CN113604240A - Heavy oil continuous coking system and process thereof - Google Patents
Heavy oil continuous coking system and process thereof Download PDFInfo
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- CN113604240A CN113604240A CN202110937528.1A CN202110937528A CN113604240A CN 113604240 A CN113604240 A CN 113604240A CN 202110937528 A CN202110937528 A CN 202110937528A CN 113604240 A CN113604240 A CN 113604240A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
- C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
- C10B49/22—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/005—After-treatment of coke, e.g. calcination desulfurization
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- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Dispersion Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a heavy oil continuous coking system and a process thereof, belonging to the technical field of petroleum refining. The system comprises a coking tower and a decoking device which are communicated; a thermal coke-carrying agent for exchanging heat with the heavy oil is arranged in the coking tower; the decoking device comprises a hot mixing area and a decoking reaction area which are communicated from top to bottom, and the heavy oil polycondensation product/cold coke-carrying agent generated by the coking tower is transported to the hot mixing area and then transported to the decoking reaction area from the hot mixing area; the heavy oil polycondensation product and the reaction gas conveyed to the decoking reaction zone are subjected to decoking reaction, and the cold coke-carrying agent returns to the hot mixing zone and is heated by the generated gas generated in the decoking reaction zone to form the hot coke-carrying agent, and the hot coke-carrying agent returns to the coking tower. The invention uses fluidization technology, introduces a coke-carrying agent as a heat carrier and a petroleum coke attachment carrier of heat required by thermal destruction reaction, circularly supplies heat between a coking tower and a decoking device, completes gasification decoking regeneration and heat exchange in the decoking device, and has continuous and closed system.
Description
Technical Field
The invention relates to the technical field of petroleum refining, in particular to a heavy oil continuous coking system and a process thereof.
Background
The delayed coking technology is a kind of heavy oil thermal destruction processing technology, which is characterized by that the heavy oil (vacuum residuum, catalytic slurry oil, deoiled asphalt, etc.) is quickly heated to reaction temp. by means of heating furnace, then quickly transferred into coke tower, and the "delayed" thermal cracking and condensation reaction is implemented in the coke tower, so that the heavy oil can be converted into dry gas, liquefied petroleum gas, coked naphtha, coked diesel oil, coked wax oil and petroleum coke, etc..
The present delayed coking technology has the advantages of strong raw material adaptability, no catalyst poisoning, less investment, low operation cost, mature and reliable technology and the like, and can be widely applied to the thermal destruction and light processing of heavy oil. However, the key reaction section in the process of the delayed coking technology is intermittent switching operation, the production fluctuation of the device is large, and the labor intensity of workers is high; a large amount of petroleum coke is generated, the yield of high-sulfur coke is increased year by year and the high-sulfur coke is difficult to utilize; the pollution of waste gas, peculiar smell and dust in the processes of coke cooling, coke removing, coke storage, transportation and dehydration becomes a common problem to be improved urgently in the delayed coking process.
Disclosure of Invention
The invention is to solve the general problems of large production fluctuation, difficult utilization of high-sulfur coke and poor production environment existing in the delayed coking technology in the oil refining field at present, firstly, the technological process is sealed and continuous, a coke-carrying agent is introduced as a heat carrier and a coke-generating carrier, a coking tower and a decoking device are communicated through a coke conveying line, the continuous production is realized, and the production process is stable; secondly, the high-sulfur coke is gasified, the generated heat is used as the heat required by the coking reaction, the steam is generated as a byproduct, and the gasified gas can be used as clean fuel after being desulfurized, so that the problems of environmental pollution caused by intermittent switching production fluctuation and open production in the delayed coking technology, difficult access of the high-sulfur coke and the like are solved, and the continuous clean production is realized.
The technical scheme for solving the technical problems is as follows:
a heavy oil continuous coking system comprises a coking tower and a decoking device which are communicated; a thermal coke-carrying agent for exchanging heat with the heavy oil is arranged in the coking tower;
the decoking device comprises a hot mixing area and a decoking reaction area which are communicated from top to bottom, and the heavy oil polycondensation product/cold coke-carrying agent generated by the coking tower is transported to the hot mixing area and then transported to the decoking reaction area from the hot mixing area; the heavy oil polycondensation product and the reaction gas conveyed to the decoking reaction zone are subjected to decoking reaction, and the cold coke-carrying agent returns to the hot mixing zone and is heated by the generated gas generated in the decoking reaction zone to form the hot coke-carrying agent, and the hot coke-carrying agent returns to the coking tower.
