CN112410069B - Hydrorefining process for catalytic cracking crude gasoline - Google Patents

Hydrorefining process for catalytic cracking crude gasoline Download PDF

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CN112410069B
CN112410069B CN202010870690.1A CN202010870690A CN112410069B CN 112410069 B CN112410069 B CN 112410069B CN 202010870690 A CN202010870690 A CN 202010870690A CN 112410069 B CN112410069 B CN 112410069B
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tower
gasoline
gas
oil
crude
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CN112410069A (en
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李国庆
卓楷升
仝保田
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Guangdong Chuanxun Technology Co.,Ltd.
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South China University of Technology SCUT
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/16—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural parallel stages only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline

Abstract

The invention discloses a hydrofining process of catalytically cracked naphtha, which is improved on the basis of the prior hydrofining process flow of catalytically cracked naphtha and catalytically stabilized naphtha as follows: the catalytic crude gasoline is changed from the original entering absorption tower to the direct entering gasoline hydrofining device, and other processes are not changed. Thus, it is possible to provideThe catalytic absorption stabilizing system only processes rich gas and does not process crude gasoline, so that the load and the energy consumption are greatly reduced; less than or equal to C hydrogenated with crude gasoline4The component does not influence the hydrogenation operation and will follow the H2S、NH3The acidic components are pulled out from the stripping tower together, and the catalytic refining is returned after the original process, so that the steam pressure of the gasoline is stabilized by the product, and the gasoline is guaranteed; a small amount of gasoline which is carried along with rich gas and is stably absorbed is continuously distilled from the bottom of the stable tower, and after heat exchange, the gasoline is mixed with crude gasoline in the original flow and is hydrogenated, so that the material balance of the combined device is not changed.

Description

Hydrorefining process for catalytic cracking crude gasoline
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a catalytic cracking crude gasoline hydrofining process.
Background
Catalytic cracking is one of the main methods for secondary processing of petroleum fractions, and is a process for converting heavy distillate oil into diesel oil, gasoline and gas through cracking reaction under the action of high temperature and catalyst. It is composed of four parts of reaction regeneration, main fractionation, stable absorption and flue gas energy recovery. The absorption stabilization function of the system is to convert the rich gas and the crude gasoline from the main fractionating tower into qualified products, and the system comprises six main units, namely a rich gas compressor, a condensation oil tank, an absorption tower, a reabsorption tower, a desorption tower and a stabilization tower. Wherein the reabsorption tower is used for absorbing the overhead gas of the tower by using the secondary adsorption of diesel oil to obtain more than or equal to C 3The component content is less than or equal to 3 mol percent of the product dry gas; the function of the stabilizer is to rectify deethanized gasoline from the bottom of the desorption tower to obtain C at the top of the tower5Liquid hydrocarbon (LPG) product with the content less than or equal to 1 mol percent, and stable gasoline product with qualified vapor pressure at the tower bottom.
Stabilized gasoline is the main product of catalytic cracking, and it is known that most of the gasoline in the country is catalytically cracked stabilized gasoline. But because of being rich in sulfur, nitrogen, olefin, aromatic hydrocarbon and the like, the catalyst can not be directly used as a product and needs hydrofining. The conventional process is to send the stable gasoline from the catalytic cracking unit to a hydrorefining unit, remove the impurities such as sulfur, nitrogen and the like from the stable gasoline through a fixed bed hydrogenation reactor under the action of a catalyst at a certain temperature, and ensure that the contents of olefin and aromatic hydrocarbon are qualified. The oil produced by the subsequent reaction is fed into a stripping tower (also called a stabilizer tower) to remove H2S、NH3The acid component formed in the course of equal hydrogenation and less than or equal to C4After the fraction is sent to a fractionation unit to obtainTo light and heavy gasoline. The problem arises that since the hydrofining device also has the function of removing C or less4The function of the distillate, then can it be processed directly into naphtha? Therefore, the upstream catalytic absorption stabilizing system only treats rich gas, and the load and the energy consumption are greatly reduced. The present invention has been made in view of such a consideration.
