is high temperature coal-tar and the line distillate that subtracts three described in table 1, and the alcohols material be ethanol, reaction bar
Part is shown in Table 2, and reaction result is referring to table 3.
Embodiment 2
Test raw material is high temperature coal-tar and the line distillate that subtracts three described in table 1, and the alcohols material be ethanol, is added simultaneously
Enter 1- butyl -3- methyl imidazolium tetrafluoroborates, the weight ratio of ethanol consumption and high temperature coal-tar is 1:25000, reaction condition
2 are shown in Table, reaction result is referring to table 3.
Embodiment 3
Test raw material is high temperature coal-tar and the line distillate that subtracts three described in table 1, and the alcohols material be methanol, is added simultaneously
Enter auxiliary agent 1- butyl -3- methylimidazole hexafluoro borates and demulsifier, the weight ratio of auxiliary dosage and high temperature coal-tar is 1:
25000, the dosage of the demulsifier is the 1/20000 of coal tar weight, and reaction condition is shown in Table 2, and reaction result is referring to table 3.
Comparative example 1
Same as Example 1, difference is that line distillate does not mix high temperature coal-tar with subtracting three, and reaction condition is shown in Table
2, reaction result is referring to table 3.
Comparative example 2
Same as Example 2, difference is to be added without alcohols material, and reaction condition is shown in Table 2, and reaction result is referring to table
3。
The reaction condition of table 2 and result
Claims (16)
1. a kind of process for handling high temperature coal-tar, methods described include following content：
（1）High temperature coal-tar is segmented to obtain light fraction and heavy distillat, and the cut-point is 330~400 DEG C；
（2）Step（1）The line distillate that subtracts three of obtained heavy distillat and naphthene base crude enters preatreating reactors after mixing, and fills
Stood after dividing stirring, isolated liquid phase and insoluble matter；
（3）Step（2）Enter demetalization after obtained liquid phase, solvent naphtha, alcohols material mixing and preheated to 150~250 DEG C
Reactor, contact and reacted with the filler loaded in demetalization reactor；
（4）Step（3）Obtained reaction effluent enters water scrubber, fully contacts with fresh water, is dissociateed in reaction effluent
The metal inorganic substance come is dissolved into aqueous phase；
（5）Step（4）Obtained mixture enters dehydrating tower, carries out water-oil separating, obtains removing the high temperature coal-tar after metal
And water；
（6）Step（2）Obtained insoluble matter mixes with aromatic solvent, isolated aromatic hydrocarbons DDGS and aromatic hydrocarbons insoluble matter；
（7）By step（6）Aromatic hydrocarbons in obtained aromatic hydrocarbons DDGS is distilled off, and obtains steaming excess；
（8）By step（1）Obtained light fraction, step（5）Obtained high temperature coal-tar and step（7）Obtained steaming excess mixing
Uniformly obtain pretreated high temperature coal-tar.
2. in accordance with the method for claim 1, it is characterised in that：The cut-point of the high temperature coal-tar is 360~380 DEG C.
3. in accordance with the method for claim 1, it is characterised in that：Step（2）Described in naphthene base crude the line cut that subtracts three
The mass ratio of oil and high temperature coal-tar is 1:50~1:10.
4. in accordance with the method for claim 1, it is characterised in that：Step（3）Described in alcohols material be methanol, it is ethanol, different
One or more in propyl alcohol, sec-butyl alcohol.
5. in accordance with the method for claim 1, it is characterised in that：The addition of the alcohols material is high temperature coal-tar weight
1/10000~1/100.
6. in accordance with the method for claim 1, it is characterised in that：The addition of the alcohols material is high temperature coal-tar weight
1/5000~1/500.
7. in accordance with the method for claim 1, it is characterised in that：Step（2）Middle addition auxiliary agent, the auxiliary agent be 1- butyl-
3- methyl imidazolium tetrafluoroborates and/or 1- butyl -3- methylimidazole hexafluoro borates.
8. in accordance with the method for claim 1, it is characterised in that：Step（2）Middle addition demulsifier.
9. in accordance with the method for claim 1, it is characterised in that：The boiling range of the solvent naphtha is 65~450 DEG C.
10. in accordance with the method for claim 1, it is characterised in that：The solvent naphtha is hydrofining diesel oil, hydrofinishing stone
One or several kinds in cerebrol, hydrofinishing washing oil, hydrofinishing carbolic oil.
11. in accordance with the method for claim 1, it is characterised in that：Step（3）Described in the weight of solvent naphtha and high temperature coal-tar
Amount is than being 1:20~1:3.
12. in accordance with the method for claim 1, it is characterised in that：The filler of filling is porcelain in the demetalization reactor
One or several kinds in ring, quartz sand, activated carbon, diatomite, silica, aluminum oxide, zeolite.
13. in accordance with the method for claim 1, it is characterised in that：The filler of filling is porcelain in the demetalization reactor
Ring, diatomite, activated carbon and silica.
14. in accordance with the method for claim 1, it is characterised in that：The aperture of the filler is 200nm~50 μm.
15. in accordance with the method for claim 1, it is characterised in that：2~5 layers of filler point in the demetalization reactor
Filling, and along the aperture of Flow of Goods and Materials direction filler from large to small, while bed voidage is also from large to small.
16. in accordance with the method for claim 15, it is characterised in that：The pore size difference of adjacent two layers filler is 50nm
~1000nm.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04224892A (en) * | 1990-12-26 | 1992-08-14 | Idemitsu Kosan Co Ltd | Method for refining crude oil |
| CN1766058A (en) * | 2004-10-29 | 2006-05-03 | 中国石油化工股份有限公司 | Coal tar whole fraction hydrotreatment process |
| CN101629107A (en) * | 2008-09-22 | 2010-01-20 | 何巨堂 | Method for hydro-upgrading coal tar containing heavy distillate |
| CN103205272A (en) * | 2012-01-12 | 2013-07-17 | 易高环保能源研究院有限公司 | Method for production of purified coal tar pitch from high temperature coal tar |
| EP2818535A1 (en) * | 2012-01-12 | 2014-12-31 | Eco Environmental Energy Research Institute Limite | Process for producing mesophase pitch by hydrogenation of high-temperature coal tar |
-
2015
- 2015-11-12 CN CN201510769230.9A patent/CN106701176B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04224892A (en) * | 1990-12-26 | 1992-08-14 | Idemitsu Kosan Co Ltd | Method for refining crude oil |
| CN1766058A (en) * | 2004-10-29 | 2006-05-03 | 中国石油化工股份有限公司 | Coal tar whole fraction hydrotreatment process |
| CN101629107A (en) * | 2008-09-22 | 2010-01-20 | 何巨堂 | Method for hydro-upgrading coal tar containing heavy distillate |
| CN103205272A (en) * | 2012-01-12 | 2013-07-17 | 易高环保能源研究院有限公司 | Method for production of purified coal tar pitch from high temperature coal tar |
| EP2818535A1 (en) * | 2012-01-12 | 2014-12-31 | Eco Environmental Energy Research Institute Limite | Process for producing mesophase pitch by hydrogenation of high-temperature coal tar |
Non-Patent Citations (1)
| Title |
|---|
| 煤焦油加氢制燃料油的试验研究;田小藏;《工业安全与环保》;20070731;第33卷(第7期);第56-57页 * |
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