Furthermore, the coking tower is provided with a heavy oil feeding hole, the top of the coking tower is provided with a light oil gas outlet, the bottom of the coking tower is provided with a heavy oil polycondensation product/cold coke-carrying agent discharging hole, and the heavy oil polycondensation product/cold coke-carrying agent discharging hole at the bottom of the coking tower is communicated with the hot mixing area through a cold coke-carrying agent line.
Furthermore, the top end of the hot mixing zone is provided with a generated gas outlet, the bottom end of the decoking reaction zone is provided with a reaction gas inlet, and the hot mixing zone and the decoking reaction zone are communicated through a to-be-decoking line for conveying the heavy oil polycondensation product/cold coke-carrying agent and a decoking return line for conveying the cold coke-carrying agent; the heat mixing zone is communicated with the coking tower through a heat coke-carrying agent line for conveying heat coke.
Furthermore, the bottom of the coking tower and the hot mixing area are also connected with a coke discharging line for removing coke blocks; preferably, the coke discharge line on the hot mixing zone is provided with an elutriator, and the elutriated gas generated by the elutriator is conveyed to the hot mixing zone through a return line.
Furthermore, a distribution plate is arranged at the outlet of the air inlet of the hot mixing area, and a distributor is also arranged at the bottom of the decoking reaction area.
Furthermore, the decoking reaction area comprises a gas cooling section and a decoking section which are communicated from top to bottom, a gas outlet at the top of the hot mixing area is communicated with a waste heat boiler to generate cold gas, and part of the cold gas is conveyed to a gas inlet of the hot mixing area through a supercharger to be mixed with the generated gas.
Further, the heat mixing area is communicated with the coking tower through a coke cleaning line for cleaning and anti-coking.
Further, the top end of the coking tower and the top of the hot mixing zone are also provided with cyclone separators.
The invention also provides a heavy oil continuous coking process, which comprises the following steps: heavy oil is subjected to cracking polycondensation reaction under the condition that a heat-carrying agent is used as a heat carrier to provide heat, a heavy oil polycondensation product of the heavy oil is loaded on the coke-carrying agent to carry out decoking reaction, heat generated by decoking heats a cold coke-carrying agent to form the heat coke-carrying agent, and the heat carrier is continuously reused.
Further, a heavy oil polycondensation product of the heavy oil is petroleum coke, and a polycondensation gas product of the heavy oil is light oil gas; preferably, the coke-carrying agent is coke particles or spent catalyst.
The invention has the following beneficial effects:
1. the invention uses fluidization technology, introduces a coke-carrying agent as a heat carrier and a petroleum coke attachment carrier of heat required by thermal destruction reaction, circularly supplies heat between a coking tower and a decoking device, completes gasification decoking regeneration and heat exchange in the decoking device, and has continuous and closed system.
2. The invention carries out closed continuous cyclic cyclization in the reaction and decoking processes, introduces a coke-carrying agent as a heat carrier and generates a coke carrier, and utilizes the solid fluidization and fluidization conveying technologies to carry out continuous closed circulation on the coke-carrying agent between a coking tower and a decoking device and between a gasification zone and a hot mixing zone of the decoking device, thereby forming a stable and continuous reaction and material and heat transfer system, realizing continuous production and having stable production process.
3. The invention gasifies the high-sulfur coke, generates heat for coking reaction, produces steam as a byproduct, and can clean fuel after the gasified gas is desulfurized, thereby solving the problems of intermittent switching production fluctuation in the delayed coking technology and environmental pollution caused by open production and realizing continuous clean production.
4. The invention directly gasifies the by-product petroleum coke with low value and difficult utilization, thereby avoiding a series of problems of periodic switching operation in the delayed coking process, namely stripping, steam blowing and cooling, water cooling, coke cutting, blowing, pressure testing and preheating of the high-temperature petroleum coke, such as complicated production operation, high labor intensity of workers, easy occurrence of safety accidents, large production fluctuation, high water and steam consumption, waste gas emission and pollution problems of a cold coke water and coke cutting water treatment system, and waste gas and dust pollution problems of an open coke cooling storage tank.
5. The technique is easy to process the gasification gas generated after petroleum coke gasification, can be used as clean fuel after conventional desulfurization, and solves the problems that high-sulfur petroleum coke is difficult to leave a factory and use.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a schematic diagram of the configuration of a heavy oil continuous coking system of the present invention;
fig. 2 is a schematic structural view of a decoker of the heavy oil continuous coking system of the present invention.
