CN117603723A - Two-step catalytic cracking distillation wax removal process flow - Google Patents

Abstract

The invention discloses a two-step catalytic cracking distillation wax removal process flow. The two-step catalytic cracking distillation paraffin removal process flow solves the problems that plastics and other paraffin-prone raw materials are cracked by adopting a step-by-step treatment method, wax oil is distilled and purified further, the technical problems of cracking the plastics and other paraffin-prone raw materials are solved, the problem that most intermittent cracking equipment basically causes the situation that high-temperature oil gas is condensed into waxy oil in an oil storage tank after precooling and liquefying in a condenser when cracking the plastics, and the waxy oil loses fluidity after being condensed in the oil storage tank at normal temperature, flexible transfer work cannot be carried out, and great difficulty is brought to the next step of treatment and transportation work is solved.

Description

A two-step catalytic cracking distillation wax removal process flow

Technical field

The invention relates to the technical field of plastic processing technology, specifically a two-step catalytic cracking distillation wax removal process flow.

Background technique

Most of the intermittent cracking equipment currently on the market will basically cause high-temperature oil and gas to be pre-cooled and liquefied in the condenser when cracking plastics, and finally condense into waxy oil in the oil storage tank. The waxy oil at room temperature will be stored in the oil storage tank. After condensation and loss of fluidity in the tank, transfer work cannot be carried out, which brings great difficulties to the next step of processing and transportation.

Contents of the invention

(1) Technical problems solved

In view of the shortcomings of the existing technology, the present invention provides a two-step catalytic cracking distillation wax removal process, which solves the problem that high-temperature oil and gas will basically occur when cracking plastics in intermittent cracking equipment. After being precooled and liquefied in the condenser, it is finally stored in the storage tank. Waxy oil condenses in the oil tank. After the waxy oil loses fluidity after condensation in the oil storage tank at room temperature, it cannot be transferred, which hinders the next step of processing.

(2) Technical solutions

In order to achieve the above object, the present invention provides the following technical solution: a two-step catalytic cracking distillation wax removal process flow, including the following steps:

S1. First put plastic and other raw materials into the reactor R-001, close the furnace door and then turn on the burner U-001 to start heating. As the temperature of the raw materials increases, it begins to crack;

S2. The heating method adopts F-001 hot air heating in the combustion chamber. The material is returned to the upper layer of the combustion chamber through the 300-CS-PG-032 flue gas recycling pipeline and the high-temperature flue gas is mixed in the tail space of the combustion chamber and reused for reactor heating. , so that the reactor is heated more evenly;

S3. When the temperature of the plastic reaches the cracking temperature, high-temperature oil and gas will be generated from the reactor and pass through the first slag discharger M-001 to reach the catalytic tower T-001 or the steam drum T-002 (can be selected according to the wax deposition of the material) Whether to use direct catalytic process or choose to collect wax oil first, open or close the corresponding catalytic tower or drum valve) After catalysis or buffering, it reaches the condenser through 200-CS-FG-200 or 200-CS-FG-009 E-001, after condensation and liquefaction, is collected into the oil storage tank TK-001;

S4. The non-condensable combustible gas passes from the oil storage tank through the condenser and is divided into two lines through the 65-CS-FG-011 pipeline. One line passes through 65-CS-FG-012 to the vacuum tank TK-003, and then passes through 65-CS after being buffered. -FG-013 pipeline reaches the vacuum pump P-003, and after being extracted by the vacuum pump, it reaches the water vapor separation tank T-004 through 65-CS-FG-014. (During the working process of the vacuum pump, the water in the water vapor separation tank is automatically extracted through 10-CS-CWS -039 pipeline circulation), reaches the water seal T-005 through 65-CS-FG-015, and is further washed by the water seal and then reaches the combustion chamber through 50-CS-FG-016. The burner burns to provide a heat source for heating the reactor. The pipeline is called the negative pressure pipeline, which can effectively guide the high-temperature oil and gas in the reactor through the condenser. The other pipeline directly reaches the water seal from the 65-CS-FG-033 pipeline without going through the vacuum system. The water seal is further washed with water for 50 seconds. -CS-FG-016 reaches the combustion chamber burner and burns to provide a heat source for the reactor to heat up. This path is a normal pressure pipeline. The oil and gas need to pass through the condenser through its own pressure. The two-path design can be switched for materials with different oil yield rates;

S5. Air distribution system for non-condensable combustible gas. Combustible gas combustion requires air distribution. Blower B-001 absorbs air from the external environment and reaches air heat exchanger E-002 through the 125-CS-AIR-031 pipeline. After heat exchange, the hot air passes through the 125-CS-AIR-032 pipeline and reaches the combustion chamber burner through 32-CS-AIR-033 and 32-CS-AIR-034 to provide air distribution for combustible gas combustion;