Disclosure of Invention
In order to solve the defects of repeated fractionation of stable gasoline, large treatment capacity of an absorption stabilization system and high energy consumption caused by the isolated design of the conventional catalytic cracking device and a catalytic stable gasoline hydrofining device, the invention provides a hydrofining process of catalytic cracking crude gasoline, which integrates gasoline stability and directly sends catalytic crude gasoline to hydrofining.
The purpose of the invention is realized by the following technical scheme:
a hydrofining process of catalytic cracking crude gasoline is improved on the basis of the process flow of the original catalytic cracking device and the original gasoline hydrofining device as follows:
crude gasoline at the top of the main fractionating tower is changed from the original crude gasoline entering an absorption tower to the crude gasoline directly entering a catalytic gasoline hydrofining device, and the flow of other pipelines is unchanged.
Further, the process of the catalytic cracking naphtha hydrofining process comprises the following specific steps:
reaction oil gas from a reaction unit enters the lower part of a herringbone baffle of a main fractionating tower 1, is in countercurrent contact with circulating slurry oil flowing downwards from the upper part of the herringbone baffle from bottom to top, enters a fractionating part after being washed and desuperheated, and is fractionated to obtain recycle oil, diesel oil, crude gasoline and gas in turn, and excess heat is taken away by a tower top cooling system, a top circulating reflux, a first-middle-segment reflux and slurry oil circulating reflux;
The gas at the top of the main fractionating tower 1 is cooled to about 40 ℃ by a fractionating tower top oil-gas-hot water heat exchanger 2, an air cooler 3 and a circulating water cooler 4, enters a gas-liquid separation tank 5, is separated to obtain non-condensable gas and condensed crude gasoline, the non-condensable gas is compressed by a rich gas compressor 6/1, is mixed with the gas at the top of a stripping tower 38, is cooled by a compressor primary outlet circulating water cooler 10, is sent to a compressor primary outlet gas-liquid separation tank 11, is separated to obtain non-condensable gas and tank bottom oil, is compressed to 1.3MPag by a rich gas compressor 6/2, is mixed with the gas at the top of a desorption tower 19, is cooled by an air cooler 13, is mixed with the bottom oil of an absorption tower 17 pumped by a bottom oil pump 18 and the bottom oil of the compressor primary outlet gas-liquid separation tank 11 pumped by a tank bottom oil pump 12, and is cooled by a circulating water cooler 14, and then enters a condensed oil tank 15 at 40 ℃; the condensed crude gasoline is pressurized by a crude gasoline pump 7 and then sent to a reactant-raw material heat exchanger 44 of the gasoline hydrofining device;
the side diesel automatically flows into a diesel stripping tower 8 from the 16 th layer of the main fractionating tower 1, is extracted by a lean diesel pump 9 after being stripped, and then is divided into product diesel and lean diesel, and the lean diesel is further cooled and then is sent to the top of a reabsorption tower 36;
the operation pressure of the absorption tower 17 is 1.2MPag, gas from the condensation oil tank 15 enters the lower part, stable gasoline as a supplementary absorbent from the stabilizing tower 24 enters the top part, and the gas and the stable gasoline are in countercurrent contact to finish mass transfer and heat transfer, and an intermediate circulating water cooler helps to realize heat balance; the lean gas coming out from the top of the absorption tower 17 is sent to the bottom of a reabsorption tower 36 and is in countercurrent contact with the lean diesel oil to absorb the C and the C carried by the lean gas 3Discharging a product dry gas from the top of the tower, and feeding diesel rich at the bottom of the tower into a main fractionating tower 1;
