CATALYTIC CRACKING FRACTIONATION AND ABSORPTION STABILIZATION SYSTEM, AND ENERGY SAVING METHOD THEREOF

Abstract

The present invention provides a catalytic cracking fractionation and absorption-stabilization system, and energy saving method thereof; the present invention is to arrange a waste heat refrigerator of the main fractionating tower, a waste heat refrigerator of rich gas and a waste heat refrigerator of stabilizer in a catalytic cracking fractionation and absorption-stabilization system so as to utilize low temperature waste heat at the top of a main fractionating tower, rich gas, stable gasoline, intermediate heat exchange flow of an absorber of the system as a refrigerator driving heat source; in order to cool naphtha and circulating gasoline to a low temperature lower than 40° C., control low temperature operations of the absorber and reduce the heat load of a desorber and a stabilizer, and the heat extracted by the refrigerators is cooled by cooling water with a higher temperature so as to reduce the consumption of the cooling water. In addition, developed residual pressure generating units and waste heat generating units coordinate to convert medium and low pressure of the dry gas and low-grade waste heat of other products in the system into electric energy that can be conveyed into a grid, therefore the electricity consumption of a dry gas compressor can be supplemented, and the operation cost of the system is reduced to the minimum.

Claims

1. A catalytic cracking fractionation and absorption-stabilization system of an oil refinery, wherein heat is extracted from the top of a main fractionating tower (1) by a waste heat refrigerator to serve as a refrigerator driving heat source after heat extraction so as to cool naphtha; rich gas (28) at the top of the main fractionating tower enters into a compressor for compression, the compressed rich gas is mixed with rich gasoline (30) discharged from the bottom of an absorber and desorbed gas (31) discharged from the top of a desorber, and the mixture enters into a gas-liquid separation tank (8) to reduce the phase splitting temperature therein after being cooled in a waste heat refrigerator; a diesel oil tower (2) is arranged on the siding of the main fractionating tower (1), after the diesel oil discharged from the bottom of the diesel oil tower (2) exchanges heat with a diesel oil heat exchanger (11), the residual waste heat is used for generating power by a waste heat generator; in an absorption-stabilization system, two absorber intermediate heat exchangers (21) serially connected are arranged on each side edge of an absorber (9) and are serially connected with the waste heat refrigerator that is driven by the waste heat of the stable gasoline by pipelines so as to extract the heat discharged by the absorber in time during absorption and control low temperature absorption of the absorber; a residual pressure generator is connected to the top of a reabsorber (10) to generate power by the medium and low residual pressure of dry gas (32) at the top; a liquid phase at the bottom of a stabilizer (18) preheats the feedstock by a feedstock heat exchanger and is entered into the waste heat refrigerator, a part of the discharge is extracted as product gasoline (34), and the other part enters into the waste heat refrigerator to be refrigerated and cooled and returns to the top of the absorber from the waste heat refrigerator to serve as circulating gasoline (35); and the electricity generated by the residual pressure generator and the waste heat generator are respectively conveyed into a grid by electric wires, and the power supply used by the compressor is led out from the grid by an electric wire.

2. An energy saving method for the catalytic cracking fractionation and absorption-stabilization system of the oil refinery according to claim 1, wherein a catalytic cracking reaction product (23) and rich diesel oil (24) returning from the bottom of the reabsorber (10) enter into the main fractionating tower (1) for oil cutting according to different boiling point ranges, heat is extracted from top oil gas (25) by a waste heat refrigerator (3) of the main fractionating tower to serve as a refrigerator driving heat source, the top oil gas enters into a naphtha tank (4) after being cooled within the temperature ranges from 40 to 80° C., the liquid phase in the tank is naphtha, a part of the naphtha returns to the tower as backflow, the other part of the naphtha is cooled by the waste heat refrigerator (3) of the main fractionating tower, and naphtha (26) is cooled within the temperature ranges from solidifying point to 40° C. and then enters into the top of the absorber (9); the rich gas (28) is discharged from the naphtha tank (4) and is pressurized to 0.1 to 3 MPa in a compressor (6), the electricity is led out by a compressor power supply (39) from a grid (22), and the compressed rich gas is mixed with the rich gasoline (30) at the bottom of the absorber and the desorbed gas (31) at the top of a desorber (15); a mixed gas-liquid phase enters into a waste heat refrigerator (7) of rich gas to exchange heat within the temperature ranges from solidifying point to 40° C., the rich gas separated by the gas-liquid separation tank (8) enters into the absorber (9) from the bottom, the operating pressure of the absorber (9) is within the pressure ranges from 0.8 to 2.6 Mpa, the naphtha and the circulating gasoline at the top mainly absorb C3, C4 components in the rich gas, and the two absorber intermediate heat exchangers (21) serially connected on the side edge of the tower extract heat from the siding so as to keep the low temperature absorption of the absorber at the temperature ranges from 5 to 80° C.; light components containing the gasoline enter into the reabsorber (10) and are absorbed by the circulating diesel oil, the operating pressure of the reabsorber (10) is within the pressure ranges from 0.8 to 2.6 Mpa, the dry gas (32) is pressurized by a residual pressure generator (13) to the atmospheric pressure to be discharged, and the electricity generated by the residual pressure generator (13) is conveyed into a grid (22) by a power supply (38) of residual pressure power generation; diesel oil containing rich gasoline components is discharged from the bottom of the reabsorber (10), exchanges heat with diesel oil (27) through the diesel oil heat exchanger (11) to be heated within the temperature ranges from 150 to 250° C., and is circulated to the top of the main fractionating tower (1) as rich diesel oil (24); the diesel oil tower is arranged on the siding of the main fractionating tower (1), light components are removed from the liquid phase extracted from the side of the main fractionating tower by the refining of the diesel oil tower (2), after the diesel oil (27) extracted from the bottom of the diesel oil tower (2) is cooled within the temperature ranges from 80 to 150° C. by the heat exchange with the diesel oil heat exchanger (11), the temperature is still high, so the diesel oil can be used as the waste heat source of a waste heat generator (12), the generated electricity is conveyed into the grid (22) by a power supply (37) of waste heat power generation to supplement the power consumption, the diesel oil is cooled to 40° C. after heat extraction, a part of the diesel oil is circulated to the reabsorber, and the rest part is extracted as product diesel oil (33).