S6. The catalytic section of the catalytic tower needs to be heated during the working process to keep the catalyst active. When heating, the high-temperature flue gas generated by the furnace heating is used. The high-temperature flue gas passes from the furnace to the high-temperature induced draft fan B-002 through 300-CS-PG-001. It is transported to the catalytic section of the catalytic tower to maintain the temperature of the catalyst. After exiting the catalytic tower, it reaches the air heat exchanger through 300-CS-PG-004/005, and then passes through 300-CS-PG-006 to the air-to-water heat exchanger E-003. 300-CS-PG-007 pipeline to the exhaust gas treatment system, and the other high-temperature flue gas without passing through the catalytic tower passes from the furnace through 300-CS-PG-001 and is transported by high-temperature induced draft fan B-002 to 300-CS-PG-003/ The 005 pipeline reaches the air heat exchanger from 300-CS-PG-006 to the air-water heat exchanger E-003 and finally reaches the exhaust gas treatment system through the 300-CS-PG-007 pipeline;

S7. The pressure relief system of the catalytic tower and steam drum. When the pressure of the system is too high, automatic emergency pressure relief is required. The catalytic tower and steam drum are connected in parallel through the 100-CS-FG-030 pipeline and the gas pressure is reduced through the automatic pressure relief valve. Released into the 200-CS-FG-009 pipeline;

S8. Slag discharging system. When the material is cracked and the temperature of the main furnace system drops to 80 degrees, slag discharging can begin. The specific operation is to switch the rotation direction of the reactor, and the slag will be transported to the slag discharging machine M through the internal lifting plate of the reactor. -001, through the 300-CS-PS-017 pipeline to the water-cooled slag extractor M-002, and finally discharged out of the furnace through the 300-CS-PS-018 pipeline;

S9. The heating system of the oil storage tank. When the oil in the oil storage tank condenses into wax at room temperature and loses fluidity, the heating coil at the bottom of the oil tank is used to introduce high-temperature steam to melt the wax oil; thereby restoring fluidity. Specifically, high-temperature water vapor is generated through the steam boiler F-002, and is transported to the internal coil of the oil storage tank through the 40-CS-LS-038 pipeline. The wax oil in the oil storage tank is preheated and begins to melt, and the steam after heat exchange It is collected through the hydrophobic collection tank TK-002 and finally returned to the steam boiler through the 40-CS-LS-037 pipeline for reuse;

S10. System circulating water cooling system, the first air-water heat exchanger pipeline is routed from pump P-001 through 50-CS-CWS-027 pipeline to air-water heat exchanger E-003 and then through 50-CS-CWS-028 /029 pipeline returns to the cooling tower to cool down and finally returns to the pool. The second routing pump P-001 passes through 50-CS-CWS-021 to reach the water-cooling jacket of the TK-001 oil storage tank and then passes through 50-CS-CWS-024 Finally, it reaches the condenser E-001 and returns to the cooling tower through the 50-CS-CWS-025/023/029 pipeline to cool down and finally returns to the pool. The third routing pump P-001 arrives respectively through the 50-CS-CWS-022. The water-cooled slag extractor M-002 and condenser E-001 return to the cooling tower through the 50-CS-CWS-023/029 pipeline for cooling and finally return to the pool;

The cracked oil in S11.TK-001 reaches the distillation kettle R-002 through the oil pump P-002 and the 50-CS-OIL-035 pipeline;

S12. After the raw materials in the distillation kettle are filled, close the incoming pipeline and turn on the burner U-001 to start heating the distillation kettle. When the raw material temperature reaches 180 degrees, the high-temperature oil and gas generated by the distillation kettle will pass through the distillation tower R-003 and then pass through the pipeline. 200-CS-FG-111/112 to the condenser E-001, and the light fraction after condensation and liquefaction is collected into the oil storage tank TK-003 through 200-CS-FG-114/116; when the raw material temperature is reached After the temperature is higher than 260 degrees, the high-temperature oil and gas generated by the distillation kettle passes through the distillation tower R-003 and then flows through the pipeline 200-CS-FG-111/113 to the condenser E-001. After condensation and liquefaction, the heavy distillation passes through 200-CS- FG-115/117 is collected into oil storage tank TK-003;

S13. The non-condensable combustible gas is collected from the oil storage tank through 65-CS-FG-118/119 to 65-CS-FG-120 and divided into two paths, one path passes through 65-CS-FG-122 to reach the vacuum tank T-003 After buffering, it reaches the water vapor separation tank T-004 through 65-CS-FG-123 (vacuum pump P-001 extracts the water in the water vapor separation tank through pipeline 50-CS-CWS-128, passes through 50-CS-CWS-129, and reaches the vacuum pump head. (to provide negative pressure for the components of the system in front of it) reaches the water seal T-005 through 65-CS-FG-124. After being washed by the water seal, it reaches the combustion chamber burner through 50-CS-FG-127 to provide a heat source for heating the reactor. , this path is called a negative pressure pipeline, which can provide the demand for reduced pressure distillation for the still; the other path directly reaches the water seal T-005 through 65-CS-FG-121, and is washed by the water seal from 50-CS-FG- 127 reaches the combustion chamber burner and burns to provide a heat source for heating the reactor. This path is called a normal pressure pipeline;