condensed oil is pressurized from a condensed oil tank 15 through a feed pump 16 of a desorption tower, then exchanges heat with stable gasoline through a condensed oil-stable gasoline heat exchanger 32 to 50 ℃ and enters the upper part of a desorption tower 19, reboilers 20 and 21 at the bottom of the desorption tower are respectively supplied with heat by reflux in a first main distillation tower and steam of 1.0MPa, a reboiler 30 at the middle of the desorption tower is supplied with heat by stable gasoline secondarily, deethanized gasoline at the bottom of the desorption tower 19 is pressurized through a feed pump 22 of the stabilization tower and then exchanges heat with the stable gasoline through a deethanized gasoline-stable gasoline heat exchanger 23 and then enters a stabilization tower 24, a reboiler 29 at the bottom of the stabilization tower is supplied with heat by reflux in a second main distillation tower, LPG light components are distilled from the top of the tower and are condensed and cooled to 40 ℃ through a cooler 25 of the stabilization tower to enter a gas-liquid separation tank 26 at the top of the stabilization tower, one part of liquefied gas is pressurized through a reflux pump 27 at the top of the stabilization tower as cold reflux, and the other part of the liquefied gas is pressurized and sent as a product outlet device through a liquefied gas product pump 28; the stable gasoline at the bottom of the tower is sequentially cooled to 40 ℃ by a deethanized gasoline-stable gasoline heat exchanger 23, a middle reboiler 30 of a desorption tower, a deoxygenated water heat exchanger 31, a condensed oil-stable gasoline heat exchanger 32, an air cooler 33 and a circulating water cooler 34, the pressure is increased by a supplementary absorbent pump 35 and then the stable gasoline is divided into two paths, one path is used as a supplementary absorbent and is sent to an absorption tower 17, and the other path is used as raw material stable gasoline and is sent to a gasoline hydrofining device;
Raw material stabilized gasoline, crude gasoline from a main fractionating tower 1 and external hydrogen are mixed and sequentially enter a reactant-raw material heat exchanger 44 and a hydrofining raw material heating furnace 43, the mixture enters a pre-hydrogenation reactor 37 after heat exchange and temperature rise, the generated reactant enters a stripping tower 38 after heat exchange through the reactant-raw material heat exchanger 44, light components are distilled out from the tower top, the light components are condensed and cooled through a stripping tower cooler 39 and then enter a stripping tower top gas-liquid separation tank 40, non-condensable gas and liquid are separated, the non-condensable gas is directly sent to a compressor primary outlet circulating water cooler 10 through a pipeline, the liquid is pressurized through a stripping tower top reflux pump 41 and then serves as cold reflux, refined gasoline is produced at the tower bottom, and a stripping tower bottom reboiler 42 is heated by 1.0MPa steam.
Compared with the prior art, the invention has the following advantages and beneficial effects:
(1) the crude gasoline is directly fed into hydrofining, so that the catalytic absorption stabilizing system does not process the crude gasoline, only processes rich gas, and the treatment capacity, energy consumption and energy consumption quality are greatly reduced;
(2) less than or equal to C brought into hydrofining device along with crude gasoline4The components do not contribute to the hydroprocessing, they will follow the H2S、NH3The acidic components are pulled out from the top of the stripping tower together and returned to catalytic refining along the original flow, thereby ensuring the quality of the gasoline of the product; the quality of the LPG product is continuously ensured by the catalytic stabilizer;
(3) A small amount of gasoline which is stably absorbed and carried along with rich gas is continuously distilled from the bottom of the stable tower, and is mixed with crude gasoline to be hydrogenated after heat exchange, so that the material balance of a combined device is not changed;
(4) most functions of the catalytic stabilizer for producing stable gasoline are skillfully transferred to a stripping tower of a hydrogenation device by a crude gasoline direct refining process, so that repeated distillation of the gasoline is avoided, which is the key reason of low energy consumption of a combined device and has remarkable innovative significance.
Drawings
FIG. 1 is a process flow diagram of a comparative example of the present invention (existing 480 ten thousand ton/year catalytic cracker and 200 ten thousand ton/year gasoline hydrorefining unit).