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0014] FIG. 1 is a schematic diagram of an energy saving flow of a catalytic cracking fractionation and absorption-stabilization system.

[0015] In which:

[0016] main fractionating tower 1, diesel oil tower 2, waste heat refrigerator 3 of main fractionating tower, naphtha tank 4, slurry heat exchanger 5, compressor 6, waste heat refrigerator 7 of rich gas, gas-liquid separation tank 8, absorber 9, reabsorber 10, diesel oil heat exchanger 11, waste heat generator 12, residual pressure generator 13, waste heat refrigerator 14 of stabilizer, desorber 15, desorber reboiler 16, feedstock heat exchanger 17, stabilizer 18, stabilizer condenser 19, stabilizer reboiler 20, absorber intermediate heat exchanger 21, grid 22; catalytic cracking reaction product 23, rich diesel oil 24, oil gas 25, naphtha 26, diesel oil 27, rich gas 28, product slurry 29, rich gasoline 30, desorbed gas 31, dry gas 32, product diesel oil 33, product gasoline 34, circulating gasoline 35, liquefied petroleum gas 36, power supply 37 of waste heat power generation, power supply 38 of residual pressure power generation and compressor power supply 39.

DETAILED DESCRIPTION OF THE EMBODIMENTS

[0017] The present invention provides a catalytic cracking fractionation and absorption-stabilization system, and an energy saving method thereof. The present invention is illustrated by the following embodiments, but is not limited to the following embodiments. The present invention will be further described in detail combining with the drawings.

[0018] The catalytic cracking fractionation and absorption-stabilization system of an oil refinery of the present invention comprises: heat is extracted from the top of a main fractionating tower 1 by a waste heat refrigerator to serve as a refrigerator driving heat source for cooling naphtha; the rich gas 28 at the top of the main fractionating tower enters into a compressor for compression, and the compressed rich gas is mixed with rich gasoline 30 discharged from the bottom of an absorber and desorbed gas 31 discharged from the top of a desorber, and the mixture enters into a gas-liquid separation tank 8 to reduce the phase splitting temperature therein after being cooled in a waste heat refrigerator. A diesel oil tower 2 is arranged on the siding of the main fractionating tower 1, after the diesel oil discharged from the bottom of the diesel oil tower 2 exchanges heat with a diesel oil heat exchanger 11, the residual waste heat is used for generating power by a waste heat generator. In an absorption-stabilization system, two absorber intermediate heat exchangers 21 serially connected are arranged on each side edge of an absorber 9 and are serially connected with the waste heat refrigerator that is driven by the waste heat of the stable gasoline by pipelines so as to extract the heat discharged by the absorber during absorption and control low temperature absorption of the absorber. A residual pressure generator is connected to the top of a reabsorber 10 to generate power by the medium and low residual pressure of dry gas 32 at the top. A liquid phase at the bottom of a stabilizer 18 preheats the feedstock by a feedstock heat exchanger and is entered into the waste heat refrigerator, a part of the discharge is extracted as product gasoline 34, and the other part enters into the waste heat refrigerator to be refrigerated and cooled and returns to the top of the absorber from the waste heat refrigerator to serve as circulating gasoline 35. The electricity generated by the residual pressure generator and the electricity generated by the waste heat generator are respectively conveyed into a grid by electric wires, and the power supply used by the compressor is led out from the grid by an electric wire.

