CN206204239U - A kind of system of fast pyrogenation coal tar - Google Patents
A kind of system of fast pyrogenation coal tar Download PDFInfo
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- CN206204239U CN206204239U CN201620890890.2U CN201620890890U CN206204239U CN 206204239 U CN206204239 U CN 206204239U CN 201620890890 U CN201620890890 U CN 201620890890U CN 206204239 U CN206204239 U CN 206204239U
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Abstract
The utility model discloses a kind of system of fast pyrogenation coal tar.It includes：Blender, floating bed hydrogenation reactor, separator, filter, vacuum distillation tower, hydrofinishing cracking reaction unit, destilling tower, knockout drum, hydrofining reactor and the first hydrogen inlet；Floating bed hydrogenation reactor is connected with blender, separator and the first hydrogen inlet respectively, filter is connected with separator and vacuum distillation tower respectively, hydrofinishing cracking reaction unit is connected with vacuum distillation tower and destilling tower respectively, knockout drum is connected with destilling tower and hydrofining reactor respectively, and hydrofining reactor is also connected with vacuum distillation tower.The system can process the fast pyrogenation coal tar of dust content high, and coal tar after floating bed hydrogenation treatment is easy to that residue component is removed by filtration, it is to avoid it directly distills the coking risk brought.
Description
Technical field
The utility model is related to effective utilization of coal tar, and in particular to a kind of system of fast pyrogenation coal tar.
Background technology
Coal sub-prime, using being considered as the efficient effective way for utilizing of Coal Clean, is also China " 13 " Coal Chemical Industry
Prior development direction.It is exactly first to be separated heterogeneity in coal by pyrolysis that the sub-prime of coal is utilized, including coal gas, Jiao
Oil and semicoke etc..Coal tar can produce gasoline, diesel oil and chemical products by hydrogenation, and semicoke becomes low volatilization by pyrolysis
Point, the clean fuel of low-sulfur or raw material.
Coal sub-prime utilizes the pyrolytic technique that " tap " is coal, to extract tar, the coal gas of scale production quantities, and coal sub-prime is utilized
Scale, maximization are needed, single set pyrolysis of coal unit scale is more and more large-scale, and pyrolysis rate is also improved rapidly, coal is in warm
Residence time in solution stove is only several seconds, also commonly referred to as fast pyrogenation, and pyrolysis oil gas overflows speed soon, the coal tar of output
Mostly middle coalite tar, its property has bigger difference with the coal tar of conventional coking output.
The coal tar generated in the middle low-temperature rapid thermal solution preocess of fine coal is generally oily under water, and substantial amounts of coal dust is contained in tar
And coal ash, gum asphaltic content is high, and viscosity is larger, and water content is higher, and heat endurance is poor, especially in low crude oil price
In generation, the economy important in inhibiting that the deep processing of high-efficiency and economic is utilized to coal sub-prime is carried out to fast pyrogenation coal tar；Cause
This is, it is necessary to develop suitable system of processing.
Utility model content
To solve the above problems, the utility model contains more dust (such as toluene insolubles there is provided a kind of fast pyrogenation
It is many with content of impurities) coal tar system.
The utility model discloses a kind of system of fast pyrogenation coal tar.It includes：Blender, floating bed hydrogenation reaction
Device, separator, filter, vacuum distillation tower, hydrofinishing-cracking reaction unit, destilling tower, knockout drum, hydrofining reaction
Device and the first hydrogen inlet；
The blender is provided with the outlet of catalyst inlet, coal tar oil-in and mixed material；
The floating bed hydrogenation reactor is provided with mixed material entrance and hydrogenation products outlet, the mixed material entrance point
It is not connected with mixed material outlet and first hydrogen inlet；
The separator is provided with hydrogenation products entrance and liquid product outlet, and the hydrogenation products entrance and the hydrogenation are produced
Thing outlet is connected；
The filter is provided with liquid product entrance and oil-phase product outlet, and the liquid product entrance and the liquid phase are produced
Thing outlet is connected；
The vacuum distillation tower is provided with oil-phase product entrance, the first light fraction outlet and restructuring sub-export, and the oil phase is produced
Thing entrance is connected with oil-phase product outlet；
The hydrofinishing-cracking reaction unit, it is provided with restructuring subentry and cracking oil export, the restructuring subentry
It is connected with the restructuring sub-export；
The destilling tower is provided with cracking oil-in and the second light fraction outlet, and the cracking oil-in and the cracked oil go out
Mouth is connected；
The knockout drum is provided with the second light component entrance and the 3rd light fraction outlet, the second light component entrance and described
Second light fraction outlet is connected；
The hydrofining reactor is provided with the outlet of the second hydrogen inlet, the 4th light component entrance and aromatic hydrocarbons, the described 4th
Light component entrance is connected with first light fraction outlet and the 3rd light fraction outlet respectively.
