CN101798515A - Process for co-production of high-quality carbon black raw oil, refined asphalt and binder asphalt - Google Patents
Process for co-production of high-quality carbon black raw oil, refined asphalt and binder asphalt Download PDFInfo
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Abstract
The invention relates to deep processing technology of coal-tar asphalt, in particular to the process for co-production of high-quality carbon black raw oil, refined asphalt and binder asphalt. The process comprises a step of mixing crude coal-tar asphalt and a solvent in a certain ratio and injecting the mixture into an extraction separator for separating, wherein the process comprises technical steps: mixing the crude coal-tar asphalt and the solvent in a certain ratio and injecting the mixture into the extraction separator and performing extraction, flocculation, sedimentation and separation; extracting a light phase component, a secondary light phase component and a heavy phase component from an upper position, a middle position and a lower position of the separator respectively according to a density distribution principle; and controlling the ratio between double solvents and the ratio between the double solvent and the crude coal-tar asphalt, wherein the double solvents consist of an aromatic solvent and an aliphatic solvent. The process not only can obtain the high-quality carbon black raw oil with a high additional value and prepare pure refined asphalt and carbon for needle coke and the binder asphalt for a refractory material product, and but also has no waste emitted in the overall technical process.
Description
Technical field
The present invention relates to a kind of coal-tar pitch deep process technology.The technology of especially a kind of co-production of high-quality carbon black raw oil, refined asphaltic bitumen and binder pitch.Carbon black raw oil is used to produce high-grade graphitized carbon black, and refined asphaltic bitumen is used to prepare coal-based needle coke and coal-tar pitch charcoal fiber, and binder pitch is used for the binding agent of charcoal element, fire resistive material product.
Background technology
At present coal tar is that carbon black raw oil production is that rough coal tar is carried out predistillation, distill out light oil, carbolic oil, naphtalene oil and washing oil after, the carbolineum that remaining coal tar soft asphalt is added suitable proportion is adjusted, and makes carbon black raw oil.This preparation method does not separate the heavy constituent in the coal tar and a quinoline insolubles, and the carbon black raw oil that is obtained is second-rate, can only can not be used to produce the raw material of high-grade graphitized carbon black as producing low-grade sooty raw material.
The production coal-based needle coke is crude coal-tar asphalt and solvent to be mixed back injection extracting and separating tower by a certain percentage separate with the reparation technology method of refined asphaltic bitumen at present, obtain light phase component and heavy phase component respectively, light phase component obtains refined asphaltic bitumen and solvent through rectifying separation, and the heavy phase component obtains binder pitch and solvent through rectifying separation.This technology is not separated low-molecular-weight component in the viscid bitumen separately, makes that the molecular weight distribution of refined asphaltic bitumen is unreasonable, affects the quality of refined asphaltic bitumen derived product.Simultaneously the course of processing of this technology is not separated the carbon black raw oil of the high added value that contains in the light phase component.
Summary of the invention
The objective of the invention is deficiency, the technology of a kind of co-production of high-quality carbon black raw oil, refined asphaltic bitumen and binder pitch is provided at above-mentioned technology existence.This technology not only can obtain the high-quality carbon black raw oil of high added value simultaneously and produce pure refined asphaltic bitumen that needle coke uses and charcoal element, fire resistive material product binder pitch, and whole technological process do not have waste discharge, meets the demand for development of recycling economy.
The objective of the invention is to be achieved through the following technical solutions.
The technology of co-production of high-quality carbon black raw oil of the present invention, refined asphaltic bitumen and binder pitch, comprise that crude coal-tar asphalt and solvent are mixed back injection extraction separator by a certain percentage to be separated, it is characterized in that described solvent is a solvent pairs, obtain high-quality carbon black raw oil, refined asphaltic bitumen and three kinds of products of binder pitch simultaneously, processing step is:
1) crude coal-tar asphalt and solvent pairs are mixed back injection extraction separator by a certain percentage, extract flocculating settling and separate, take out light phase component, inferior light phase component and heavy phase component from the upper, middle and lower different positions of separator respectively according to the density distribution principle;
2) ratio between the control solvent pairs and the ratio between solvent pairs and the crude coal-tar asphalt.