Embodiment

[0019] A 1.2 million t/year catalytic cracking fractionation and absorption-stabilization system of a petrochemical enterprise is reformed, the waste heat refrigeration, residual pressure and waste heat power generation technology are not adopted in the original process, the cooling temperature is a circulating water temperature 40° C., as shown in FIG. 1, the energy consumption under a certain condition is compared with that of the original process after reformation:

[0020] The mixture product 23 produced about 92 t/h of gasoline, diesel oil and slurry produced by a catalytic cracking reaction device, and 31.5 t/h rich diesel oil 24 returning from the bottom of the reabsorber 10 respectively enter into the main fractionating tower 1 from the bottom and the top for distillating separation at the atmospheric pressure, the top oil gas 25 is cooled by the waste heat refrigerator 3 of main fractionating tower to 40° C., heat is extracted to serve as the refrigerator driving heat source, and the liquid phase in the naphtha tank 4 performs back flow at 40° C., 30 t/h naphtha 26 is subjected to further low temperature cooling by the waste heat refrigerator 3 of the main fractionating tower for cooling down to 20° C., and enters into the top of the absorber 9. The gas phase 32 t/h rich gas 28 in the naphtha tank 4 enters into the compressor 6 to be pressurized to 1.5 MPa, the compressed rich gas is then mixed with the rich gasoline 30 discharged from the bottom of the absorber and the desorbed gas 31 discharged from the top of the desorber 15, and the mixture is cooled by the waste heat refrigerator 7 of rich gas to 30° C. by heat extraction. The rich gas enters into the bottom of the absorber 9 with the operating pressure ranges from 1.2 to 1.4 MPa after 30° C. gas-liquid balance, the absorber intermediate heat exchangers 21 extract heat from the siding of the absorber via a cold source provided by the waste heat refrigerator 14 of stabilizer so as to keep the low temperature absorption at the temperature ranges from 25 to 35° C., the light components carrying gasoline enter into the reabsorber 10 to be absorbed by the circulating diesel oil, the 4 t/h dry gas 32 is depressurized to the atmospheric pressure via the energy extraction of the residual pressure generator 13 to be discharged for combustion, and the electricity generated by the residual pressure generator 13 is conveyed into the grid 22.

[0021] The diesel oil at the bottom of the reabsorber 10 exchanges heat with the diesel oil 27 through the diesel oil heat exchanger 11 to be heated to 210° C., and is circulated to the top of the main fractionating tower 1 as rich diesel oil 24. A diesel oil tower is arranged on the siding of the main fractionating tower 1. The diesel oil tower 2 removes the light components by refining, the 51 t/h diesel oil 27 extracted from the bottom is cooled to 130° C. by the heat exchange with the diesel oil heat exchanger 11 and is used as the waste heat source of a waste heat generator 12, the diesel oil after heat extraction is cooled to 40° C., 21 t/h product diesel oil 33 is extracted, and the rest is circulated to the reabsorber.

[0022] The liquid phase separated from the gas-liquid separation tank 8 enters into the desorber 15 with an operating pressure of 1.6 MPa to separate C2, C3 and C4 components, the desorbed gas 31 is mixed with compressed gas, heavy components enter into the stabilizer 18 with the operating pressure of 1.2 MPa to be separated, a product of liquefied petroleum gas 36 is discharged from the top, after stable gasoline at the bottom preheats the feedstock, heat is extracted from the same by a waste heat refrigerator 14 of stabilizer, 35 t/h product gasoline 34 is extracted, and the rest is cooled by the waste heat refrigerator 14 of stabilizer to 20° C. and is circulated to the top of the absorber 9. A slurry heat exchanger 5 is arranged at the bottom of the main fractionating tower 1, after cooled the high-temperature slurry from 310° C. to 250° C., 3.8 t product slurry 29 is extracted, and the rest returns to the bottom of the main fractionating tower 1.

TABLE-US-00001 TABLE 1 Energy consumption and output statistics of waste heat refrigerating unit Waste heat Waste heat Waste heat refrigerator 3 of main refrigerator 7 refrigerator 14 fractionating tower of rich gas of stabilizer Waste heat input 22800 2370 5518 Mkcal/h Refrigerating 400 600 350 capacity KW Circulating water 1900 0 540 consumption t/h

[0023] The generating capacity of the waste heat generator 12 is 10 KW, and the generating capacity of the residual pressure generator 13 is 300 KW.

TABLE-US-00002 TABLE 2 Comparison of energy consumption and emission of the original process and the energy saving process Energy Statistical item Original process saving process Dry gas dosage t/h 4281 4253 Circulating gasoline dosage t/h 38244 27930 Power consumption KW 730 410 System heat input Mkcal/h 15.14 12.13 Waste heat emission Mkcal/h 32.8 24.1 Circulating water consumption t/h 4124 3003 20% of energy is saved after system reformation, and the waste heat emission is reduced by 27% Note: the raw material of the fractionating tower is the high-temperature material discharged from the reactor, the carried heat energy is not included in the heat input of the system, and the heat input of the fractionating tower is only included in the energy consumption of the reboiler.

[0024] The catalytic cracking fractionation and absorption-stabilization system of the oil refinery and the energy saving method provided by the present invention have been described by preferred embodiments. Apparently, those skilled in the art can make modifications or proper variations and combinations to the structures and equipment described herein without departing from the contents, spirit and scope of the present invention so as to achieve the technology of the present invention. It should be particularly noted that all similar substitutions and modifications are apparent to those skilled in the art, and these substitutions and modifications are deemed to be encompassed within the spirit, scope and contents of the present invention.