In an embodiment of the present utility model, the destilling tower is additionally provided with gasoline fraction outlet, diesel oil distillate and goes out
Mouth and wax oil fraction outlets.
In an embodiment of the present utility model, the destilling tower is additionally provided with hydrogenation tail oil outlet, the hydrogenation essence
System-cracking reaction unit is additionally provided with hydrogenation tail oil entrance, and the hydrogenation tail oil entrance is connected with hydrogenation tail oil outlet.
The utility model can process the fast pyrogenation coal tar of dust content high, and coal tar is processed through floating bed hydrogenation
After be easy to that residue component is removed by filtration, it is to avoid it directly distills the coking risk brought.
Additionally, coal tar first isolates the first light component after being processed through floating bed hydrogenation, heavy component carries out hydrogenation essence again
Make and be hydrocracked, it is to avoid the loss of aromatic hydrocarbons can significantly improve the lighting degree of heavy coal tar in the first light component,
The light components of preparing aromatic hydrocarbon (BTX) can be obtained with maximum, while clean fuel can be produced with simultaneous, adding for heavy coal tar is improved
Work economy.
Brief description of the drawings
Fig. 1 is a kind of structural representation of the system of the fast pyrogenation coal tar in the utility model embodiment.
In figure：
1st, blender；1-1, catalyst inlet；1-2, coal tar oil-in；1-3, mixed material outlet；
2nd, floating bed hydrogenation reactor；2-1, mixed material entrance；2-2, hydrogenation products outlet；
3rd, separator；3-1, hydrogenation products entrance；3-2, liquid product outlet；3-3, gas vent；
4th, filter；4-1, liquid product entrance；4-2, oil-phase product outlet；4-3, solid discharge；
5th, vacuum distillation tower；5-1, oil-phase product entrance；5-2, restructuring sub-export；5-3, the first light fraction outlet；
6th, hydrofinishing-cracking reaction unit；6-1, restructuring subentry；6-2, cracking oil export；6-3, hydrogenation tail oil enter
Mouthful；
7th, destilling tower；7-1, cracking oil-in；7-2, the second light fraction outlet；7-3, gasoline fraction outlet；7-4, diesel oil
Fraction outlets；7-5, wax oil fraction outlets；7-6, hydrogenation tail oil outlet；
8th, knockout drum；8-1, the second light component entrance；8-2, the 3rd light fraction outlet；8-3, fixed gas outlet；
9th, hydrofining reactor；9-1, the 4th light component entrance；9-2, the second hydrogen inlet；9-3, aromatic hydrocarbons outlet；
10th, aromatics seperation unit；10-1, benzene outlet；10-2, toluene outlet；10-3, mixed xylenes outlet；It is 10-4, mixed
Close aromatic hydrocarbons outlet；
11st, the first hydrogen inlet.
Specific embodiment
Below in conjunction with drawings and Examples, specific embodiment of the present utility model is described in more details, with
Just better understood when the advantage of scheme of the present utility model and its various aspects.However, specific implementations described below side
Formula and embodiment are only descriptive purposes, rather than to limitation of the present utility model.
It should be noted that it must be 1-2 rings and a small amount of thrcylic aromatic hydrocarbon compound that " light component " in the utility model refers to；
" heavy constituent " refer to must be most Fourth Rings and the above polycyclic aromatic hydrocarbon；What " hydrogenation tail oil " referred to is cracked oil by after air-distillation
Residue, its major part is uncracked saturated hydrocarbons in hydrocracking process.Additionally, the term " in the utility model
One ", " second ", " the 3rd " or " the 4th " is only used for describing purpose, and it is not intended that indicating or implying relative importance or hidden
Containing the quantity for indicating indicated technical characteristic, thus, define " first ", " second ", " the 3rd " or the feature of " the 4th " can
To express or implicitly include one or more this feature.