S14. The heating method uses hot air heating in the combustion chamber F-001. The combustion chamber adopts a double-layer structure design. The inside is the high-temperature air provided by the burner. The outer layer is the furnace high-temperature flue gas reuse space. The high-temperature flue gas is passed through the high-temperature fan B-002. The 300-CS-PG-102 pipeline is divided into two lines. One line goes through the 300-CS-PG-103 pipeline and returns to the upper layer of the combustion chamber. The high-temperature air is mixed in the tail space of the combustion chamber and then reused for reactor heating. Flue gas is used. The reuse technology can save fuel to a certain extent and make the reactor heated more evenly. The other path goes through 300-CS-PG-102 to reach the air heat exchanger E-002, and exchanges heat with the air through 300-CS-PG. The -106 pipeline reaches the air-to-water heat exchanger E-003, and finally reaches the exhaust gas treatment system through the 400-CS-PG-107 pipeline;

S15. System circulating water cooling system, the first air-water heat exchanger pipeline is routed from pump P-001 through 50-CS-CWS-134 pipeline to air-water heat exchanger E-003 and then through 50-CS-CWS-135 The pipeline returns to the cooling tower to cool down and finally returns to the pool. The second routing pump P-001 passes through 50-CS-CWS-131 and reaches the condenser E-001 through the 50-CS-CWS-133 pipeline to return to the cooling tower for cooling. Finally, it returns to the pool. The third routing pump P-001 passes through the 50-CS-CWS-132 condenser E-001 and returns to the cooling tower through the 50-CS-CWS-133 pipeline to cool down and finally returns to the pool;

S16. The exhaust gas treatment system is assembled from 300-CS-PG-007 and 300-CS-PG-107 and then reaches the spray tower T-006. After spraying and dust removal, it reaches the spray tower T through the pipeline 400-PS-PG-202. -007 After secondary spraying and dust removal, it reaches the activated carbon box T-008 through pipeline 400-PS-PG-203. After adsorption and deodorization, it passes through 400-PS-PG-204 and is relay-pressurized by exhaust fan B-002 and finally passes through 400-PS. -PG-205 is discharged into the chimney;

S17. Fuel supply system, fuel tank TK-004 supplies fuel to the cracking burner U-001 through pipelines 25-CS-OIL-210 and 25-CS-HEATING-OIL-212; through pipeline 25-CS-OIL -211 and 25-CS-HEATING-OIL-213 supply fuel oil to distillation burner U-001;

S18. The distillation oil storage tank TK-003 transports the finished light and heavy oil to the finished oil tank TK-003 through the oil pump P-002 and the pipeline 50-CS-OIL-130/209/216217 respectively. It can be used as final storage. As the burner fuel provides a heat source for the system, the two-step process ends.

Preferably, in S2, the combustion chamber adopts a double-layer structure design, the inner layer is the high-temperature air provided by the burner, and the outer layer is the furnace high-temperature flue gas recycling space.

Preferably, in S6, there is an air-cooled end at the top of the catalytic tower, which is provided with cold air by blower B-001, which can provide a cooling effect to the top of the catalytic tower, allowing the oil and gas to fully contact the catalyst. In S17, the fuel tank It is designed with dual zones and can store heavy oil and diesel at the same time.

(3) Beneficial effects

The invention provides a two-step catalytic cracking distillation wax removal process flow, which has the following beneficial effects:

(1) This two-step catalytic cracking distillation wax removal process adopts a step-by-step treatment method to crack and remove plastics and other wax-prone raw materials, and further distills and purifies the wax oil to solve the problem of plastics and other wax-prone materials. Problems in the raw material cracking technology industry.

(2) This two-step catalytic cracking distillation wax removal process can save fuel to a certain extent through flue gas reuse technology, and can make the reactor more evenly heated, avoiding the risk of material coking caused by local heating of the reactor. The use of hot air for air distribution can save fuel to a certain extent and make the system more efficient. The air-cooled end at the top of the catalytic tower is provided by the blower B-001 to provide cold air, which can provide a cooling effect to the top of the catalytic tower and make the oil and gas more fully circulated. Contact with the catalyst, and pass through the catalytic tower and steam drum in parallel through the 100-CS-FG-030 pipeline and through the automatic pressure relief valve to release the gas pressure into the 200-CS-FG-009 pipeline. It is used to avoid unnecessary risks caused by high-pressure time in the system and increase the safety of the overall process.

Description of drawings

Figure 1 is a schematic diagram of the overall process of this process;

Figure 2 is a partial flow diagram of this process;

Figure 3 is a partial flow diagram of this process;

Figure 4 is a partial enlarged flow diagram of this process.

