CN102899088A - Hydrogenation method for medium and low temperature coal tar - Google Patents
Hydrogenation method for medium and low temperature coal tar Download PDFInfo
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Abstract
The invention discloses a hydrogenation method for medium and low temperature coal tar. The medium and low temperature coal tar is pretreated and fractionated to obtain carbolic oil, light distillates and asphalt; the carbolic is subjected to dephenolization to obtain phenol products and dephenolized oil; the light distillates and the dephenolized oil are mixed and sent into a hydrotreating reaction zone; liquid generated from hydrotreatment is sent into a hydrocracking reaction zone; the liquid generated from hydrotreatment is fractionated to obtain intermediate distillate oil used as diesel; the tail oil obtained from fractionation is recycled to the hydrocracking reaction zone or the hydrotreating reaction zone; naphtha obtained from fractionation is sent into a catalytic reforming reaction zone; hydrogen obtained from catalytic reforming is used in a hydrogen system; and the obtained liquid is extracted and fractionated to obtain premium gasoline or light aromatic products. Compared with the prior art, the method provided by the invention employs a combined process comprising fractionation, dephenolization, hydrotreating, hydrocracking and catalytic reforming to obtain phenol products, light aromatic products and high-quality motor fuel, and greatly prolongs operation cycle of the device.
Description
Technical field
What the present invention relates to is a kind of Coal Chemical Industry complete processing, specifically the method for hydrotreating of a kind of light aromatic hydrocarbons of middle coalite tar production and automotive fuel.
Background technology
Oil is one of important sources of automotive fuel and industrial chemicals.At present, petroleum consumption sustainable growth in the world wide, and the rate of growth of workable reserve is considerably slower than the speed of consumption is processed extra heavy oil in addition and oil sands bitumen also becomes development trend, and therefore seeking other substitute energys becomes a kind of developing direction.Coal and oil are all fossil energy, mainly consist of carbon and hydrogen, and relatively abundanter 2/3rds of the world's fossil energy residual recoverable reserves that accounts for of coal resources, therefore produce automotive fuel by coal or industrial chemicals has larger development prospect.
The thick liquid with pungent odour that coal tar generates when being coal destructive distillation or gasification.In, coalite tar comes from the product of destructive distillation under the lesser temps or gasification, form very complicated, topmost elementary composition be carbon, hydrogen, sulphur, nitrogen, oxygen etc.Its chemical constitution mainly is aromatics, alkene and alkane, and all the other are oxygenatedchemicals, nitrogenous compound and sulfocompound.Oxygenatedchemicals mainly is to have weakly acidic various phenols, and nitrogenous compound mainly is to have weakly alkaline pyridine, quinoline and their derivative, and sulfocompound mainly is thiophene, mercaptan, thiophenol, thioether etc.Take middle coalite tar as stock oil, adopt more suitable working method and suites of measure can produce the Chemicals suitable with oil and cleaning automotive fuel, not only have significant economic benefit, also have obvious social benefit simultaneously.
The deep processing method of middle coalite tar is along with the increasingly stringent of the growing tension of petroleum resources and environmental regulation and come into one's own.Main working method has at present:
Chinese patent CN200910048881.3 discloses a kind of middle coalite tar deep processing method, mainly be that coal tar is at first obtained phenol products by fractionation and dephenolize, then dephenolize oil carries out coking with last running, the full cut of coking carries out hydrofining and hydrocracking, and then naphtha reforming-Aromatics Extractive Project is produced benzene, toluene and dimethylbenzene and solvent oil.The dephenolize oil of the method and heavy distillate have produced coke product through after the coking, and liquid product yield is had very large impact.
Chinese patent CN200910166828.3 discloses a kind of deep processing method of middle coalite tar, coal tar is separated obtaining diesel oil distillate and lighter cut, then produces light aromatic hydrocarbons by the method for hydrofining and catalytic reforming combination.The method has only been carried out the hydrofining processing to light ends, the cut of decompressed wax oil is not carried out hydrotreatment, and not only liquid product yield is very low, and aromatic production is also lower.