3) will extract the flocculating settling temperature is controlled in 70 ℃～160 ℃ scopes;
4) will extract flocculation settling velocity is controlled in 50mm/h～250mm/h scope;
5) rectifying separation of light phase component, inferior light phase component and heavy phase component, normal pressure is controlled 270 ℃～310 ℃ of light phase rectifying tower top temperature down, 270 ℃～310 ℃ of inferior light phase rectifying tower tower top temperatures, 270 ℃～310 ℃ of heavy phase rectifying tower tower top temperatures, the operating parameters that heavy phase rectifying tower side stream temperature is 285 ℃～320 ℃, light phase component obtains high-quality carbon black raw oil and solvent through separating the back, inferior light phase component obtains refined asphaltic bitumen and solvent after separating, the heavy phase component obtains binder pitch and solvent after separating, all reclaim solvent and all return repeated use;
Described solvent pairs is aromatic solvent and aliphatic solvent, aromatic solvent is toluene, dimethylbenzene, heavy benzol solvent oil, naphtalene oil, washing oil or heavy aromatics, aliphatic solvent is sherwood oil, aliphatic solvent oil, oil wax oil, kerosene or solar oil, and the mass ratio between aromatic solvent and the aliphatic solvent is controlled at (0.5～1.5): in 1 scope;
Mass ratio between described solvent pairs and the crude coal-tar asphalt is (0.6～1.4): 1.
According to the density distribution principle, controlling light phase component outflow mass ratio is 5～25%, and inferior light phase component flows out mass ratio 30～65%, and the heavy phase component stream goes out mass ratio 20～35%.
In actually operating, can select solvent for use according to resource situation, determine operating parameters.For example: the described aromatic solvent benzene solvent oil of attaching most importance to, described aliphatic solvent is a wax oil, the mass ratio of described heavy benzol solvent oil and wax oil is 1: 1, described solvent pairs and crude coal-tar asphalt are mixed the back by 0.65: 1 mass ratio inject extraction separator, controlling settlement separate temperature is 135 ℃, the control settling velocity is 126mm/h, extracting flocculating settling separates, according to the density distribution principle respectively from separator, in, light phase component mass ratio 5% is taken out in following different positions control, inferior light phase component mass ratio 65%, the heavy phase constituent mass is than 30%, three kinds of components are through rectifying separation, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures, after deviating from solvent, the yield that obtains carbon black raw oil is 10.4%, the refined asphaltic bitumen yield is 59.6%, the binder pitch yield is 30.0%.
Perhaps, the described aromatic solvent benzene solvent oil of attaching most importance to, described aliphatic solvent is a wax oil, the mass ratio of described heavy benzol solvent oil and wax oil is 1: 1, be mixed with solvent pairs, inject extraction separator after described solvent pairs and crude coal-tar asphalt pressed 0.8: 1 mixed of mass ratio, controlling settlement separate temperature is 135 ℃, the control settling velocity is 178mm/h, extracting flocculating settling separates, according to the density distribution principle, respectively from separator, in, light phase component mass ratio 6% is taken out in following different positions control, inferior light phase component mass ratio 63%, the heavy phase constituent mass is than 31%, each component removes solvent through rectifying separation, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures, deviate from solvent after, the yield that obtains carbon black raw oil is 9.9%, the refined asphaltic bitumen yield is 61.7%, the binder pitch yield is 28.4%.
Described aromatic solvent is a washing oil, described aliphatic solvent is a wax oil, the mass ratio of described washing oil and wax oil is 1.1: 1, described solvent pairs and crude coal-tar asphalt are mixed the back by 1.1: 1 mass ratio inject extraction separator, controlling settlement separate temperature is 135 ℃, the control settling velocity is 182mm/h, extracting flocculating settling separates, according to the density distribution principle, respectively from separator, in, light phase component mass ratio 7% is taken out in following different positions control, inferior light phase component mass ratio 67%, the heavy phase constituent mass is than 26%, three kinds of components that obtain are carried out rectifying separation respectively, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures, after deviating from solvent, the acquisition yield is 9.9% carbon black raw oil, yield is 62.2% refined asphaltic bitumen, yield is 27.9% binder pitch.
Described aromatic solvent is a washing oil, described aliphatic solvent is a wax oil, the mass ratio of described washing oil and wax oil is 0.9: 1, described rough coal tar viscid bitumen and solvent pairs are injected extraction separator by 1: 1.25 mass ratio mixing back, controlling settlement separate temperature is 135 ℃, the control settling velocity is 187mm/h, extracting flocculating settling separates, according to the density distribution principle respectively from separator, in, light phase component mass ratio 9% is taken out in following different positions control, middle phase component mass ratio 65%, the heavy phase constituent mass is than 26%, three kinds of components are through rectifying separation, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures.After deviating from solvent, the yield that obtains carbon black raw oil is 10.3%, the refined asphaltic bitumen yield is 61.0%, the binder pitch yield is 28.7%.