Figure 5 is a partial enlarged flow diagram of this process;

Figure 6 is a partial enlarged flow diagram of this process;

Figure 7 is a partial enlarged flow diagram of this process;

Figure 8 is a partial enlarged flow diagram of this process;

Figure 9 is a partial enlarged flow diagram of this process;

Figure 10 is a partial enlarged flow diagram of this process;

Figure 11 is a partial enlarged flow diagram of this process;

Figure 12 is a partial enlarged flow diagram of this process;

Figure 13 is a partial enlarged flow diagram of this process;

Figure 14 is a partial enlarged flow diagram of this process.

Detailed ways

Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative efforts fall within the scope of protection of the present invention.

The invention provides a technical solution: a two-step catalytic cracking distillation wax removal process flow, including the following steps:

S1. First put plastic and other raw materials into the reactor R-001, close the furnace door and then turn on the burner U-001 to start heating. As the temperature of the raw materials increases, it begins to crack.

S2. The heating method adopts combustion chamber F-001 hot air heating. The combustion chamber adopts a double-layer structure design. The inside is the high-temperature air provided by the burner, and the outer layer is the furnace high-temperature flue gas recycling space. After 300-CS-PG-032 smoke The gas recycling pipeline returns to the outer layer of the combustion chamber and the high-temperature flue gas is mixed in the tail space of the combustion chamber and then reused for heating the reactor. The use of flue gas recycling technology can save fuel to a certain extent and make the reactor heated more evenly. , to avoid the risk of material coking caused by local heating of the reactor.

S3. When the temperature of the plastic reaches the cracking temperature, high-temperature oil and gas will be generated from the reactor and pass through the first slag discharger M-001 to reach the catalytic tower T-001 or the steam drum T-002 (can be selected according to the wax deposition of the material) Whether to use direct catalytic process or choose to collect wax oil first, open or close the corresponding catalytic tower or drum valve) After catalysis or buffering, it reaches the condenser through 200-CS-FG-200 or 200-CS-FG-009 E-001, after condensation and liquefaction, is collected into the oil storage tank TK-001.

S4. The non-condensable combustible gas passes from the oil storage tank through the condenser and is divided into two lines through the 65-CS-FG-011 pipeline. One line passes through 65-CS-FG-012 to the vacuum tank TK-003, and then passes through 65-CS after being buffered. -FG-013 pipeline reaches the vacuum pump P-003, and after being extracted by the vacuum pump, it reaches the water vapor separation tank T-004 through 65-CS-FG-014. (During the working process of the vacuum pump, the water in the water vapor separation tank is automatically extracted through 10-CS-CWS -039 pipeline circulation), reaches the water seal T-005 through 65-CS-FG-015, and is further washed by the water seal and then reaches the combustion chamber through 50-CS-FG-016. The burner burns to provide a heat source for heating the reactor. The pipeline is called a negative pressure pipeline, which can effectively guide the high-temperature oil and gas in the reactor through the condenser. The other route goes directly from the 65-CS-FG-033 pipeline to the water seal without going through the vacuum system. The water seal is further washed and then reaches the combustion chamber through 50-CS-FG-016. The burner burns to provide a heat source for heating the reactor. It is a normal pressure pipeline, and oil and gas need to pass through the condenser under their own pressure. The two-way design can be switched for materials with different oil yield rates.

S5. Air distribution system for non-condensable combustible gas. Combustible gas combustion requires air distribution. Blower B-001 absorbs air from the external environment and reaches air heat exchanger E-002 through the 125-CS-AIR-031 pipeline. After heat exchange, the hot air passes through the 125-CS-AIR-032 pipeline and reaches the combustion chamber burner through 32-CS-AIR-033 and 32-CS-AIR-034 to distribute air for combustible gas combustion. In this way, using hot air for air distribution can save fuel to a certain extent and make the system more efficient.

S6. The catalytic section of the catalytic tower needs to be heated during the working process to keep the catalyst active. When heating, the high-temperature flue gas generated by the furnace heating is used. The high-temperature flue gas passes from the furnace to the high-temperature induced draft fan B-002 through 300-CS-PG-001. It is transported to the catalytic section of the catalytic tower to maintain the temperature of the catalyst. After exiting the catalytic tower, it reaches the air heat exchanger through 300-CS-PG-004/005, and then passes through 300-CS-PG-006 to the air-to-water heat exchanger E-003. 300-CS-PG-007 pipeline to exhaust gas treatment system. The other high-temperature flue gas, which does not pass through the catalytic tower, passes from the furnace through 300-CS-PG-001 and is transported by high-temperature induced draft fan B-002 and then reaches the air heat exchanger through 300-CS-PG-003/005 pipeline. -006 to the air-to-water heat exchanger E-003 and finally to the exhaust gas treatment system through the 300-CS-PG-007 pipeline. This design can meet the requirements of different catalysts that do not require temperature rise. There is an air-cooled end at the top of the catalytic tower, which is provided with cold air by the blower B-001, which can provide a cooling effect on the top of the catalytic tower, allowing the oil and gas to fully contact the catalyst.

S7. The pressure relief system of the catalytic tower and steam drum. When the pressure of the system is too high, automatic emergency pressure relief is required. The catalytic tower and steam drum are connected in parallel through the 100-CS-FG-030 pipeline and the gas pressure is reduced through the automatic pressure relief valve. Release into line 200-CS-FG-009. Used to avoid unnecessary risks caused by high-voltage times in the system.