Chinese patent CN200910077529.2 discloses the method that a kind of middle coalite tar is produced high-cleanness fuel oil, mainly is that the method by solvent extraction is divided into light-weight fuel oil and heavy fuel oil (HFO) with coal tar.The method is only processed by the method centering coalite tar of physics, and quality product is relatively poor, and does not produce aromatic hydrocarbon product
In the above-mentioned working method, basically all be that the diesel oil distillate that obtains of centering coalite tar and the cut lighter than diesel oil distillate have used hydrorefined method, usually using the method for coking to carry out lighting for the cut heavier than diesel oil distillate processes, main products is hydrotreated naphtha and diesel oil in addition, rare light aromatic hydrocarbon product.
Background technology part should be described emphatically the existing problem of prior art, and solves the existing technical difficulty of this (these) problem, and these to be the application can solve.Employment application although background technology has partly been described a lot, still is not very clear, and what the difficulty of the application's prior art to be solved is.
Summary of the invention
For the deficiencies in the prior art, the object of the present invention is to provide a kind of method of hydrotreating of middle coalite tar, direct production phenol, light aromatic hydrocarbon product and cleaning automotive fuel, and realize long-period stable operation.
The method of hydrotreating of coalite tar comprises following processing step among the present invention:
A) coalite tar carries out fractionation after pretreatment in, obtains carbolic oil, benzoline and pitch;
B) carbolic oil that a) obtains of step carries out dephenolize, obtains phenol products and dephenolize oil;
C) the dephenolize oil that obtains the benzoline, the step b that obtain in a) of step) is mixed into the hydrotreatment reaction zone with hydrogen, and hydrotreatment resultant flow point is from reaching liquid and hydrogen-rich gas, and hydrogen-rich gas recycles;
D) liquid that step c) obtains enters the hydrocracking reaction district, hydrocracking resultant flow point is from obtaining liquid and hydrogen-rich gas, hydrogen-rich gas recycles, the liquid fractionation obtains light naphthar, heavy naphtha, diesel product and tail oil, tail oil can loop back the hydrotreatment reaction zone, also can loop back the hydrocracking reaction district;
E) heavy naphtha that steps d) obtains enters catalytic reforming reaction zone, catalytic reforming production logistics extracting, separates and to obtain light aromatic hydrocarbon product and raffinate oil, and raffinates oil and step 4) light naphthar be mixed to get gasoline products.
The inventive method step a) in, the coal tar that obtains of low-temperature pyrolysis, the coal tar of gasification by-product, perhaps this several mixed coal tar in the preferred coal of described middle coalite tar.Pre-treatment mainly removes moisture and mechanical impurity, specifically can adopt the methods such as centrifuging, electrodesalting and electrodehydrating to carry out pre-treatment.Described carbolic oil is the cut that is rich in phenols.Described benzoline is the cut of doing less than 560 ℃ not carbolic oil, preferably does the cut less than 540 ℃ not carbolic oil, preferably does the cut less than 520 ℃ not carbolic oil.
The inventive method step b) in, the alkali method for extracting is used in described dephenolize, and the phenol products that obtains generally comprises crude phenols, phenol, industrial cresols, ortho-cresol, M-and P-cresols and xylenol etc.Extracting the cut that obtains behind the phenol products is dephenolize oil.