The main technique flow process of the new process of co-production of high-quality carbon black raw oil proposed by the invention, refined asphaltic bitumen and binder pitch is: crude coal-tar asphalt and solvent are mixed the back by a certain percentage inject extraction separator and extract flocculating settling and separate, take out light phase component, inferior light phase component and heavy phase component from the upper, middle and lower different positions of separator respectively according to the density distribution principle, respectively light phase component, inferior light phase component and heavy phase component are carried out rectifying separation.Light phase component obtains high-quality carbon black raw oil and solvent through rectifying separation, and inferior light phase component obtains refined asphaltic bitumen and solvent through rectifying separation, and the heavy phase component obtains binder pitch and solvent through rectifying separation.All recovered solvents all return repeated use.Gained high-quality carbon black raw oil product is a raw material of producing senior graphitized carbon black; The refined asphaltic bitumen product is the raw material of preparation needle coke and the raw material of preparation coal measures carbon fiber; The binder pitch product is the binding agent that preparation graphite product, carbon containing refractory use.
Selected material asphalt is the thick coal-tar heavy oil pitch of 25 ℃～40 ℃ of softening temperatures among the present invention.
In the sepn process of extraction flocculating settling, according to the density distribution principle, controlling light phase component output quality ratio is 5%～15%, and inferior light phase component output quality ratio is 30%～65%, and heavy phase component output quality is than 20%～35%.The double solvent extraction agent of selecting for use is aromatic solvent and aliphatic solvent, wait a kind of, or two or more mixture in them.Aliphatic solvent comprises: sherwood oil, aliphatic solvent oil, oil wax oil, kerosene, solar oil etc. are a kind of, or two or more mixture in them.Ratio control between the solvent pairs is in (0.5～1.5): 1 (preferred 0.6～1.1: 1) in the scope.Ratio between solvent pairs and the crude coal-tar asphalt is (0.6～1.5): 1.
The advantage of co-production of high-quality carbon black raw oil of the present invention, refined asphaltic bitumen and cakingagent pitch technology is: this is that a kind of energy consumption is low, cost is low, the coal-tar pitch complete processing of no waste discharge, high benefit, and has plurality of advantages such as simple to operate, safe and reliable.The present invention effectively makes up preparation high-quality coal measures carbon black raw oil, coal measures refined asphaltic bitumen and coal measures binder pitch technology, make each component group of crude coal-tar asphalt reasonably be separated and utilize, for the preparation of coal-tar pitch downstream high value added product provides high quality raw material.
Description of drawings
Fig. 1 is a production line structured flowchart of the present invention.
Embodiment
Below in conjunction with description of drawings the specific embodiment of the present invention.
As shown in Figure 1, the technology of co-production of high-quality carbon black raw oil of the present invention, refined asphaltic bitumen and binder pitch, comprise that crude coal-tar asphalt and solvent 2 are mixed back injection extraction separator 1 by a certain percentage to be separated, it is characterized in that described solvent is a solvent pairs, obtain high-quality carbon black raw oil, refined asphaltic bitumen and three kinds of products of binder pitch simultaneously, processing step is:
1) crude coal-tar asphalt and solvent pairs 2 are mixed back injection extraction separator 1 by a certain percentage, extracting flocculating settling separates, take out light phase component 3, inferior light phase component 4 and heavy phase component 12 from the upper, middle and lower different positions of separator respectively according to the density distribution principle
2) ratio between the control solvent pairs and the ratio between solvent pairs and the crude coal-tar asphalt,
3) will extract the flocculating settling temperature and be controlled in 70 ℃～160 ℃ scopes,
4) will extract flocculation settling velocity and be controlled in 50mm/h～250mm/h scope,
5) rectifying separation of light phase component 3, inferior light phase component 4 and heavy phase component 12, control rectifying tower 5,6,7 tower top temperatures are 270 ℃～310 ℃ under the normal pressure, the operating parameters that heavy phase rectifying tower side stream temperature is 285 ℃～320 ℃, light phase component obtains high-quality carbon black raw oil 9 and solvent 8 through separating the back, inferior light phase component obtains refined asphaltic bitumen 10 and solvent after separating, the heavy phase component obtains binder pitch 11 and solvent after separating, all reclaim solvent and all return repeated use
Described solvent pairs is aromatic solvent and aliphatic solvent, aromatic solvent is toluene, dimethylbenzene, heavy benzol solvent oil, naphtalene oil, washing oil or heavy aromatics, aliphatic solvent is sherwood oil, aliphatic solvent oil, oil wax oil, kerosene or solar oil, mass ratio between aromatic solvent and the aliphatic solvent is controlled at (0.5～1.5): in 1 scope
Mass ratio between described solvent pairs and the crude coal-tar asphalt is (0.6～1.4): 1.