Wherein, in the figure: 100-a coking tower, 110-a cyclone separator, 200-a decoking device, 210-a heat mixing area, 220-a decoking reaction area, 221-a gas cooling section, 222-a decoking section, 230-a distribution plate and 240-a distributor.
Detailed Description
The principles and features of the present invention are described below in conjunction with the embodiments and the accompanying drawings, which are set forth by way of illustration only and are not intended to limit the scope of the invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
The invention relates to a heavy oil continuous coking process, which comprises the following steps: heavy oil is subjected to cracking polycondensation reaction under the condition that a heat-carrying agent is used as a heat carrier to provide heat, the heavy oil is fully contacted with the heat-carrying agent to absorb heat to perform heat exchange, heated heavy oil is gasified and subjected to cracking condensation reaction to generate heavy oil coke polycondensation product and light oil gas polycondensation gas product, the heat of the heat-carrying agent is released to become a cold coke-carrying agent which is used as a carrier, the petroleum coke is coalesced on the coke-carrying agent and is conveyed to a decoking unit to perform decoking reaction, the petroleum coke is subjected to gasification reaction with air and steam in the decoking reaction to generate gasified gas containing carbon monoxide, hydrogen and nitrogen, and the coke-carrying agent is decoked and regenerated. The generated gasified gas is high-temperature gas and has high heat, and the carrier cold coke-carrying agent is heated by the gasified gas generated by decoking to form the hot coke-carrying agent, so that the hot coke-carrying agent can return to the initial reaction stage to continuously provide heat for the heavy oil, and the continuous coking production of the heavy oil is realized by the recycling of the coke-carrying agent. In the application, the coke carrier is coke particles or a waste catalyst, and is used as a carrier of petroleum coke to only exchange heat with heavy oil without reaction.
The invention introduces a coke-carrying agent as a carrier of heat and petroleum coke, solid petroleum coke formed by heavy oil coking reaction is attached to the coke-carrying agent, the petroleum coke product attached to the coke-carrying agent is converted into gasification gas convenient to use by a gasification technology, the heat generated by gasification heats the coke-carrying agent by heat exchange, and the coke-carrying agent is continuously circulated in a closed manner between a coking tower and a decoking device, a gasification zone of the decoking device and a hot mixing zone by solid fluidization and fluidization conveying technologies to form a stable and continuous reaction and material and heat transfer system.
Referring to fig. 1 and fig. 2, the present embodiment provides a continuous heavy oil coking system, which includes a coking tower 100 and a decoking device 200 that are communicated, the coking tower 100 is used for heat exchange between heavy oil and a hot coke-carrying agent and pyrolysis condensation reaction of the heavy oil due to thermal gasification, the decoking device 200 is used for gasification reaction of petroleum coke generated from the heavy oil to generate gasification gas, the coke-carrying agent is decoked and regenerated, and the regenerated cold coke-carrying agent is heated to generate the hot coke-carrying agent.
The coking tower 100 is internally provided with a thermal coke-carrying agent for exchanging heat with heavy oil, in the invention, the coking tower 100 is an R101 fluidized bed layer, the R101 is internally provided with the thermal coke-carrying agent in circulating fluidization, and when the heat of the coke-carrying agent in the coking tower 100 is insufficient, the coke-carrying agent is heated by stripping steam and impact steam to supplement the heat exchanged between the coke-carrying agent and the heavy oil.
The coking tower 100 is provided with a heavy oil feeding hole, the top of the coking tower 100 is provided with a light oil gas outlet, the bottom of the coking tower 100 is provided with a heavy oil polycondensation product/cold coke-carrying agent discharging hole, the heavy oil polycondensation product/cold coke-carrying agent discharging hole at the bottom of the coking tower 100 is communicated with a hot mixing area 210 through a cold coke-carrying agent line, the top end of the coking tower 100 is provided with a cyclone 110, and the cyclone 110 is a primary cyclone.
Heavy oil enters the coking tower 100 from a heavy oil feed inlet to fully contact with a hot coke-carrying agent, is gasified by heating and undergoes cracking condensation reaction, the generated polycondensation gas product light oil gas ascends, coke-carrying agent particles carried in the oil gas are separated out by a cyclone separator 110 and fall back into the coking tower 100, and clean oil gas is discharged from a light oil gas outlet and enters a fractionation system to be further separated into different products; the generated petroleum coke of the heavy oil polycondensation product is agglomerated on a coke carrier, the heat coke carrier after heat exchange is changed into a cold coke carrier with the surface loaded with the petroleum coke, and the cold coke carrier descends to the bottom of the coking tower 100 and is conveyed to a hot mixing area 210 at the upper section of the decoking device 200 from a discharge port of the heavy oil polycondensation product/the cold coke carrier through a cold coke carrier line.
