CN114437771B - Process method for regenerating asphalt activator by utilizing refined oil slurry - Google Patents
Process method for regenerating asphalt activator by utilizing refined oil slurry Download PDFInfo
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- CN114437771B CN114437771B CN202011117359.9A CN202011117359A CN114437771B CN 114437771 B CN114437771 B CN 114437771B CN 202011117359 A CN202011117359 A CN 202011117359A CN 114437771 B CN114437771 B CN 114437771B
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- 239000010426 asphalt Substances 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 33
- 230000008569 process Effects 0.000 title claims abstract description 25
- 239000002002 slurry Substances 0.000 title claims abstract description 24
- 239000012190 activator Substances 0.000 title claims abstract description 23
- 230000001172 regenerating effect Effects 0.000 title claims abstract description 11
- 238000000926 separation method Methods 0.000 claims abstract description 31
- 239000000463 material Substances 0.000 claims abstract description 18
- 238000000605 extraction Methods 0.000 claims abstract description 14
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 11
- 239000012528 membrane Substances 0.000 claims abstract description 11
- 239000000203 mixture Substances 0.000 claims abstract description 10
- 238000010438 heat treatment Methods 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 5
- 230000001276 controlling effect Effects 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 238000006555 catalytic reaction Methods 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 3
- 239000000047 product Substances 0.000 abstract description 24
- 239000002699 waste material Substances 0.000 abstract description 16
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 238000004064 recycling Methods 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 abstract description 4
- 238000005485 electric heating Methods 0.000 abstract description 3
- 239000006227 byproduct Substances 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 31
- 238000004231 fluid catalytic cracking Methods 0.000 description 24
- 125000003118 aryl group Chemical group 0.000 description 5
- 230000009286 beneficial effect Effects 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 238000004939 coking Methods 0.000 description 3
- 238000005259 measurement Methods 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 230000004913 activation Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000003801 milling Methods 0.000 description 2
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 206010035148 Plague Diseases 0.000 description 1
- 241000607479 Yersinia pestis Species 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000011384 asphalt concrete Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000010705 motor oil Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
Classifications
-
- 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
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- 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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
Abstract
The invention discloses a process method for regenerating an asphalt activator by utilizing refined oil slurry. The invention adjusts the feed composition of FCC flow, the feed is full hydrogenation residual oil of residual oil hydrogenation device, and adjusts the temperature of the sensitive plate of the fractionating tower in FCC, and the fractionating tower product is sent to the membrane filter. And feeding the filtered material into an electric heating furnace, and stably controlling the temperature of the material. And feeding the heated material into a vacuum separation tower, wherein the vacuum separation tower maintains a certain vacuum degree. Separating tower extraction is divided into tower top extraction, side line extraction and tower bottom extraction. The top of the tower is recovered to the FCC unit, the side recovery is recovered to the residual oil hydrogenation unit, and the bottom recovery is recovered to the asphalt activator product. The invention solves the problem of higher cost of recycling the existing waste asphalt, and simultaneously solves the problem of utilization of byproduct slurry oil of the FCC process, and the production process is simple and feasible.
Description
Technical Field
The invention belongs to the technical field of asphalt activator production, and in particular relates to a novel process method for producing an asphalt activator by using refined oil slurry as a raw material.
Background
Asphalt concrete pavement is exposed to outdoor environment for a long time, and rutting, cracking, potholes and other damages can occur, so that the pavement performance of the asphalt pavement is deteriorated, and the driving safety is influenced. Currently, for severely damaged pavement, the pavement needs to be rebuilt by milling and then paving, and a great amount of waste asphalt mixture is generated by the maintenance method. If the waste asphalt mixture is not reasonably disposed and is disposed in a discarding way, the environment is polluted, and the waste asphalt mixture is extremely resource waste. Therefore, how to recycle the waste road milling materials is a technology which needs to be solved urgently.