According to the density distribution principle, controlling light phase component outflow mass ratio is 5～25%, and inferior light phase component flows out mass ratio 30～65%, and the heavy phase component stream goes out mass ratio 20～35%.
Embodiment 1
The described aromatic solvent benzene solvent oil of attaching most importance to, described aliphatic solvent is a wax oil, the mass ratio of described heavy benzol solvent oil and wax oil is 1: 1, described solvent pairs and crude coal-tar asphalt are mixed the back by 0.65: 1 mass ratio inject extraction separator, controlling settlement separate temperature is 135 ℃, the control settling velocity is 126mm/h, extracting flocculating settling separates, according to the density distribution principle respectively from separator, in, light phase component mass ratio 5t% is taken out in following different positions control, inferior light phase component mass ratio 65%, the heavy phase constituent mass is than 30%, three kinds of components are through rectifying separation, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures, after deviating from solvent, the yield that obtains carbon black raw oil is 10.4%, the refined asphaltic bitumen yield is 59.6%, the binder pitch yield is 30.0%.The performance index of product are seen attached list.
Embodiment 2
The described aromatic solvent benzene solvent oil of attaching most importance to, described aliphatic solvent is a wax oil, the mass ratio of described heavy benzol solvent oil and wax oil is 1: 1, be mixed with solvent pairs, inject extraction separator after described solvent pairs and crude coal-tar asphalt pressed 0.8: 1 mixed of mass ratio, controlling settlement separate temperature is 135 ℃, the control settling velocity is 178mm/h, extracting flocculating settling separates, according to the density distribution principle, respectively from separator, in, light phase component mass ratio 6% is taken out in following different positions control, inferior light phase component mass ratio 63%, the heavy phase constituent mass is than 31%, each component removes solvent through rectifying separation, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures, after deviating from solvent, the yield that obtains carbon black raw oil is 9.9%, the refined asphaltic bitumen yield is 61.7%, the binder pitch yield is 28.4%.The performance index of product are seen attached list.
Embodiment 3
Described aromatic solvent is a washing oil, described aliphatic solvent is a wax oil, the mass ratio of described washing oil and wax oil is 1.1: 1, described solvent pairs and crude coal-tar asphalt are mixed the back by 1.1: 1 mass ratio inject extraction separator, controlling settlement separate temperature is 135 ℃, the control settling velocity is 182mm/h, extract flocculation separation, according to the density distribution principle, respectively from separator, in, light phase component mass ratio 7% is taken out in following different positions control, inferior light phase component mass ratio 67%, the heavy phase constituent mass is than 26%, three kinds of components that obtain are carried out rectifying separation respectively, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures, after deviating from solvent, the acquisition yield is 9.9% carbon black raw oil, yield is 62.2% refined asphaltic bitumen, yield is 27.9% binder pitch.The performance index of product are seen attached list.
Embodiment 4
Described aromatic solvent is a wax oil, described aliphatic solvent is a wax oil, the mass ratio of described washing oil and wax oil is 0.9: 1, described solvent pairs and crude coal-tar asphalt are mixed the back by 1.25: 1 mass ratio inject extraction separator, controlling settlement separate temperature is 135 ℃, the control settling velocity is 187mm/h, extract flocculation separation, according to the density distribution principle respectively from separator, in, light phase component mass ratio 9% is taken out in following different positions control, middle phase component mass ratio 65%, the heavy phase constituent mass is than 26%, three kinds of components are through rectifying separation, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures.After deviating from solvent, the yield that obtains carbon black raw oil is 10.3%, the refined asphaltic bitumen yield is 61.0%, the binder pitch yield is 28.7%.The performance index of product are seen attached list.