As shown in figure 1, the utility model discloses a kind of system of fast pyrogenation coal tar.It includes：It is blender 1, outstanding
Floating bed hydrogenation reactor 2, separator 3, filter 4, vacuum distillation tower 5, hydrofinishing-cracking reaction unit 6, destilling tower 7, point
From tank 8, hydrofining reactor 9, the hydrogen inlet 11 of aromatics seperation unit 10 and first.
Blender 1 is provided with catalyst inlet 1-1, coal tar oil-in 1-2, mixed material outlet 1-3.
Floating bed hydrogenation reactor 2 is provided with mixed material entrance 2-1 and hydrogenation products outlet 2-2, mixed material entrance 2-1
1-3 is exported with mixed material and the first hydrogen inlet 11 is connected respectively.
Separator 3 is provided with hydrogenation products entrance 3-1, liquid product outlet 3-2 and gas vent 3-3, hydrogenation products entrance
3-1 is connected with hydrogenation products outlet 2-2.
Filter 4 is provided with liquid product entrance 4-1, oil-phase product outlet 4-2 and solid discharge 4-3, liquid product entrance
4-1 is connected with liquid product outlet 3-2.
Vacuum distillation tower 5 is provided with oil-phase product entrance 5-1, restructuring sub-export 5-2 and the first light fraction outlet 5-3, oil phase
Product inlet 5-1 and oil-phase product outlet 4-2.
Hydrofinishing-cracking reaction unit 6, it is provided with restructuring subentry 6-1, cracking oil export 6-2 and hydrogenation tail oil and enters
Mouth 6-3, restructuring subentry 6-1 are connected with restructuring sub-export 5-2.
Destilling tower 7 is provided with cracking oil-in 7-1, the second light fraction outlet 7-2, gasoline fraction outlet 7-3, diesel oil distillate and goes out
Mouth 7-4, wax oil fraction outlets 7-5 and hydrogenation tail oil export 7-6, and cracking oil-in 7-1 is connected with cracking oil export 6-2.
Knockout drum 8 is provided with the second light component entrance 8-1, the 3rd light fraction outlet 8-2 and fixed gas outlet 8-3, and second is light
Component entrance 8-1 and the second light fraction outlet 7-2 is connected.
Hydrofining reactor 9 is provided with the 4th light component entrance 9-1, the second hydrogen inlet 9-2 and aromatic hydrocarbons outlet 9-3, the
Four light component entrance 9-1 are connected with the first light fraction outlet 5-3 and the 3rd light fraction outlet 8-2 respectively.
Aromatics seperation unit 10 is provided with aromatic hydrocarbons entrance, benzene outlet 10-1, toluene outlet 10-2, mixed xylenes outlet 10-3
10-4 is exported with other BTX aromatics, aromatic hydrocarbons entrance is connected with aromatic hydrocarbons outlet 9-3.
Blender 1 is used for mixed coal tar and suspension bed hydrogenation catalyst.
Floating bed hydrogenation reactor 2 is used to for the macromolecular in coal tar to carry out thermal cracking and hydrogenation.
Separator 3 is used to remove the gas in hydrogenation products (product after coal tar hydrogenating), and remaining hydrogenation products are
Liquid product.
Filter 4 is used to remove the residue in liquid product, and remaining liquid product is oil-phase product.
Vacuum distillation tower 5 is used to separate the first light component and heavy constituent in oil-phase product.
Hydrofinishing-cracking reaction unit 6 is used to carry out heavy constituent hydrofinishing and be hydrocracked, to produce cracking
Oil.
Destilling tower 7 is atmospheric distillation tower, for being distilled to cracked oil, isolates the second light component.Steaming shown in Fig. 1
Tower 7 is evaporated in addition to being provided with cracking oil-in 7-1 and the second light fraction outlet 7-2, is additionally provided with gasoline fraction outlet 7-3, diesel oil and is evaporated
Sub-export 7-4, wax oil fraction outlets 7-5 and hydrogenation tail oil outlet 7-6, therefore, cracked oil can be with after distilling in the destilling tower 7
Gasoline, diesel oil and wax oil is obtained.Additionally, hydrofinishing-cracking reaction the unit 6 shown in Fig. 1 is provided with hydrogenation tail oil entrance 6-3,
Hydrogenation tail oil outlet 7-6 is connected with hydrogenation tail oil entrance 6-3, i.e., cracked oil can send by remaining hydrogenation tail oil after air-distillation
Return to and carry out hydrofinishing again in hydrofinishing-cracking reaction unit 6 and be hydrocracked.Hydrogenation tail oil entrance 6-3, gasoline evaporate
Sub-export 7-3, diesel oil distillate outlet 7-4, wax oil fraction outlets 7-5 and hydrogenation tail oil outlet 7-6 are not indispensability, can basis
Actual technological requirement is increased and decreased.