The asphalt activator can be used for repairing aged asphalt of aged asphalt pavement. The activator is mixed with the aged asphalt, so that the asphalt pavement can be repaired, and the asphalt pavement can continuously reach the use standard.
The activation and recycling of the waste asphalt can effectively treat the waste asphalt, solve the problem of environmental pollution caused by random discarding of the waste asphalt mixture, reduce the amount of new asphalt and new stone due to repeated use of the waste asphalt and the waste stone, be beneficial to environmental protection, save a large amount of new materials and reduce the construction cost.
At present, the activation and recycling of the waste asphalt generally comprises the steps of blending the soft components rich in the aromatic components into the waste asphalt according to a certain proportion, but the problems of high manufacturing cost exist, so that the recycling of the waste asphalt is limited. In the related art, there is also a problem that the used engine oil is recycled for waste use, but the long-term stability is poor.
The problem of slurry utilization in the FCC process of a refinery is always a major problem that plagues the production arrangement of the enterprise. In the FCC process (Fluid catalytic cracking fluid catalytic cracking) as disclosed in chinese patent CN 110628457A, the utilization of slurry oil is only beneficial to the extraction of light slurry oil by adding a pretreatment device, but the heavy slurry oil component has no subsequent treatment process, resulting in insufficient utilization of the heavy slurry oil component. Typically, refineries are self-digesting by coker blending or take the form of take-away. However, the coking blending coking rate is high, and at present, a plurality of sets of delayed coking devices have unplanned shutdown because of processing catalytic slurry oil; even enterprises have the problem of leaking fire caused by processing catalytic slurry oil. As for take-out, the price is low, and no profit can be said. By analysis, the slurry oil product produced in the FCC process flow consists of saturated components, aromatic components, colloid and the like, wherein the saturated components are generally less than 20%, the slurry oil product is mainly rich in aromatic components and colloid, and the content of polycyclic aromatic hydrocarbon exceeds 50%. Polycyclic aromatic hydrocarbons are the active ingredient in the preparation of asphalt activators. For economic and rationality, the utilization of the refined oil slurry product in the production of asphalt activator and other high-benefit products is more beneficial to the application prospect.
Disclosure of Invention
The invention provides a process method for regenerating an asphalt activator by utilizing refined oil slurry, which solves the problem of higher cost of recycling the existing waste asphalt, and simultaneously solves the problem of utilization of byproduct oil slurry in an FCC (fluid catalytic cracking) process, and the production process is simple and feasible.
The invention adjusts the feed composition of FCC flow, the feed is full hydrogenation residual oil of residual oil hydrogenation device, and adjusts the temperature of the sensitive plate of the fractionating tower in FCC, and the fractionating tower product is sent to the membrane filter. And feeding the filtered material into an electric heating furnace, and stably controlling the temperature of the material. And feeding the heated material into a vacuum separation tower, wherein the vacuum separation tower maintains a certain vacuum degree. Separating tower extraction is divided into tower top extraction, side line extraction and tower bottom extraction. The top of the tower is recovered to the FCC unit, the side recovery is recovered to the residual oil hydrogenation unit, and the bottom recovery is recovered to the asphalt activator product.
The following is a specific technical scheme of the invention.