FIG. 2 is a process flow diagram of an embodiment of the present invention, wherein the numbers are as follows: 1-main fractionation column; 2-fractionating tower top oil gas-hot water heat exchanger; 3-an air cooler; 4-a circulating water cooler; 5-a gas-liquid separation tank; 6-rich gas compressor (6/1 and 6/2); 7-crude gasoline pump; 8-diesel stripper column; 9-a lean diesel pump; 10-a compressor first-stage outlet circulating water cooler; 11-a gas-liquid separation tank at the first-stage outlet of the compressor; 12-a tank bottom oil pump; 13-an air cooler; 14-a circulating water cooler; 15-condensation oil tank; 16-desorber feed pump; 17-an absorption column; 18-a bottom oil suction pump; 19-a desorber; 20-a reboiler at the bottom of the desorption tower; 21-a reboiler at the bottom of the desorption tower; 22-stabilizer column feed pump; 23-deethanized gasoline-stabilized gasoline heat exchanger; 24-a stabilizer column; 25-a stabilizer tower cooler; 26-a gas-liquid separation tank at the top of the stabilizing tower; 27-a stabilizer overhead reflux pump; 28-liquefied gas product pump; 29-a stabilizer column bottom reboiler; 30-a stripper column intermediate reboiler; 31-a deoxygenated water heat exchanger; 32-condensed oil-stabilized gasoline heat exchanger; 33-an air cooler; 34-a circulating water cooler; 35-make-up absorbent pump; 36-a reabsorption column; 37-a pre-hydrogenation reactor; 38-stripper column; 39-stripper cooler; 40-a gas-liquid separation tank at the top of the stripping tower; 41-stripping column top reflux pump; 42-a stripper bottoms reboiler; 43-hydrofining raw material heating furnace; 44-reactant-feedstock heat exchanger.
Detailed Description
The present invention will be described in further detail with reference to examples and drawings, but the embodiments of the present invention are not limited thereto.
Those who do not specify specific conditions in the examples of the present invention follow conventional conditions or conditions recommended by the manufacturer. The raw materials, reagents and the like which are not indicated for manufacturers are all conventional products which can be obtained by commercial purchase.
Comparative example
The comparative example is a conventional catalytic cracking fractionation and absorption stabilization system, and the process flow diagram is shown in FIG. 1. The specific process is as follows:
reaction oil gas from a reaction unit enters the lower part of a herringbone baffle of a main fractionating tower 1, is in countercurrent contact with 275 ℃ circulating slurry oil flowing downwards from the upper part of the herringbone baffle from bottom to top, enters a fractionating part after being washed and desuperheated, and sequentially obtains recycle oil, diesel oil, crude gasoline and gas through fractionation, and excess heat is taken away by a tower top cooling system, a top circulating reflux, a middle-section reflux and slurry oil circulating reflux;
the gas at the top of the main fractionating tower 1 is cooled to 40 ℃ through a fractionating tower top oil gas-hot water heat exchanger 2, an air cooler 3 and a circulating water cooler 4, enters a gas-liquid separation tank 5, is separated into non-condensable gas and condensed crude gasoline, the non-condensable gas enters a rich gas compressor 6/1, mixed with the top gas of the stripping tower 38, cooled by a compressor primary outlet circulating water cooler 10, sent to a compressor primary outlet gas-liquid separation tank 11, separated from non-condensed steam and tank bottom oil, compressed to 1.3MPag by a rich gas compressor 6/2, mixed with the top gas of a desorption tower 19, cooled by an air cooler 13, mixing with bottom oil of the absorption tower 17 pumped by a bottom oil suction pump 18 and bottom oil of a gas-liquid separation tank 11 at a first-stage outlet of a compressor pumped by a tank bottom oil pump 12, cooling by a circulating water cooler 14, feeding the mixture into a condensation oil tank 15 at 40 ℃, and pressurizing condensed crude gasoline by a crude gasoline pump 7 and then sending the compressed crude gasoline to the absorption tower 17;
The side diesel automatically flows into a diesel stripping tower 8 from the 16 th layer of the main fractionating tower 1, is extracted by a lean diesel pump 9 after being stripped, and then is divided into product diesel and lean diesel, and the lean diesel is further cooled and then is sent to the top of a reabsorption tower 36;