The inventive method step c) in, described hydrotreatment reaction zone operational condition is generally reaction pressure 4.0MPa～20.0MPa, and hydrogen to oil volume ratio is 200: 1～4000: 1, and the cumulative volume air speed is 0.1h
-1～6.0h
-1, 150 ℃～460 ℃ of average reaction temperature; Preferred operational condition is reaction pressure 5.0MPa～19.0MPa, and hydrogen to oil volume ratio is 400: 1～3000: 1, and the cumulative volume air speed is 0.2h
-1～4.0h
-1, 170 ℃～440 ℃ of average reaction temperature.Because a large amount of unsaturated hydro carbons and other easy coking precursors being arranged in the coal tar; therefore use the hydrogenation protecting agent on the top of hydrotreating catalyst; the catalyzer of hydrotreatment reaction zone of the present invention is conventional hydrogenation protecting agent and hydrotreating catalyst, and the volume ratio of two class catalyzer is 10: 90～60: 40.Described hydrogenation protecting agent can be selected existing commercial catalyst, can prepare by this area general knowledge, generally form by carrier and the hydrogenation metal component that is loaded in above it, take catalyst weight as benchmark, comprise group vib active metal component such as tungsten and/or molybdenum in the periodic table of elements, count 1wt%～15wt% with metal oxide, preferred 1wt%～10wt%; And group VIII reactive metal such as nickel and/or cobalt, count 0.1wt%～7wt% with metal oxide, preferred 0.2wt%～6wt%.The carrier that the hydrogenation protecting agent is used is inorganic refractory oxide, and such as aluminum oxide, amorphous silicon aluminium, silicon oxide, titanium oxide etc., shape can be Raschig ring, trifolium, Herba Galii Bungei, trilobed wheel, four impellers, butterfly type, porous ball-type etc.Described hydrotreating catalyst can be selected existing commercial catalyst, can prepare by this area general knowledge, generally form by carrier and the hydrogenation metal component that is loaded in above it, take catalyst weight as benchmark, comprise group vib active metal component such as tungsten and/or molybdenum in the periodic table of elements, count 10wt%～35wt% with metal oxide, preferred 15wt%～30wt%; And group VIII reactive metal such as nickel and/or cobalt, count 1wt%～7wt% with metal oxide, preferred 1.5wt%～6wt%.The carrier that hydrotreating catalyst uses is inorganic refractory oxide, such as aluminum oxide, amorphous silicon aluminium, silicon oxide, titanium oxide etc.
The inventive method steps d) in, described hydrocracking reaction district operational condition is generally reaction pressure 4.0MPa～20.0MPa, and hydrogen to oil volume ratio is 400: 1～4000: 1, and the cumulative volume air speed is 0.2h
-1～6.0h
-1, 300 ℃～460 ℃ of average reaction temperature; Preferred operational condition is reaction pressure 5.0MPa～19.0MPa, and hydrogen to oil volume ratio is 500: 1～3000: 1, and the cumulative volume air speed is 0.2h
-1～4.0h
-1, 320 ℃～450 ℃ of average reaction temperature.The catalyzer in hydrocracking reaction of the present invention district is conventional pretreating catalyst by hydrocracking and hydrocracking catalyst, and the volume ratio of two class catalyzer is 20: 80～70: 30.Described pretreating catalyst by hydrocracking can be selected existing commercial catalyst, can prepare by this area general knowledge, generally form by carrier and the hydrogenation metal component that is loaded in above it, take catalyst weight as benchmark, comprise group vib active metal component such as tungsten and/or molybdenum in the periodic table of elements, count 10wt%～35wt% with metal oxide, preferred 15wt%～30wt%; And group VIII reactive metal such as nickel and/or cobalt, count 1wt%～7wt% with metal oxide, preferred 1.5wt%～6wt%.The carrier that hydrotreating catalyst uses is inorganic refractory oxide, such as aluminum oxide, amorphous silicon aluminium, silicon oxide, titanium oxide etc.The cracking component that described hydrocracking catalyst contains is one or more of amorphous aluminum silicide, Y zeolite, ZSM-5 molecular sieve and beta-molecular sieve.The hydrogenation active metals component of hydrocracking catalyst is generally 5wt%～40wt% in the weight content of oxide compound.The weight content of molecular sieve component in hydrocracking catalyst is generally 0%～60%.Can contain simultaneously other refractory inorganic oxides in the hydrocracking catalyst.
The inventive method steps d) in, the cut point temperature of described tail oil and diesel oil is 300 ℃～385 ℃, preferred 310 ℃～375 ℃.
The inventive method step e) in, the operational condition of catalytic reforming reaction zone is generally reaction pressure 0.3MPa～1.0MPa, and hydrogen/oil mol ratio is 2～6, and the cumulative volume air speed is 0.5h
-1～2.0h
-1, 400 ℃～560 ℃ of average reaction temperature.
The inventive method step e) in, the solvent that extracting is used is tetramethylene sulfone etc.
The inventive method step e) in, described light aromatic hydrocarbons is benzene, toluene, o-Xylol, m-xylene, p-Xylol, Mixed XYLENE, ethylbenzene etc., perhaps their mixture.