The invention provides a process method for regenerating an asphalt activator by utilizing refined oil slurry, which comprises the following steps:
1) The raw material of FCC is hydrogenated residual oil produced by an upstream residual oil hydrogenation device, the feed composition of FCC flow is regulated, hydrogenated tail oil and unhydrogenated residual oil can not be mixed, namely, the feed is 100% hydrogenated residual oil, catalytic reaction is carried out, the reaction temperature is 510 ℃, the reaction pressure is 0.25MPa, the reacted oil gas enters an FCC fractionating tower, and the temperature of a sensitive plate of the fractionating tower is controlled between 335 and 345 ℃;
2) Feeding the bottom product of the FCC fractionating tower into a membrane filter, and controlling the filtering precision to be 5 mu m;
3) Introducing the filtered material into a heating furnace for heating, and keeping the heating temperature at 365-375 ℃;
4) Feeding the heated material into a vacuum separation tower, wherein the pressure at the top of the tower is kept between 0.02 and 0.04MPa, the temperature at the top of the tower is kept between 150 and 170 ℃, and the temperature at the bottom of the tower is kept between 370 and 385 ℃; the density of the bottom product of the vacuum separation tower is kept within the range of 1.10-1.15 g/cm < 3 >;
the vacuum separation tower is a float valve tower, the aperture ratio of the float valve is 1.95%, 12 layers of tower plates are arranged in total, the feeding position is the 7 th layer of tower plates from top to bottom, the 3 rd layer of tower plates are extracted from the side line of the vacuum separation tower, then part of heat is removed, the extracted line is divided into two paths, one path returns to the top of the vacuum separation tower, the reflux temperature is controlled at 95-105 ℃, the other path goes to the residual oil hydrogenation device, and the extraction rate is controlled at 5-9%.
Further, the membrane filter in the step 2) is a flexible membrane filter.
Further, the heating temperature in the step 3) is maintained at 368-372 ℃.
Further, the pressure of the top of the vacuum separation tower in the step 4) is 0.025-0.03 MPa, the temperature of the top of the tower is kept at 155-165 ℃, and the temperature of the bottom of the tower is kept at 375-380 ℃.
Further, the side reflux temperature of the vacuum separation tower in the step 4) is controlled to be 98-100 ℃, and the side extraction rate is controlled to be 7-8%.
Further, the density of the bottom product of the vacuum separation tower in the step 4) is kept in the range of 1.13-1.14 g/cm 3.
Compared with the prior art, the invention has the beneficial effects that:
in the technical scheme, the upstream FCC process feed raw material is firstly regulated, and the temperature of a sensitive plate of an FCC fractionating tower is regulated, so that the aromatic component content of the separated material is ensured. And sending the fractionating tower product into a membrane filter to remove catalyst powder. And feeding the filtered material into an electric heating furnace, and stably controlling the temperature of the material. The heated material enters a vacuum separation tower, and the temperature and the extraction of the separation tower are controlled, so that the composition of a tower bottom product is ensured to be an asphalt activator product.
By combining the FCC unit with the separation unit, the asphalt activator product can be obtained under the condition without large-scale equipment reconstruction and building. Avoiding the complex blending method of soft components rich in aromatic components commonly used in the prior art. Therefore, the construction cost is lower, the operation parameters required to be controlled are fewer, the process is simple, the occupied area of the device is small, the cheap and rich FCC tailings are reasonably utilized, the pollution to the environment is reduced, and the economic benefit is improved.
Drawings
FIG. 1 is a process flow of the present invention for regenerating asphalt activator using refined slurry;
in the figure, the 1-FCC process feed line, 2-FCC reactor, 3-FCC fractionator, 4-separation system feed line, 5-filter, 6-heater, 7-vacuum separator, 8-vacuum separator bottoms line, 9-vacuum separator overhead lights, 10-vacuum separator overhead recycle, and 11-vacuum separator side draw.
Detailed Description
The present invention will be described in detail with reference to specific examples. The following examples will assist those skilled in the art in further understanding the present invention, but are not intended to limit the invention in any way. It should be noted that several modifications and improvements can be made by those skilled in the art without departing from the inventive concept. These are all within the scope of the present invention.
Examples 1 to 10
As shown in FIG. 1, the process flow of the invention for regenerating asphalt activator by using refined oil slurry.