S8. Slag discharging system. When the material is cracked and the temperature of the main furnace system drops to 80 degrees, slag discharging can begin. The specific operation is to switch the rotation direction of the reactor, and the slag will be transported to the slag discharging machine M through the internal lifting plate of the reactor. -001, through the 300-CS-PS-017 pipeline to the water-cooled slag tapping machine M-002, and finally discharged out of the furnace through the 300-CS-PS-018 pipeline.

S9. Heating system of oil storage tank. When the oil in the oil storage tank condenses into wax at room temperature and loses fluidity, the heating coil at the bottom of the oil tank is used to introduce high-temperature steam to melt the wax oil. Then the fluidity is restored, specifically through the steam boiler F-002 to generate high-temperature water vapor, which is transported to the internal coil of the oil storage tank through the 40-CS-LS-038 pipeline. The wax oil in the oil storage tank is preheated and begins to melt. The heat-exchanged steam is collected through the hydrophobic collection tank TK-002 and finally returned to the steam boiler through the 40-CS-LS-037 pipeline for reuse.

S10. System circulating water cooling system, the first air-water heat exchanger pipeline is routed from pump P-001 through 50-CS-CWS-027 pipeline to air-water heat exchanger E-003 and then through 50-CS-CWS-028 /029 pipeline returns to the cooling tower to cool down and finally returns to the pool. The second routing pump P-001 passes through 50-CS-CWS-021 to reach the water-cooling jacket of the TK-001 oil storage tank and then passes through 50-CS-CWS-024 Finally, it reaches the condenser E-001 and returns to the cooling tower through the 50-CS-CWS-025/023/029 pipeline to cool down and finally returns to the pool. The third routing pump P-001 arrives respectively through the 50-CS-CWS-022. The water-cooled slag extractor M-002 and condenser E-001 return to the cooling tower through the 50-CS-CWS-023/029 pipeline for cooling and finally return to the pool.

The cracked oil in S11.TK-001 reaches the distillation kettle R-002 through the oil pump P-002 and the 50-CS-OIL-035 pipeline.

S12. After the raw materials in the distillation kettle are filled, close the incoming pipeline and turn on the burner U-001 to start heating the distillation kettle. When the raw material temperature reaches 180 degrees, the high-temperature oil and gas generated by the distillation kettle will pass through the distillation tower R-003 and then pass through the pipeline. 200-CS-FG-111/112 to the condenser E-001, and the light fraction after condensation and liquefaction is collected into the oil storage tank TK-003 through 200-CS-FG-114/116. When the raw material temperature is higher than 260 degrees, the high-temperature oil and gas produced by the distillation kettle passes through the distillation tower R-003 and then flows through the pipeline 200-CS-FG-111/113 to the condenser E-001. After condensation and liquefaction, it is re-distilled. Collected into oil storage tank TK-003 via 200-CS-FG-115/117. Through this design, light and heavy fractions can be collected separately.

S13. The non-condensable combustible gas is collected from the oil storage tank through 65-CS-FG-118/119 to 65-CS-FG-120 and divided into two paths, one path passes through 65-CS-FG-122 to reach the vacuum tank T-003 After buffering, it reaches the water vapor separation tank T-004 through 65-CS-FG-123 (vacuum pump P-001 extracts the water in the water vapor separation tank through pipeline 50-CS-CWS-128, passes through 50-CS-CWS-129, and reaches the vacuum pump head. (to provide negative pressure for the components of the system in front of it) reaches the water seal T-005 through 65-CS-FG-124. After being washed by the water seal, it reaches the combustion chamber burner through 50-CS-FG-127 to provide a heat source for heating the reactor. , this path is called a negative pressure pipeline, which can provide the vacuum distillation needs for the still. The other path goes directly to the water seal T-005 through 65-CS-FG-121. After being washed by the water seal, it reaches the combustion chamber burner through 50-CS-FG-127 to provide a heat source for heating the reactor. This path is called normal pressure. pipeline.

S14. The heating method uses hot air heating in the combustion chamber F-001. The combustion chamber adopts a double-layer structure design. The inside is the high-temperature air provided by the burner. The outer layer is the furnace high-temperature flue gas reuse space. The high-temperature flue gas is passed through the high-temperature fan B-002. The 300-CS-PG-102 pipeline is divided into two lines. One line goes through the 300-CS-PG-103 pipeline and returns to the upper layer of the combustion chamber. The high-temperature air is mixed in the tail space of the combustion chamber and then reused for reactor heating. Flue gas is used. The reuse technology can save fuel to a certain extent and make the reactor heated more evenly. The other path goes through 300-CS-PG-102 to reach the air heat exchanger E-002, and exchanges heat with the air through 300-CS-PG. The -106 pipeline reaches the air-to-water heat exchanger E-003, and finally reaches the exhaust gas treatment system through the 400-CS-PG-107 pipeline.