The decoking device 200 comprises a heat mixing zone 210 and a decoking reaction zone 220 which are communicated from top to bottom, wherein the heat mixing zone 210 is a heat exchange place and provides a heat transfer space between gasification gas and a coke-carrying agent; the decoking reaction zone 220 is a decoking place and provides a decoking gasification reaction space for a coke-carrying agent carrying petroleum coke.
The heavy oil polycondensation product/cold coke-carrying agent produced by the coker 100 is transported to the hot mixing zone 210 and then transported from the hot mixing zone 210 to the decoking reaction zone 220; after the heavy oil polycondensation product and the reaction gas conveyed to the decoking reaction zone 220 are subjected to decoking reaction, the cold coke-carrying agent returns to the hot mixing zone 210, and is heated into hot coke-carrying agent by the generated gas generated in the decoking reaction zone 220, and the hot coke-carrying agent returns to the coking tower 100. Specifically, the hot mixing zone 210 and the decoking reaction zone 220 are also communicated through a line to be decoked for conveying the heavy oil polycondensation product/cold coke-carrying agent and a decoking return line for conveying the cold coke-carrying agent; the heat-mixing zone 210 is in communication with the coke drum 100 through a hot coke carrier line for transporting hot coke.
The top end of the heat mixing area 210 is provided with a generated gas outlet, the bottom end of the decoking reaction area 220 is provided with a reaction gas inlet, the gas inlet of the heat mixing area 210 is provided with a distribution plate 230, the distribution plate 230 separates the heat mixing area 210 and the decoking reaction area 220, and the distribution plate 230 is used as a material flow channel. The distributor 240 is also arranged at the bottom of the decoking reaction zone 220, the cyclone 110 is also arranged at the top of the hot mixing zone 210, and the cyclone 110 is a two-stage cyclone 110.
Steam and air from a blower enter the decoking reaction zone 220 from a reaction gas inlet at the bottom end of the decoking reaction zone 220 through the distributor 240, and are subjected to gasification reaction with petroleum coke on a cold carrier in the decoking reaction zone 220 to generate gasification gas containing carbon monoxide, hydrogen and nitrogen, the coke-carrying agent is decoked and regenerated, the high-temperature gasification gas goes upwards through the distribution plate 230 and enters the upper-section hot mixing zone 210 of the decoking device 200, contacts with the coke-carrying agent for heat exchange, and after being cooled, the carried coke-carrying agent particles are separated out through the two-stage cyclone 110 and then enter a subsequent gas treatment system. The heated hot coke-carrier is circulated through a hot coke-carrier line into the coke drum 100 to provide heat for the reaction.
The coke discharging line for removing coke blocks is connected to the bottom of the coke drum 100 and the hot mixing zone 210, which is to maintain the heat balance of the system and to remove coke blocks formed by carbon deposition or metal sintering from the system, so as to ensure the good fluidization state of the system. The coke discharge line of the hot mixing zone 210 is provided with an elutriator, and the elutriated gas generated by the elutriator is delivered to the hot mixing zone 210 through a return line. The elutriator is also in communication with decoking, and periodically introduces a portion of the coke-carrying agent into the elutriator using the line to be decoked, and lifts the small particle coke-carrying agent back to the thermal mixing zone 210 using steam.
The hot mixing zone 210 is also communicated with the coking tower 100 through a coke cleaning line for cleaning and coking prevention, and the hot coke-carrying agent is conveyed to the top of the coking tower 100 through a coke cleaning line to clean the part of the cyclone separator 110 which is easy to coke, so as to prevent the cyclone separator 110 from being blocked due to coking.