1) The raw material of FCC is hydrogenated residual oil produced by an upstream residual oil hydrogenation device, the feed composition of FCC flow is adjusted, hydrogenated tail oil and unhydrogenated residual oil can not be mixed, namely, the feed is 100% hydrogenated residual oil, catalytic reaction is carried out, the reaction temperature is 510 ℃, the reaction pressure is 0.25MPa, the reacted oil gas enters an FCC fractionating tower, and the temperature control of a sensitive plate of the FCC fractionating tower is specifically shown in table 1;
2) Feeding the bottom product of the FCC fractionating tower into a membrane filter, wherein the filtering precision is controlled to be 5 mu m, and the membrane filter is flexible;
3) Introducing the filtered material into a heating furnace for heating, wherein the heating temperature is controlled specifically as shown in table 2;
4) Feeding the heated material into a vacuum separation tower, wherein the feeding amount of the vacuum separation tower is 25t/h, the feeding temperature is 340 ℃, the steam stripping amount in the tower is 1200kg/h, and the separation condition in the vacuum separation tower is controlled specifically as shown in table 3;
5) The bottom of the vacuum separation tower is produced into a required product, the basic property of the product can be used as an asphalt activator, and the yield and the product viscosity ratio of the obtained heavy component product are shown in Table 4.
TABLE 1 separation conditions in FCC fractionators of various embodiments
| Temperature of fractionating tower sensitive plate (DEG C) | |
| Example 1 | 335 |
| Example 2 | 335 |
| Example 3 | 337 |
| Example 4 | 339 |
| Example 5 | 340 |
| Example 6 | 341 |
| Example 7 | 342 |
| Example 8 | 343 |
| Example 9 | 344 |
| Example 10 | 345 |
TABLE 2 heater temperatures for various embodiments
| Heater temperature (DEG C) | |
| Example 1 | 365 |
| Example 2 | 368 |
| Example 3 | 369 |
| Example 4 | 370 |
| Example 5 | 371 |
| Example 6 | 371 |
| Example 7 | 372 |
| Example 8 | 372 |
| Example 9 | 373 |
| Example 10 | 375 |
TABLE 3 separation conditions in the separation columns of the examples
TABLE 4 yield of the heavy fraction products and product viscosity ratio obtained in each example
| Yield of heavy component (%) | Viscosity ratio (less than or equal to 3) | |
| Example 1 | 94.5 | 3.0 |
| Example 2 | 94.1 | 2.9 |
| Example 3 | 93.6 | 2.7 |
| Example 4 | 91.5 | 2.2 |
| Example 5 | 92.8 | 2.6 |
| Example 6 | 92.2 | 2.5 |
| Example 7 | 92.1 | 2.8 |
| Example 8 | 92.4 | 2.7 |
| Example 9 | 89.7 | 2.0 |
| Example 10 | 88.6 | 2.1 |
From examples 1 to 10, 3 products were selected for performance measurement, and specific measurement results are shown in Table 5. As can be seen from the test results in Table 5, the performance indexes of the produced asphalt activator completely meet the actual use requirements and can be used in the aged asphalt thermal regeneration process.
TABLE 5 measurement of product Properties of part of examples
While the preferred embodiments of the present invention have been illustrated and described, the present invention is not limited to the embodiments, and various equivalent modifications and substitutions can be made by one skilled in the art without departing from the spirit of the present invention, and these equivalent modifications and substitutions are intended to be included in the scope of the present invention as defined in the appended claims.