Knockout drum 8 is used to remove the fixed gas in the second light component, and remaining light component is herein defined as the 3rd
Light component.
Hydrofining reactor 9 is used to for obtained first light component and the 3rd light component to carry out hydrofinishing again, makes
Obtain refined oil.
Aromatics seperation unit 10 is used for the various aromatics seperations in refined oil out.Aromatics seperation unit 10 is not system
Indispensable equipment, refined oil can carry out separation can also be not isolated, and can be increased and decreased according to actual technological requirement.Figure
Aromatics seperation unit 10 shown in 1 is used to prepare benzene, toluene and mixed xylenes, and certain aromatics seperation unit 10 can be additionally used in system
Standby others aromatic hydrocarbons.
The system can process the fast pyrogenation coal tar of dust content high, and coal tar is easy after floating bed hydrogenation treatment
In residue component is removed by filtration, it is to avoid it directly distills the coking risk brought.The system can be obtained with maximum and produced
The light components of aromatic hydrocarbons, while clean fuel (gasoline, diesel oil, wax oil etc.) can be produced with simultaneous.
Remaining hydrogenation tail oil has been sent back in hydrofinishing-cracking reaction unit 6 and has been hydrogenated with again after cracked oil distillation
Refined and hydrocracking reaction, can so improve the yield of aromatic hydrocarbons and clean fuel.Certainly, hydrogenation tail oil can also separately make him
With can be determined according to actual technological requirement.
The system can process the fast pyrogenation coal tar of dust content high, and coal tar is easy after floating bed hydrogenation treatment
In residue component is removed by filtration, it is to avoid it directly distills the coking risk brought.
Additionally, coal tar first isolates the first light component after being processed through floating bed hydrogenation, heavy component carries out hydrogenation essence again
Make and be hydrocracked, it is to avoid the loss of aromatic hydrocarbons can significantly improve the lighting degree of heavy coal tar in the first light component,
The light components of preparing aromatic hydrocarbon can be obtained with maximum, while clean fuel can be produced with simultaneous, the processing warp of heavy coal tar is improved
Ji property.
Below with reference to specific embodiment, the utility model is illustrated.
Technological process used by following embodiments is as follows：
Mixing：To be well mixed in coal tar and suspension bed hydrogenation catalyst feeding blender 1, mixed material is obtained；
Floating bed hydrogenation：To be reacted in mixed material and hydrogen feeding floating bed hydrogenation reactor 2, hydrogenation products are obtained；
It is first to separate：Separated during hydrogenation products are sent into separator 3, liquid product is obtained；
Filtering：Filtered during liquid product is sent into filter 4, oil-phase product is obtained；
Vacuum distillation：Distilled during oil-phase product is sent into vacuum distillation tower 5, the first light component and heavy constituent is obtained；
Hydrofinishing-cracking：Restructuring is distributed into hydrofinishing-cracking reaction unit 6 to carry out hydrofinishing respectively anti-
Should and hydrocracking reaction, be obtained cracked oil；
Air-distillation：Distilled during cracked oil is sent into destilling tower 7, the second light component, gasoline, diesel oil and wax oil is obtained, and
Hydrofinishing and hydrocracking reaction are carried out again during remaining hydrogenation tail oil is sent into the anti-unit 6 of hydrofinishing-cracking；
Secondary separation：Separated during second light component is sent into knockout drum 8, the 3rd light component is obtained；
Hydrofinishing：First light component and the 3rd light component are mixed, the 4th light component is obtained, and the 4th light component is sent
Enter reaction in hydrofining reactor 9, aromatic hydrocarbons is obtained；
Aromatics seperation：To be separated in obtained aromatic hydrocarbons feeding aromatics seperation unit 10, and benzene, toluene be obtained respectively and mixes
Close dimethylbenzene.