Product performance index among four kinds of embodiment of subordinate list
Claims (6)
1. the technology of a co-production of high-quality carbon black raw oil, refined asphaltic bitumen and binder pitch comprises that crude coal-tar asphalt and solvent are mixed back injection extraction separator by a certain percentage to be separated, and it is characterized in that described solvent is a solvent pairs, and processing step is:
1) crude coal-tar asphalt and solvent pairs are mixed back injection extraction separator by a certain percentage, extracting flocculating settling separates, take out light phase component, inferior light phase component and heavy phase component from the upper, middle and lower different positions of separator respectively according to the density distribution principle
2) ratio between the control solvent pairs and the ratio between solvent pairs and the crude coal-tar asphalt,
3) will extract the flocculating settling temperature and be controlled in 70 ℃～160 ℃ scopes,
4) will extract flocculation settling velocity and be controlled in 50mm/h～250mm/h scope,
5) rectifying separation of light phase component, inferior light phase component and heavy phase component, normal pressure is controlled 270 ℃～310 ℃ of rectifying tower top temperature down, the operating parameters that heavy phase rectifying tower side stream temperature is 285 ℃～320 ℃, light phase component obtains high-quality carbon black raw oil and solvent through separating the back, inferior light phase component obtains refined asphaltic bitumen and solvent after separating, the heavy phase component obtains binder pitch and solvent after separating, all reclaim solvent and all return repeated use
Described solvent pairs is aromatic solvent and aliphatic solvent, aromatic solvent is toluene, dimethylbenzene, heavy benzol solvent oil, naphtalene oil, washing oil or heavy aromatics, aliphatic solvent is sherwood oil, aliphatic solvent oil, oil wax oil, kerosene or solar oil, mass ratio between aromatic solvent and the aliphatic solvent is controlled at 0.5～1.5: in 1 scope
Mass ratio between described solvent pairs and the crude coal-tar asphalt is 0.6～1.4: 1.
2. the technology of co-production of high-quality carbon black raw oil according to claim 1, refined asphaltic bitumen and binder pitch, it is characterized in that according to the density distribution principle, controlling light phase component outflow mass ratio is 5～25%, inferior light phase component flows out mass ratio 30～65%, and the heavy phase component stream goes out mass ratio 20～35%.
3. co-production of high-quality carbon black raw oil according to claim 1, the technology of refined asphaltic bitumen and binder pitch, it is characterized in that the described aromatic solvent benzene solvent oil of attaching most importance to, described aliphatic solvent is a wax oil, the mass ratio of described heavy benzol solvent oil and wax oil is 1: 1, described solvent pairs and crude coal-tar asphalt are injected extraction separator by 0.65: 1 mass ratio mixing back, controlling settlement separate temperature is 135 ℃, the control settling velocity is 126mm/h, extracting flocculating settling separates, according to the density distribution principle respectively from separator, in, light phase component mass ratio 5% is taken out in following different positions control, inferior light phase component mass ratio 65%, the heavy phase constituent mass is than 30%, three kinds of components are through rectifying separation, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures, after deviating from solvent, the yield that obtains carbon black raw oil is 10.4%, the refined asphaltic bitumen yield is 59.6%, the binder pitch yield is 30.0%.
4. co-production of high-quality carbon black raw oil according to claim 1, the technology of refined asphaltic bitumen and binder pitch, it is characterized in that the described aromatic solvent benzene solvent oil of attaching most importance to, described aliphatic solvent is a wax oil, the mass ratio of described heavy benzol solvent oil and wax oil is 1: 1, be mixed with solvent pairs, inject extraction separator after described solvent pairs and crude coal-tar asphalt pressed 0.8: 1 mixed of mass ratio, controlling settlement separate temperature is 135 ℃, the control settling velocity is 178mm/h, extracting flocculating settling separates, according to the density distribution principle, respectively from separator, in, light phase component mass ratio 6% is taken out in following different positions control, inferior light phase component mass ratio 63%, the heavy phase constituent mass is than 31%, each component removes solvent through rectifying separation, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures, after deviating from solvent, the yield that obtains carbon black raw oil is 9.9%, the refined asphaltic bitumen yield is 61.7%, the binder pitch yield is 28.4%.