the operation pressure of the absorption tower 17 is 1.2MPag, gas from the condensation oil tank 15 enters the lower part, stable gasoline as a supplementary absorbent from the stabilizing tower enters the top part, the stable gasoline and the stable gasoline are in countercurrent contact to finish mass transfer and heat transfer, and an intermediate circulating water cooler helps to realize heat balance; the lean gas coming out from the top of the absorption tower 17 is sent to the bottom of a reabsorption tower 36 and is in countercurrent contact with the lean diesel oil to absorb the C and the C carried by the lean gas3Discharging dry gas from the top of the tower, and feeding diesel rich at the bottom of the tower into a main fractionating tower 1;
condensed oil is pressurized from a condensed oil tank 15 through a feed pump 16 of a desorption tower, then exchanges heat with stable gasoline through a condensed oil-stable gasoline heat exchanger 32 to 50 ℃ and enters the upper part of a desorption tower 19, reboilers 20 and 21 at the bottom of the desorption tower exchange heat with the stable gasoline through reflux in a first main fractionating tower and steam of 1.0MPa respectively, a reboiler 30 in the middle of the desorption tower exchanges heat with the stable gasoline through secondary heat supply of the stable gasoline, deethanized gasoline at the bottom of the desorption tower 19 is pressurized through a feed pump 22 of the stabilization tower and then exchanges heat with the stable gasoline through a deethanized gasoline-stable gasoline heat exchanger 23 and then enters a stabilization tower 24, a reboiler 29 at the bottom of the stabilization tower exchanges heat through reflux in a second main fractionating tower, LPG light components are distilled from the top of the tower and condensed and cooled to 40 ℃ through a cooler 25 of the stabilization tower and enter a gas-liquid separation tank 26 at the top of the stabilization tower, a part of the liquefied gas is pressurized through a reflux pump 27 at the top of the stabilization tower as cold reflux, and a part of the liquefied gas is pressurized and sent as a product outlet device through a liquefied gas product pump 28; the stable gasoline at the bottom of the tower sequentially passes through a deethanized gasoline-stable gasoline heat exchanger 23, a desorption tower intermediate reboiler 30, a deoxygenated water heat exchanger 31, a condensed oil-stable gasoline heat exchanger 32, an air cooler 33 and a circulating water cooler 34 to be cooled to 40 ℃, and is pressurized by a supplementary absorbent pump 35 and then divided into two paths, wherein one path is used as a supplementary absorbent and sent to the absorption tower 17, and the other path is used as raw material stable gasoline and sent to a gasoline hydrogenation device;
Raw material stabilized gasoline and external hydrogen are mixed and sequentially enter a reactant-raw material heat exchanger 44 and a hydrofining raw material heating furnace 43, the mixture enters a pre-hydrogenation reactor 37 after heat exchange and temperature rise, the generated reactant enters a stripping tower 38 after heat exchange through the reactant-raw material heat exchanger 44, light components are distilled off from the top of the tower, the light components are condensed and cooled through a stripping tower cooler 39 and then enter a stripping tower top gas-liquid separation tank 40, non-condensable gas and liquid are separated, the non-condensable gas is directly sent to a compressor primary outlet circulating water cooler 10 through a pipeline, the liquid is pressurized through a stripping tower top reflux pump 41 and then serves as cold reflux, gasoline is generated at the bottom of the tower, and a reboiler 42 at the bottom of the stripping tower supplies heat through 1.0MPa steam.
Examples
The embodiment of the combined energy-saving process flow of the catalytic cracking device and the gasoline hydrogenation device is an improvement on the original catalytic cracking device and process flow as follows:
the crude gasoline at the top of the main fractionating tower is directly sent to a gasoline hydrogenation device instead of the original absorption tower, and the flow of other pipelines is unchanged.