The inventive method step c) and steps d) in, the hydrogen that hydrotreatment reaction zone and hydrocracking reaction district need can derive from step e of the present invention) hydrogen that obtains of the product hydrogen manufacturing such as by-product hydrogen, dry distillation of coal coal gas and gasification coal gas that obtain, perhaps their mixture.
The compositing characteristic of coalite tar in the inventive method basis, by pre-treatment, fractionation, dephenolize, hydrotreatment and the combination process processes such as hydrocracking, catalytic reforming to coal tar raw material, can obtain industrial chemicals and the cleaning automotive fuels such as phenols, light aromatic hydrocarbons, premium, fine-quality diesel oil, and the optimization by Technology, catalyzer and operational condition, prolonged cycle of operation of device.Have following advantage: 1) combination process by multiple technology takes full advantage of middle coalite tar resource; 2) isolate bituminous matter and solid particulate matter by the hydrotreatment technology, optimized the raw material of hydrogenation unit; 3) utilize hydrocracking technology to realize at utmost lighting of mink cell focus; 4) take full advantage of the latent heavy naphtha of high virtue, catalytic reforming obtains light aromatic hydrocarbon product, has also reduced hydrogen consumption simultaneously; 5) direct production clean diesel product.
Description of drawings
Fig. 1 is the FB(flow block) of coalite tar method of hydrotreating among the present invention.
Embodiment
Concrete grammar of the present invention is as follows: carry out carrying out in separation column fractionation after the raw materials pretreatment of middle low temperature coal tar, obtain carbolic oil, light ends oil and pitch, wherein carbolic oil carries out phenol removal, obtain phenol products and dephenolize oil, the benzoline that fractionation obtains, dephenolize oil and hydrogen are mixed into the hydrotreatment reaction zone, hydrotreatment generates liquid and enters the hydrocracking reaction district, hydrocracking generates liquid and enters the product separation column, the intermediate oil that fractionation obtains is as the clean diesel product, the tail oil that fractionation obtains loops back hydrocracking reaction district or hydrotreatment reaction zone, the petroleum naphtha that fractionation obtains enters catalytic reforming reaction zone, the hydrogen that catalytic reforming obtains uses in hydrogenation system, the liquid fractionation that obtains obtains light aromatic hydrocarbon product, and catalytic reforming obtains the light naphthar that gasoline fraction and hydrocracking obtain and is mixed to get the clean gasoline product.
Further specify the particular case of invention below by embodiment.The stock oil character that embodiment uses is listed in table 1.
Table 1 stock oil character
| The stock oil title | Coal tar-1 | Coal tar-2 |
| Density (20 ℃), g/cm 3 | 0.985 | 1.037 |
| The boiling range scope, ℃ | 150～580 | 160～650 |
| Sulphur content, wt% | 0.40 | 0.50 |
| Nitrogen content, wt% | 0.80 | 1.20 |
The main character of table 2 the inventive method automotive fuel product
| Project | Embodiment 1 | Embodiment 2 |
| Fractionation | ||
| Lighting end is done, ℃ | 440 | 480 |
| The phenol extracting | ||
| Solvent | Sodium hydroxide | Sodium hydroxide |
| Hydrotreatment | ||
| Average reaction temperature, ℃ | 300 | 350 |
| The hydrogen dividing potential drop, MPa | 12.0 | 16.0 |
| Volume space velocity, h -1 | 0.6 | 0.3 |
| Hydrogen to oil volume ratio | 1000 | 2000 |
| Hydrocracking | ||
| Average reaction temperature, ℃ | 350 | 370 |
| The hydrogen dividing potential drop, MPa | 12.0 | 16.0 |
| Volume space velocity, h -1 | 0.6 | 0.4 |
| Hydrogen to oil volume ratio | 1000 | 1500 |
| Catalytic reforming | ||
| Average reaction temperature, ℃ | 510 | 500 |
| Stagnation pressure, MPa | 0.5 | 0.5 |
| Volume space velocity, h -1 | 1.6 | 1.4 |
| Hydrogen/oil mol ratio | 3.5 | 4.5 |
| Extraction solvent | Tetramethylene sulfone | Tetramethylene sulfone |
Table 3 the inventive method main products yield
| Project | Embodiment 1 | Embodiment 2 |
| Gasoline, wt% | 21.3 | 18.6 |