Institute's taking technique condition value is exemplary, for example foregoing utility model of its desirable number range in following embodiments
Shown in content.Detection method used by following embodiments is the conventional detection method of the industry.Used by following embodiments
The main character of fast pyrogenation coal tar is see table 1.
Embodiment 1
System used by the present embodiment is as shown in Figure 1.
Suspension bed hydrogenation catalyst in the present embodiment used by floating bed hydrogenation step for josephinite (iron content 48.5wt%,
Nickeliferous 1.5wt%), particle diameter is 65-75 μm, and addition is 2.0wt% (accounting for the mass fraction of suspension bed charging, similarly hereinafter), reaction
Condition is：Reaction pressure 18MPa, reaction temperature is 420 DEG C.
The hydrogenation active component choosing of Hydrobon catalyst and hydrocracking catalyst used by hydrofinishing-hydrocracking step
Select Ni, W composition metal, wherein NiO and WO3Content be respectively 3.1wt%, 16.7wt%, carrier is γ-Al2O3, react bar
Part is：Reaction pressure 10MPa, 400 DEG C of reaction temperature, volume space velocity 1.0h-1.The cracking active component choosing of hydrocracking catalyst
Y type molecular sieve is selected, carrier is γ-Al2O3, reaction pressure 8MPa, 380 DEG C of reaction temperature, volume space velocity 1.0h-1。
Active component selection Co, Mo of Hydrobon catalyst used by hydrofinishing step, the matter of wherein CoO and MoO
Amount fraction is respectively 2.0wt%, 8.0wt%, 320 DEG C of reaction temperature, reaction pressure 3.0MPa, volume space velocity 1.0h during liquid-1, hydrogen
Oil volume ratio is 800:1.
The primary product distribution of the present embodiment is shown in Table 2.
Embodiment 2
System used by the present embodiment is as shown in Figure 1.
Suspension bed hydrogenation catalyst in the present embodiment used by floating bed hydrogenation step is red mud (iron content 37.8wt%), grain
Footpath is 60-70 μm, and addition is 3.0wt%, and reaction condition is：Reaction pressure 20.0MPa, reaction temperature is 460 DEG C.
The hydrogenation active component choosing of Hydrobon catalyst and hydrocracking catalyst used by hydrofinishing-hydrocracking step
Select Ni, W composition metal, wherein NiO and WO3Content be respectively 3.1wt%, 16.7wt%, carrier is γ-Al2O3, react bar
Part is：Reaction pressure 12MPa, 420 DEG C of reaction temperature, volume space velocity 1.0h-1.The cracking active component choosing of hydrocracking catalyst
Super-stable Y molecular sieves are selected, carrier is γ-Al2O3, reaction pressure 10MPa, 400 DEG C of reaction temperature, volume space velocity 1.0h-1。
Active component selection Co, Mo of Hydrobon catalyst used by hydrofinishing step, the matter of wherein CoO and MoO
Amount fraction is respectively 2.0wt%, 8.0wt%, 350 DEG C of reaction temperature, reaction pressure 4.0MPa, volume space velocity 1.5h during liquid-1, hydrogen
Oil volume ratio is 1000:1.
The primary product distribution of the present embodiment is shown in Table 2.
The main character of the fast pyrogenation coal tar of table 1
The primary product distribution of the embodiment of table 2
As known from Table 1, the content of Conradson carbon residue is up to 27.3wt% in the fast pyrogenation coal tar that above-described embodiment is used,
Toluene insolubles and mechanical admixture are respectively 16.0wt and 4.0wt%.
As known from Table 2, in above-described embodiment 1, the yield of aromatic hydrocarbons (BTX) is 36.14wt%, gasoline fraction, diesel oil distillate
And the yield of wax oil cut is respectively 12.78wt%, 33.74wt% and 11.68wt%；In above-described embodiment 2, aromatic hydrocarbons (BTX)
Yield be 34.69wt%, the yield of gasoline fraction, diesel oil distillate and wax oil cut is respectively 10.56wt%, 32.33wt%
And 13.86wt%.Understand, compared to existing technology, system provided by the utility model can obtain preparing aromatic hydrocarbon with maximum
Light components, obtain aromatic hydrocarbons (BTX) composition higher, while clean fuel can be produced with simultaneous, improve the processing warp of heavy coal tar
Ji property.