S15. System circulating water cooling system, the first air-water heat exchanger pipeline is routed from pump P-001 through 50-CS-CWS-134 pipeline to air-water heat exchanger E-003 and then through 50-CS-CWS-135 The pipeline returns to the cooling tower to cool down and finally returns to the pool. The second routing pump P-001 passes through 50-CS-CWS-131 and reaches the condenser E-001 through the 50-CS-CWS-133 pipeline to return to the cooling tower for cooling. Finally, it returns to the pool. The third routing pump P-001 passes through the 50-CS-CWS-132 condenser E-001 and returns to the cooling tower through the 50-CS-CWS-133 pipeline to cool down and finally returns to the pool.

S16. The exhaust gas treatment system is assembled from 300-CS-PG-007 and 300-CS-PG-107 and then reaches the spray tower T-006. After spraying and dust removal, it reaches the spray tower T through the pipeline 400-PS-PG-202. -007 After secondary spraying and dust removal, it reaches the activated carbon box T-008 through pipeline 400-PS-PG-203. After adsorption and deodorization, it passes through 400-PS-PG-204 and is relay-pressurized by exhaust fan B-002 and finally passes through 400-PS. -PG-205 is discharged into the chimney.

S17. Fuel supply system, fuel tank TK-004 supplies fuel to the cracking burner U-001 through pipelines 25-CS-OIL-210 and 25-CS-HEATING-OIL-212. Fuel is supplied to the distillation burner U-001 through pipelines 25-CS-OIL-211 and 25-CS-HEATING-OIL-213. The fuel tank is a dual-zone design that can store heavy oil and diesel to meet the utilization of different oil products.

S18. The distillation oil storage tank TK-003 transports the finished light and heavy oil to the finished oil tank TK-003 through the oil pump P-002 and the pipeline 50-CS-OIL-130/209/216217 respectively. It can be used as final storage. As the burner fuel provides a heat source for the system, the two-step process ends.

In summary, this two-step catalytic cracking distillation wax removal process uses a step-by-step approach to crack and remove plastics and other wax-prone raw materials, and further distills and purifies the wax oil, solving the problem of plastics and other wax-prone materials. The technical problem of cracking wax raw materials solves the problem that most intermittent cracking equipment will basically cause high-temperature oil and gas to be pre-cooled and liquefied in the condenser when cracking plastics, and finally condenses into waxy oil in the oil storage tank. Wax at room temperature After the liquid oil condenses in the oil storage tank and loses its fluidity, it cannot be flexibly transferred, which brings huge difficulties to the next processing and transportation work.

It should be noted that in this article, relational terms such as first and second are only used to distinguish one entity or operation from another entity or operation, and do not necessarily require or imply that these entities or operations are mutually exclusive. any such actual relationship or sequence exists between them. Furthermore, the terms "comprises," "comprises," or any other variations thereof are intended to cover a non-exclusive inclusion such that a process, method, article, or apparatus that includes a list of elements includes not only those elements, but also those not expressly listed other elements, or elements inherent to the process, method, article or equipment.

Although the embodiments of the present invention have been shown and described, those of ordinary skill in the art will understand that various changes, modifications, and substitutions can be made to these embodiments without departing from the principles and spirit of the invention. and modifications, the scope of the invention is defined by the appended claims and their equivalents.

Claims (3)

1. A two-step catalytic cracking distillation wax removal process flow is characterized in that: the method comprises the following steps:

s1, firstly, putting raw materials such as plastics and the like into a reaction kettle R-001, closing a furnace door, opening a burner U-001 to start heating, and starting cracking along with the temperature rise of the raw materials;

s2, adopting a combustion chamber F-001 hot air heating mode, returning materials to the outer layer of the combustion chamber through a 300-CS-PG-032 flue gas recycling pipeline, and mixing the materials with high-temperature flue gas in the tail space of the combustion chamber and then reusing the materials for heating the reaction kettle, so that the reaction kettle is heated more uniformly;

s3, when the temperature rise of plastics and the like is reached and the cracking temperature is reached, high-temperature oil gas is generated, and then reaches a catalytic tower T-001 or a steam drum T-002 (whether a direct catalytic process or a first wax oil collection process is adopted or a corresponding catalytic tower or steam drum valve is selected according to the wax precipitation condition of materials) from the reaction kettle, and then reaches a condenser E-001 through 200-CS-FG-200 or 200-CS-FG-009 after catalysis or buffering, and is collected into an oil storage tank TK-001 after condensation and liquefaction;