| Diesel oil, wt% | 35.4 | 45.0 |
| Phenols, wt% | 20.6 | 14.7 |
| Light aromatic hydrocarbons, wt% | 17.6 | 16.9 |
The main character of table 4 the inventive method automotive fuel product
| Project | Embodiment 1 | Embodiment 2 |
| Gasoline | ||
| Density (20 ℃), g/cm 3 | 0.749 | 0.755 |
| Boiling range, ℃ | 40～180 | 42～168 |
| S，μg/g | ＜0.5 | ＜0.5 |
| N，μg/g | ＜0.5 | ＜0.5 |
| RON | 85 | 89 |
| Diesel oil | ||
| Density (20 ℃), g/cm 3 | 0.842 | 0.860 |
| Boiling range, ℃ | 167～340 | 160～365 |
| 10% steams excess carbon residue, % | ＜0.01 | ＜0.01 |
| Condensation point, ℃ | ＜-50 | ＜-35 |
| Cetane value | 52 | 46 |
| S，μg/g | ＜5 | ＜5 |
| N，μg/g | ＜1 | ＜1 |
The main character of several phenol products of table 4 the inventive method
Can find out from above-described embodiment, can be produced by middle coalite tar industrial chemicals and the high-quality automotive fuels such as phenol products, light aromatic hydrocarbons, gasoline and diesel oil by the inventive method.
Claims (10)
1. the method for hydrotreating of coalite tar in a kind is characterized in that comprising following processing step:
A) coalite tar carries out fractionation after pretreatment in, obtains carbolic oil, benzoline and pitch;
B) carbolic oil that a) obtains of step carries out dephenolize, obtains phenol products and dephenolize oil;
C) the dephenolize oil that the benzoline, the step b that obtain in a) of step) obtains is mixed into the hydrotreatment reaction zone with hydrogen, and hydrotreatment resultant flow point is from reaching liquid and hydrogen-rich gas, and hydrogen-rich gas recycles;
D) liquid that step c) obtains enters the hydrocracking reaction district, hydrocracking resultant flow point is from obtaining liquid and hydrogen-rich gas, hydrogen-rich gas recycles, the liquid fractionation obtains light naphthar, heavy naphtha, diesel product and tail oil, and tail oil loops back the hydrotreatment reaction zone or loops back the hydrocracking reaction district;
E) heavy naphtha that steps d) obtains enters catalytic reforming reaction zone, catalytic reforming production logistics extracting, separates and to obtain light aromatic hydrocarbon product and raffinate oil, and raffinates oil and step 4) light naphthar be mixed to get gasoline products.
2. it is characterized in that in accordance with the method for claim 1: the middle coalite tar of step (a) is the coal tar that low-temperature pyrolysis obtains in the coal, coal tar or this several mixed coal tar of gasification by-product.
3. in accordance with the method for claim 1, it is characterized in that: the pre-treatment of step (a) mainly removes moisture and mechanical impurity, specifically can adopt the methods such as centrifuging, electrodesalting and electrodehydrating to carry out pre-treatment.
4. in accordance with the method for claim 1, it is characterized in that: step described carbolic oil a) is the cut that is rich in phenols, described benzoline is the cut of doing less than 560 ℃ not carbolic oil, preferably do the cut less than 540 ℃ not carbolic oil, preferably do the cut less than 520 ℃ not carbolic oil.
5. in accordance with the method for claim 1, it is characterized in that: the alkali method for extracting is used in dephenolize step b), the phenol products that obtains comprises crude phenols, phenol, industrial cresols, ortho-cresol, M-and P-cresols and xylenol, and extracting the cut that obtains behind the phenol products is dephenolize oil.
6. in accordance with the method for claim 1, it is characterized in that: hydrotreatment reaction zone operational condition step c) is reaction pressure 4.0MPa～20.0MPa, and hydrogen to oil volume ratio is 200: 1～4000: 1, and the cumulative volume air speed is 0.1h
-1～6.0h
-1, 150 ℃～460 ℃ of average reaction temperature; Preferred operational condition is reaction pressure 5.0MPa～19.0MPa, and hydrogen to oil volume ratio is 400: 1～3000: 1, and the cumulative volume air speed is 0.2h
-1～4.0h
-1, 170 ℃～440 ℃ of average reaction temperature; The catalyzer of hydrotreatment reaction zone step c) is conventional hydrogenation protecting agent and hydrotreating catalyst, and the volume ratio of two class catalyzer is 10: 90～60: 40.