5. co-production of high-quality carbon black raw oil according to claim 1, the technology of refined asphaltic bitumen and binder pitch, it is characterized in that described aromatic solvent is a washing oil, described aliphatic solvent is a wax oil, the mass ratio of described washing oil and wax oil is 1.1: 1, described solvent pairs and crude coal-tar asphalt are injected extraction separator by 1.1: 1 mass ratio mixing back, controlling settlement separate temperature is 135 ℃, the control settling velocity is 182mm/h, extracting flocculating settling separates, according to the density distribution principle, respectively from separator, in, light phase component mass ratio 7% is taken out in following different positions control, inferior light phase component mass ratio 67%, the heavy phase constituent mass is than 26%, three kinds of components that obtain are carried out rectifying separation respectively, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures, after deviating from solvent, the acquisition yield is 9.9% carbon black raw oil, yield is 62.2% refined asphaltic bitumen, yield is 27.9% binder pitch.
6. co-production of high-quality carbon black raw oil according to claim 1, the technology of refined asphaltic bitumen and binder pitch, it is characterized in that described aromatic solvent is a washing oil, described aliphatic solvent is a wax oil, the mass ratio of described washing oil and wax oil is 0.9: 1, described solvent pairs and crude coal-tar asphalt are injected extraction separator by 0.9: 1 mass ratio mixing back, controlling settlement separate temperature is 135 ℃, the control settling velocity is 187mm/h, extracting flocculating settling separates, according to the density distribution principle, respectively from separator, in, light phase component mass ratio 9% is taken out in following different positions control, inferior light phase component mass ratio 65%, the heavy phase constituent mass is than 26%, three kinds of components are through rectifying separation, control rectifying tower tower top temperature is 280 ℃ under the normal pressure, 295 ℃ of heavy phase rectifying tower side stream temperatures, after deviating from solvent, the yield that obtains carbon black raw oil is 10.3%, the refined asphaltic bitumen yield is 61.0%, the binder pitch yield is 28.7%.
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| CN101967388A (en) * | 2010-11-03 | 2011-02-09 | 攀钢集团钢铁钒钛股份有限公司 | Preparation method of impregnant asphalt |
| CN102311800A (en) * | 2011-08-29 | 2012-01-11 | 云南昆钢煤焦化有限公司 | Modification method of coal tar pitch needle coke oily by product |
| CN102329637A (en) * | 2011-08-29 | 2012-01-25 | 云南昆钢煤焦化有限公司 | Intensive production method of coal tar pitch needle coke |
| CN103215058A (en) * | 2013-05-02 | 2013-07-24 | 枣庄矿业集团煤化工研究院有限公司 | Method for extracting and separating light component from coal tar at low temperature |
| CN103710039A (en) * | 2013-11-28 | 2014-04-09 | 枣庄矿业集团煤化工研究院有限公司 | Technology for one-step production of maltha from coal tar |
| CN111925814A (en) * | 2020-07-22 | 2020-11-13 | 山东益大新材料股份有限公司 | Delayed coking system and method for producing coal-series and oil-series needle coke in time-sharing manner |
| CN115216324A (en) * | 2022-06-29 | 2022-10-21 | 鞍钢化学科技有限公司 | System and method for prolonging operation period of coal-based needle coke pretreatment settling tank |
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Cited By (10)
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| CN101967388A (en) * | 2010-11-03 | 2011-02-09 | 攀钢集团钢铁钒钛股份有限公司 | Preparation method of impregnant asphalt |
| CN102311800A (en) * | 2011-08-29 | 2012-01-11 | 云南昆钢煤焦化有限公司 | Modification method of coal tar pitch needle coke oily by product |
| CN102329637A (en) * | 2011-08-29 | 2012-01-25 | 云南昆钢煤焦化有限公司 | Intensive production method of coal tar pitch needle coke |
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| CN103215058A (en) * | 2013-05-02 | 2013-07-24 | 枣庄矿业集团煤化工研究院有限公司 | Method for extracting and separating light component from coal tar at low temperature |
| CN103710039A (en) * | 2013-11-28 | 2014-04-09 | 枣庄矿业集团煤化工研究院有限公司 | Technology for one-step production of maltha from coal tar |
| CN111925814A (en) * | 2020-07-22 | 2020-11-13 | 山东益大新材料股份有限公司 | Delayed coking system and method for producing coal-series and oil-series needle coke in time-sharing manner |
| CN115216324A (en) * | 2022-06-29 | 2022-10-21 | 鞍钢化学科技有限公司 | System and method for prolonging operation period of coal-based needle coke pretreatment settling tank |
| CN115216324B (en) * | 2022-06-29 | 2023-12-08 | 鞍钢化学科技有限公司 | System and method for prolonging operation period of coal-based needle coke pretreatment settling tank |
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