The decoking reaction zone 220 comprises a gas cooling section 221 and a decoking section 222 which are communicated from top to bottom, the decoking section 222 at the lower end of the petroleum coke is used for decoking and gasifying, and generated gasification gas enters the gas cooling section 221 for cooling, so as to reduce the temperature of the gasification gas and prevent the gasification gas distribution plate 230 from being damaged due to the high temperature of the gasification gas. An air outlet at the top of the heat mixing area 210 is communicated with a waste heat boiler to generate cold air gas, and part of the cold air gas is conveyed to an air inlet of the heat mixing area 210 through a supercharger to be mixed with generated gas. And a part of cold gasified gas which leaves the decoking device 200 and passes through the waste heat boiler and is generated after steam is introduced to a circular pipe at the outer side of a gasified gas ascending channel by using medium-pressure steam in a pressurizing device, a plurality of nozzles are arranged along the inner periphery of the circular pipe, the cold gasified gas is sprayed into the circular pipe and is fully mixed with high-temperature gasified gas, and the gasified gas is cooled to a safe temperature range.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (10)
1. A heavy oil continuous coking system is characterized by comprising a coking tower and a decoking device which are communicated; a heat coke-carrying agent for exchanging heat with heavy oil is arranged in the coking tower;
the decoking device comprises a hot mixing area and a decoking reaction area which are communicated from top to bottom, and the heavy oil polycondensation product/cold coke-carrying agent generated by the coking tower is transported to the hot mixing area and then transported to the decoking reaction area from the hot mixing area; and carrying out a decoking reaction on the heavy oil polycondensation product and the reaction gas conveyed to the decoking reaction zone, returning the cold coke-carrying agent to the hot mixing zone, heating the cold coke-carrying agent by the generated gas generated in the decoking reaction zone to form a hot coke-carrying agent, and returning the hot coke-carrying agent to the coking tower.
2. The continuous heavy oil coking system of claim 1 in which the coking drum has a heavy oil feed inlet, the top of the coking drum has a light oil gas outlet, the bottom of the coking drum has a heavy oil polycondensation product/cold coke carrier discharge outlet, and the heavy oil polycondensation product/cold coke carrier discharge outlet at the bottom of the coking drum communicates with the hot mixing zone through a cold coke carrier line.
3. The heavy oil continuous coking system according to claim 1, characterized in that the top end of the hot mixing zone is provided with a generated gas outlet, the decoking reaction zone is provided with a reaction gas inlet, and the hot mixing zone and the decoking reaction zone are also communicated through a to-be-decoking line for conveying heavy oil polycondensation products/cold coke carriers and a decoking return line for conveying cold coke carriers; the hot mixing zone is communicated with the coking tower through a hot coke-carrying agent line for conveying hot coke.
4. The heavy oil continuous coking system of claim 1, where a coke discharge line for removing coke pieces is also connected to the bottom of the coking column and the hot mix zone; preferably, the coke discharge line on the hot mixing zone is provided with an elutriator, and the elutriated gas generated by the elutriator is conveyed to the hot mixing zone through a return line.
5. The continuous heavy oil coking system according to claim 1, characterized in that a distribution plate is arranged at the gas inlet of the heat mixing zone, and a distributor is further arranged at the bottom of the decoking reaction zone.
6. The heavy oil continuous coking system according to any one of claims 1 to 5, characterized in that the decoking reaction zone comprises a gas cooling section and a decoking section which are communicated from top to bottom, a gas outlet at the top of the hot mixing zone is communicated with a waste heat boiler to generate cold gas, and part of the cold gas is conveyed to a gas inlet of the hot mixing zone through a supercharger to be mixed with the generated gas.
7. The continuous heavy oil coking system of claim 6 in which the hot mixing zone is also in communication with the coking drum through a coke cleaning line for cleaning coke.
8. The continuous heavy oil coking system of claim 6, where the top of the coking drum and the top of the thermal mixing zone are further provided with cyclones.
9. A heavy oil continuous coking process is characterized by comprising the following steps: heavy oil is subjected to cracking polycondensation reaction under the condition that a heat-carrying agent is used as a heat carrier to provide heat, a heavy oil polycondensation product of the heavy oil is loaded on the coke-carrying agent to carry out decoking reaction, heat generated by decoking heats a cold coke-carrying agent to form the heat coke-carrying agent, and the heat carrier is continuously reused.
10. The continuous heavy oil coking process of claim 9 where the heavy oil polycondensation product of the heavy oil is petroleum coke and the heavy oil polycondensation gas product is a light oil gas; preferably, the coke-carrying agent is coke particles or spent catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202110937528.1A CN113604240A (en) | 2021-08-16 | 2021-08-16 | Heavy oil continuous coking system and process thereof |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202110937528.1A CN113604240A (en) | 2021-08-16 | 2021-08-16 | Heavy oil continuous coking system and process thereof |
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