7. in accordance with the method for claim 1, it is characterized in that: hydrocracking reaction district operational condition steps d) is reaction pressure 4.0MPa～20.0MPa, and hydrogen to oil volume ratio is 400: 1～4000: 1, and the cumulative volume air speed is 0.2h
-1～6.0h
-1, 300 ℃～460 ℃ of average reaction temperature; Preferred operational condition is reaction pressure 5.0MPa～19.0MPa, and hydrogen to oil volume ratio is 500: 1～3000: 1, and the cumulative volume air speed is 0.2h
-1～4.0h
-1, 320 ℃～450 ℃ of average reaction temperature; Steps d) catalyzer in hydrocracking reaction district is conventional pretreating catalyst by hydrocracking and hydrocracking catalyst, and the volume ratio of two class catalyzer is 20: 80～70: 30.
8. in accordance with the method for claim 1, it is characterized in that: the cut point temperature of tail oil steps d) and diesel oil is 300 ℃～385 ℃, preferred 310 ℃～375 ℃.
9. in accordance with the method for claim 1, it is characterized in that: step e) operational condition of catalytic reforming reaction zone is reaction pressure 0.3MPa～1.0MPa, and hydrogen/oil mol ratio is 2～6, and the cumulative volume air speed is 0.5h
-1～2.0h
-1, 400 ℃～560 ℃ of average reaction temperature.
10. it is characterized in that in accordance with the method for claim 1: the solvent that extracting step e) is used is tetramethylene sulfone.
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| CN103965078A (en) * | 2014-05-05 | 2014-08-06 | 大连理工大学 | Method for preparing benzonitrile and clean fuel from dephenolized carbolic oil |
| CN104194828A (en) * | 2014-08-06 | 2014-12-10 | 何巨堂 | Inferior hydrocarbon hydrogenation method comprising reaction heat recycling step |
| WO2015077052A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Method of converting a coal to chemicals |
| WO2015076980A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for pyrolysis and gasification of a coal feed |
| WO2015076993A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Hydrocracking process for a hydrocarbon stream |
| WO2015076972A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for producing olefins from a coal feed |
| WO2015076979A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for hydrotreating a coal tar stream |
| WO2015077039A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Hydroprocess for a hydrocarbon stream from coal tar |
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| WO2015076979A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for hydrotreating a coal tar stream |
| WO2015077045A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for hydrotreating a coal tar stream |
| WO2015077052A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Method of converting a coal to chemicals |
| WO2015076980A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for pyrolysis and gasification of a coal feed |
| WO2015076993A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Hydrocracking process for a hydrocarbon stream |
| WO2015076972A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Process for producing olefins from a coal feed |
| CN105722953B (en) * | 2013-11-19 | 2018-09-18 | 环球油品公司 | The method for converting coal into chemicals |
| WO2015077039A1 (en) * | 2013-11-19 | 2015-05-28 | Uop Llc | Hydroprocess for a hydrocarbon stream from coal tar |
| CN105722951A (en) * | 2013-11-19 | 2016-06-29 | 环球油品公司 | Hydrocracking process for a hydrocarbon stream |
| CN105722953A (en) * | 2013-11-19 | 2016-06-29 | 环球油品公司 | Method of converting a coal to chemicals |
| CN103965078A (en) * | 2014-05-05 | 2014-08-06 | 大连理工大学 | Method for preparing benzonitrile and clean fuel from dephenolized carbolic oil |
| CN104194828A (en) * | 2014-08-06 | 2014-12-10 | 何巨堂 | Inferior hydrocarbon hydrogenation method comprising reaction heat recycling step |
| CN106635153A (en) * | 2015-10-29 | 2017-05-10 | 中国石油化工股份有限公司 | Processing method of medium and low-temperature coal tar whole distillate |
| CN106635153B (en) * | 2015-10-29 | 2018-03-20 | 中国石油化工股份有限公司 | A kind of processing method of the full cut of middle coalite tar |
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Application publication date: 20130130 |