Claims (4)
1. A process method for regenerating an asphalt activator by utilizing refined oil slurry comprises the following steps:
1) The raw material of FCC is hydrogenated residual oil produced by an upstream residual oil hydrogenation device, the feed composition of FCC flow is regulated, hydrogenated tail oil and unhydrogenated residual oil can not be mixed, namely, the feed is 100% hydrogenated residual oil, catalytic reaction is carried out, the reaction temperature is 510 ℃, the reaction pressure is 0.25MPa, the reacted oil gas enters an FCC fractionating tower, and the temperature of a sensitive plate of the fractionating tower is controlled between 335 and 345 ℃;
2) Feeding the bottom product of the FCC fractionating tower into a membrane filter, and controlling the filtering precision to be 5 mu m; wherein the membrane filter is a flexible membrane filter;
3) Introducing the filtered material into a heating furnace for heating, and keeping the heating temperature at 365-375 ℃;
4) Feeding the heated material into a vacuum separation tower, wherein the pressure at the top of the tower is kept between 0.025 and 0.03MPa, the temperature at the top of the tower is kept between 155 and 165 ℃, and the temperature at the bottom of the tower is kept between 375 and 380 ℃; the density of the bottom product of the vacuum separation tower is kept within the range of 1.10-1.15 g/cm < 3 >; the vacuum separation tower is a float valve tower, the aperture ratio of the float valve is 1.95%, 12 layers of tower plates are arranged in total, the feeding position is the 7 th layer of tower plates from top to bottom, the 3 rd layer of tower plates are extracted from the side line of the vacuum separation tower, then part of heat is removed, the extracted line is divided into two paths, one path returns to the top of the vacuum separation tower, the reflux temperature is controlled at 95-105 ℃, the other path goes to the residual oil hydrogenation device, and the extraction rate is controlled at 5-9%.
2. The process for regenerating asphalt activator by utilizing refined oil slurry according to claim 1, wherein the process comprises the following steps: the heating temperature in the step 3) is kept at 368-372 ℃.
3. The process for regenerating asphalt activator by utilizing refined oil slurry according to claim 1, wherein the process comprises the following steps: the side reflux temperature of the vacuum separation tower in the step 4) is controlled to be 98-100 ℃, and the side extraction rate is controlled to be 7-8%.
4. The process for regenerating asphalt activator by utilizing refined oil slurry according to claim 1, wherein the process comprises the following steps: the density of the bottom product of the vacuum separation tower in the step 4) is kept in the range of 1.13-1.14 g/cm 3.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1546613A (en) * | 2003-12-09 | 2004-11-17 | 中国石油化工集团公司 | Combined process for heavy oil upgrading |
| CN101668831A (en) * | 2007-04-24 | 2010-03-10 | 琳德北美股份有限公司 | Flash processing of asphaltic residual oil |
| CN103254936A (en) * | 2012-02-16 | 2013-08-21 | 中国石油天然气股份有限公司 | Combined process of hydrotreatment-catalytic cracking for residuum |
| CN104105780A (en) * | 2011-09-30 | 2014-10-15 | Meg能源公司 | Solvent de-asphalting with cyclonic separation |
| CA3059214A1 (en) * | 2017-04-07 | 2018-10-11 | Exxonmobil Research And Engineering Company | Hydroprocessing of catalytic slurry oil and coker bottoms |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006241181A (en) * | 2005-02-28 | 2006-09-14 | Sekiyu Combinat Kodo Togo Unei Gijutsu Kenkyu Kumiai | Method for preventing fouling of heat exchanger for cooling residual oil of hydrogenation-desulfurizing decomposition process |
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2020
- 2020-10-19 CN CN202011117359.9A patent/CN114437771B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1546613A (en) * | 2003-12-09 | 2004-11-17 | 中国石油化工集团公司 | Combined process for heavy oil upgrading |
| CN101668831A (en) * | 2007-04-24 | 2010-03-10 | 琳德北美股份有限公司 | Flash processing of asphaltic residual oil |
| CN104105780A (en) * | 2011-09-30 | 2014-10-15 | Meg能源公司 | Solvent de-asphalting with cyclonic separation |
| CN103254936A (en) * | 2012-02-16 | 2013-08-21 | 中国石油天然气股份有限公司 | Combined process of hydrotreatment-catalytic cracking for residuum |
| CA3059214A1 (en) * | 2017-04-07 | 2018-10-11 | Exxonmobil Research And Engineering Company | Hydroprocessing of catalytic slurry oil and coker bottoms |
Non-Patent Citations (1)
| Title |
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| "热拌用沥青再生剂的工业试生产";王俊华;石油化工技术与经济;第34卷(第3期);说明书第48-49页1 油浆减压深拔工艺简介及改造 * |
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