In summary, the utility model can process dust content high (content of toluene insolubles and mechanical admixture is high)
Fast pyrogenation coal tar, and coal tar through floating bed hydrogenation process after be easy to that residue component is removed by filtration, it is to avoid its is direct
The coking risk that distillation brings.
Additionally, coal tar first isolates the first light component after being processed through floating bed hydrogenation, heavy component carries out hydrogenation essence again
Make and be hydrocracked, it is to avoid the loss of aromatic hydrocarbons can significantly improve the lighting degree of heavy coal tar in the first light component,
The light components of preparing aromatic hydrocarbon can be obtained with maximum, while clean fuel can be produced with simultaneous, the processing warp of heavy coal tar is improved
Ji property.
It should be noted that each embodiment above by reference to described by accompanying drawing is only used to illustrate the utility model rather than limit
Scope of the present utility model is made, it will be understood by those within the art that, do not departing from spirit of the present utility model and model
The modification carried out to the utility model on the premise of enclosing or equivalent, all should cover within the scope of the utility model.
Additionally, unless stated otherwise, then all or part of of any embodiment can be with reference to the whole or of any other embodiment
Part uses.
Claims (3)
1. a kind of system of fast pyrogenation coal tar, it is characterised in that it includes：Blender, floating bed hydrogenation reactor, separation
Device, filter, vacuum distillation tower, hydrofinishing-cracking reaction unit, destilling tower, knockout drum, hydrofining reactor and first
Hydrogen inlet；
The blender is provided with the outlet of catalyst inlet, coal tar oil-in and mixed material；
The floating bed hydrogenation reactor be provided with mixed material entrance and hydrogenation products outlet, the mixed material entrance respectively with
The mixed material outlet is connected with first hydrogen inlet；
The separator is provided with hydrogenation products entrance and liquid product outlet, and the hydrogenation products entrance and the hydrogenation products go out
Mouth is connected；
The filter is provided with liquid product entrance and oil-phase product outlet, and the liquid product entrance and the liquid product go out
Mouth is connected；
The vacuum distillation tower is provided with oil-phase product entrance, the first light fraction outlet and restructuring sub-export, and the oil-phase product enters
Mouth is connected with oil-phase product outlet；
The hydrofinishing-cracking reaction unit, it is provided with restructuring subentry and cracking oil export, the restructuring subentry and institute
Restructuring sub-export is stated to be connected；
The destilling tower is provided with cracking oil-in and the second light fraction outlet, the cracking oil-in and the cracking oil export phase
Even；
The knockout drum is provided with the second light component entrance and the 3rd light fraction outlet, the second light component entrance and described second
Light fraction outlet is connected；
The hydrofining reactor is provided with the outlet of the second hydrogen inlet, the 4th light component entrance and aromatic hydrocarbons, described 4th light group
Subentry is connected with first light fraction outlet and the 3rd light fraction outlet respectively.
2. system according to claim 1, it is characterised in that the destilling tower is additionally provided with gasoline fraction outlet, diesel oil and evaporates
Sub-export and wax oil fraction outlets.
3. system according to claim 1, it is characterised in that the destilling tower is additionally provided with hydrogenation tail oil outlet, it is described plus
Hydrogen is refined-and cracking reaction unit is additionally provided with hydrogenation tail oil entrance, and the hydrogenation tail oil entrance is connected with hydrogenation tail oil outlet.
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| CN201620890890.2U CN206204239U (en) | 2016-08-16 | 2016-08-16 | A kind of system of fast pyrogenation coal tar |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106065336A (en) * | 2016-08-16 | 2016-11-02 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for fast pyrogenation coal tar |
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2016
- 2016-08-16 CN CN201620890890.2U patent/CN206204239U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106065336A (en) * | 2016-08-16 | 2016-11-02 | 北京神雾环境能源科技集团股份有限公司 | A kind of system and method for fast pyrogenation coal tar |
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Address after: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee after: Shenwu science and technology group Limited by Share Ltd Address before: 102200 Beijing City, Changping District science and Technology Park Chang Huai Lu No. 155 Patentee before: Beijing Shenwu Environment Energy Technology Group Co., Ltd. |
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Granted publication date: 20170531 Effective date of abandoning: 20171124 |
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