s4, the non-condensable combustible gas is divided into two paths by a 65-CS-FG-011 pipeline from an oil storage tank through a condenser, one path reaches a vacuum tank TK-003 through a 65-CS-FG-012 pipeline after buffering, reaches a vacuum pump P-003 through a 65-CS-FG-014 pipeline after being pumped by the vacuum pump, (water in the water vapor separation tank is automatically pumped in the working process of the vacuum pump and circulates through a 10-CS-CWS-039 pipeline), reaches a water seal T-005 through the 65-CS-FG-015, is further washed by water seal and reaches a combustion chamber flame nozzle through a 50-CS-FG-016 pipeline to burn to provide a heat source for the temperature rise of the reaction kettle, the path is called a negative pressure pipeline, high-temperature oil gas in the reaction kettle can be effectively guided through the condenser, the other path does not directly reach the water seal through the 65-CS-FG-033 pipeline, is further washed by the water seal and reaches the combustion chamber flame nozzle through the 50-CS-016 pipeline to burn to provide a heat source for the reaction kettle, and the path is a pipeline, and the pressure of the path is required to be switched to the two different rates by the design of the pressure of the oil gas;

s5, an AIR distribution system of the non-condensable combustible gas is used for distributing AIR when the combustible gas is combusted, an AIR blower B-001 sucks AIR in an external environment, the AIR passes through a 125-CS-AIR-031 pipeline to reach an AIR heat exchanger E-002, and hot AIR passes through the 125-CS-AIR-032 pipeline to reach a combustion chamber nozzle from 32-CS-AIR-033 and 32-CS-AIR-034 to distribute AIR for the combustible gas combustion;

s6, the catalytic section of the catalytic tower needs to be heated in the working process to keep the activity of the catalyst, high-temperature flue gas generated by heating a hearth is adopted in the heating process, the high-temperature flue gas is conveyed from the hearth to the catalytic section of the catalytic tower through a high-temperature induced draft fan B-002 to keep the temperature of the catalyst, after the high-temperature flue gas exits from the catalytic tower, the high-temperature flue gas reaches from the 300-CS-PG-004/005 to an air heat exchanger through a 300-CS-PG-006 to an air heat exchanger E-003 and finally flows through a 300-CS-PG-007 pipeline to a tail gas treatment system, and the other high-temperature flue gas which does not pass through the catalytic tower is conveyed from the hearth through the 300-CS-PG-001 to the air heat exchanger through a high-temperature induced draft fan B-002 to reach from the 300-CS-PG-003/005 pipeline to the air heat exchanger through the 300-CS-PG-006 to the air heat exchanger E-003 and finally flows through the 300-CS-PG-007 pipeline to the tail gas treatment system;

s7, a pressure relief system of the catalytic tower and the steam drum needs to automatically and emergently relieve pressure when the pressure of the system is excessive, and the catalytic tower and the steam drum are connected in parallel to release the gas pressure into a 200-CS-FG-009 pipeline through an automatic pressure relief valve through a 100-CS-FG-030 pipeline;

s8, a slag discharging system starts slag discharging after the temperature of the main furnace system is reduced to 80 ℃ after the pyrolysis of the materials is finished, specifically, the rotating direction of the reaction kettle is switched, the materials are conveyed into a slag discharging machine M-001 by slag through a shoveling plate in the reaction kettle, and finally discharged out of the furnace through a 300-CS-PS-018 pipeline to a water-cooling slag discharging machine M-002 through a 300-CS-PS-017 pipeline;

s9, a heating system of the oil storage tank is adopted, and when the oil in the oil storage tank is condensed into wax and loses fluidity in a normal temperature state, high-temperature steam is introduced into a heating coil at the bottom of the oil tank to melt wax oil; the fluidity is recovered, namely high-temperature steam is generated through a steam boiler F-002 and is conveyed into a coil pipe inside an oil storage tank through a 40-CS-LS-038 pipeline, wax oil in the oil storage tank is preheated and begins to melt, and the steam after heat exchange is collected through a hydrophobic collection tank TK-002 and finally returned into the steam boiler through the 40-CS-LS-037 pipeline for reuse;

s10, a circulating water cooling system of the system, wherein a first path of empty water heat exchanger pipeline is returned to a cooling tower by a 50-CS-CWS-028/029 pipeline to be cooled after reaching an empty water heat exchanger E-003 by a 50-CS-CWS-027 pipeline, a second path of empty water heat exchanger pipeline is returned to a cooling jacket of a TK-001 oil storage tank by a 50-CS-CWS-021, then reaches a condenser E-001 by a 50-CS-CWS-024 pipeline to be returned to the cooling tower to be cooled and finally returned to a water tank by a 50-CS-CWS-025/023/029 pipeline, and a third path of empty water heat exchanger pipeline is returned to the cooling tower by a 50-CS-CWS-022 pipeline to be cooled after reaching a water cooling slag extractor M-002 and a condenser E-001 by a 50-CS-CWS-023/029 pipeline, respectively, and finally returned to the water tank;

s11, the pyrolysis OIL in the TK-001 reaches the distillation still R-002 from a 50-CS-OIL-035 pipeline through an OIL pump P-002;

s12, closing an incoming material pipeline after the raw material of the distillation still is filled, starting a burner U-001 to start heating the distillation still, and collecting light fraction after condensation and liquefaction into an oil storage tank TK-003 through a pipeline 200-CS-FG-111/112 after high-temperature oil gas generated by the distillation still passes through a distillation tower R-003 until the temperature of the raw material reaches 180 DEG; when the temperature of the raw materials is higher than 260 ℃, high-temperature oil gas generated by the distillation kettle passes through a distillation tower R-003 and then enters a condenser E-001 through a pipeline 200-CS-FG-111/113, and the heavy fraction after condensation and liquefaction is collected into an oil storage tank TK-003 through a pipeline 200-CS-FG-115/117;

s13, collecting non-condensable combustible gas from an oil storage tank, namely 65-CS-FG-118/119, dividing the gas into two paths, namely 65-CS-FG-120, namely 65-CS-FG-122, buffering the gas in a vacuum tank T-003, and then 65-CS-FG-123, namely a water-vapor separation tank T-004 (a vacuum pump P-001 pumps water in the water-vapor separation tank through a pipeline 50-CS-CWS-128, namely 50-CS-CWS-129, a vacuum pump head and negative pressure for parts of a previous system) and then 65-CS-FG-124, namely a water seal water-washing, and then 50-CS-FG-127, namely a combustion chamber nozzle for heating the reaction kettle to provide a heat source, namely a negative pressure pipeline, so that the distillation kettle can provide a decompression distillation requirement; the other path directly reaches a water seal T-005 through 65-CS-FG-121, and reaches a combustion chamber nozzle from 50-CS-FG-127 for combustion after water seal washing to provide a heat source for heating the reaction kettle, and the path is called a normal pressure pipeline;

s14, the heating mode adopts a combustion chamber F-001 hot air heating mode, the combustion chamber adopts a double-layer structure design, high-temperature air is provided for a combustion machine inside, the outer layer is a hearth high-temperature flue gas recycling space, high-temperature flue gas is divided into two paths by a 300-CS-PG-102 pipeline through a high-temperature fan B-002, one path of the high-temperature flue gas returns to the outer layer of the combustion chamber through a 300-CS-PG-103 pipeline and is reused for heating a reaction kettle after being mixed in the tail space of the combustion chamber, the fuel can be saved to a certain extent by adopting the flue gas recycling technology, the reaction kettle can be heated more uniformly, the other path of the high-temperature flue gas reaches an air heat exchanger E-003 through the 300-CS-PG-102, and finally reaches the air water heat exchanger E-003 through the 300-CS-PG-106 pipeline after air heat exchange, and finally reaches the tail gas treatment system through a 400-CS-PG-107 pipeline;

s15, a circulating water cooling system of the system, wherein a first path of empty water heat exchanger pipeline is returned to a cooling tower by a 50-CS-CWS-135 pipeline to be cooled by a pump P-001 after reaching an empty water heat exchanger E-003 through a 50-CS-CWS-134 pipeline, a second path of empty water heat exchanger pipeline is returned to a cooling tower by a 50-CS-CWS-131 to be cooled by a condenser E-001 after being returned to the cooling tower by a 50-CS-CWS-133 pipeline, and a third path of empty water heat exchanger pipeline is returned to the cooling tower by a 50-CS-CWS-133 pipeline to be cooled by a third path of empty water heat exchanger pipeline P-001;

s16, the tail gas treatment system is collected by 300-CS-PG-007 and 300-CS-PG-107, then reaches a spray tower T-006, is subjected to spray dust removal, then reaches the spray tower T-007 by a pipeline 400-PS-PG-202, is subjected to secondary spray dust removal, reaches an activated carbon box T-008 by a pipeline 400-PS-PG-203, is subjected to adsorption deodorization, and finally is subjected to relay pressurization by a tail gas fan B-002 by a tail gas fan 204 to be finally discharged to a chimney through 400-PS-PG-205;

s17, a fuel supply system, wherein a fuel tank TK-004 supplies fuel to a cracking burner U-001 through pipelines 25-CS-OIL-210 and 25-CS-HEATING-OIL-212; supplying fuel to the distillation burner U-001 via lines 25-CS-OIL-211 and 25-CS-HEATING-OIL-213;

s18, distilling the OIL storage tank TK-003, and conveying the finished light heavy OIL into the finished OIL tank TK-003 through the OIL pump P-002 by the pipeline 50-CS-OIL-130/209/216217 respectively, wherein the finished light heavy OIL can be stored as the final product, and can also be used as the fuel of a combustion engine to provide a heat source for a system, so that the two-step process is finished.

2. The two-step catalytic cracking distillation dewaxing process according to claim 1, wherein: in the S2, the combustion chamber adopts a double-layer structure design, the inside is high-temperature air provided by the combustion machine, and the outer layer is a high-temperature flue gas recycling space of the hearth.

3. The two-step catalytic cracking distillation dewaxing process according to claim 1, wherein: in S6, there is the forced air cooling end at catalysis tower top by air-blower B-001 provides cold wind, can provide the cooling effect for catalysis tower top, make oil gas more abundant with the catalyst contact, in S17, the fuel tank is two district designs, can deposit heavy oil and diesel oil simultaneously.