The process flow diagram is shown in fig. 2, and the specific process flow is as follows:
reaction oil gas from a reaction unit enters the lower part of a herringbone baffle of a main fractionating tower 1, is in countercurrent contact with circulating slurry oil flowing downwards from the upper part of the herringbone baffle from bottom to top, enters a fractionating part after being washed and desuperheated, and is fractionated to obtain recycle oil, diesel oil, crude gasoline and gas in turn, and excess heat is taken away by a tower top cooling system, a top circulating reflux, a first-middle-segment reflux and slurry oil circulating reflux;
The gas at the top of the main fractionating tower 1 is cooled to about 40 ℃ by a fractionating tower top oil-gas-hot water heat exchanger 2, an air cooler 3 and a circulating water cooler 4, enters a gas-liquid separation tank 5, is separated to obtain non-condensable gas and condensed crude gasoline, the non-condensable gas is compressed by a rich gas compressor 6/1, is mixed with the gas at the top of a stripping tower 38, is cooled by a compressor primary outlet circulating water cooler 10, is sent to a compressor primary outlet gas-liquid separation tank 11, is separated to obtain non-condensable gas and tank bottom oil, is compressed to 1.3MPag by a rich gas compressor 6/2, is mixed with the gas at the top of a desorption tower 19, is cooled by an air cooler 13, is mixed with the bottom oil of an absorption tower 17 pumped by a bottom oil pump 18 and the bottom oil of the compressor primary outlet gas-liquid separation tank 11 pumped by a tank bottom oil pump 12, and is cooled by a circulating water cooler 14, and then enters a condensed oil tank 15 at 40 ℃; the condensed crude gasoline is pressurized by a crude gasoline pump 7 and then sent to a reactant-raw material heat exchanger 44 of the gasoline hydrofining device;
the side diesel automatically flows into a diesel stripping tower 8 from the 16 th layer of the main fractionating tower 1, is extracted by a lean diesel pump 9 after stripping, and then is divided into product diesel and lean diesel, and the lean diesel is further cooled and then is sent to the top of a reabsorption tower 36;
the operation pressure of the absorption tower 17 is 1.2MPag, gas from the condensation oil tank 15 enters the lower part, stable gasoline as a supplementary absorbent from the stabilizing tower 24 enters the top part, and the gas and the stable gasoline are in countercurrent contact to finish mass transfer and heat transfer, and an intermediate circulating water cooler helps to realize heat balance; the lean gas coming out from the top of the absorption tower 17 is sent to the bottom of a reabsorption tower 36 and is in countercurrent contact with the lean diesel oil to absorb the C or more carried by the lean gas 3Discharging a product dry gas from the top of the tower, and feeding diesel rich at the bottom of the tower into a main fractionating tower 1;
condensed oil is pressurized from a condensed oil tank 15 through a feed pump 16 of a desorption tower, then exchanges heat with stable gasoline through a condensed oil-stable gasoline heat exchanger 32 to 50 ℃ and enters the upper part of a desorption tower 19, reboilers 20 and 21 at the bottom of the desorption tower are respectively supplied with heat by reflux in a first main distillation tower and steam of 1.0MPa, a reboiler 30 at the middle of the desorption tower is supplied with heat by stable gasoline secondarily, deethanized gasoline at the bottom of the desorption tower 19 is pressurized through a feed pump 22 of the stabilization tower and then exchanges heat with the stable gasoline through a deethanized gasoline-stable gasoline heat exchanger 23 and then enters a stabilization tower 24, a reboiler 29 at the bottom of the stabilization tower is supplied with heat by reflux in a second main distillation tower, LPG light components are distilled from the top of the tower and are condensed and cooled to 40 ℃ through a cooler 25 of the stabilization tower to enter a gas-liquid separation tank 26 at the top of the stabilization tower, one part of liquefied gas is pressurized through a reflux pump 27 at the top of the stabilization tower as cold reflux, and the other part of the liquefied gas is pressurized and sent as a product outlet device through a liquefied gas product pump 28; the stable gasoline at the bottom of the tower is sequentially cooled to 40 ℃ by a deethanized gasoline-stable gasoline heat exchanger 23, a middle reboiler 30 of a desorption tower, a deoxygenated water heat exchanger 31, a condensed oil-stable gasoline heat exchanger 32, an air cooler 33 and a circulating water cooler 34, the pressure is increased by a supplementary absorbent pump 35 and then the stable gasoline is divided into two paths, one path is used as a supplementary absorbent and is sent to an absorption tower 17, and the other path is used as raw material stable gasoline and is sent to a gasoline hydrofining device;
Raw material stabilized gasoline, crude gasoline from a main fractionating tower 1 and external hydrogen are mixed and sequentially enter a reactant-raw material heat exchanger 44 and a hydrofining raw material heating furnace 43, the mixture enters a pre-hydrogenation reactor 37 after heat exchange and temperature rise, the generated reactant enters a stripping tower 38 after heat exchange through the reactant-raw material heat exchanger 44, light components are distilled out from the tower top, the light components are condensed and cooled through a stripping tower cooler 39 and then enter a stripping tower top gas-liquid separation tank 40, non-condensable gas and liquid are separated, the non-condensable gas is directly sent to a compressor primary outlet circulating water cooler 10 through a pipeline, the liquid is pressurized through a stripping tower top reflux pump 41 and then serves as cold reflux, refined gasoline is produced at the tower bottom, and a stripping tower bottom reboiler 42 is heated by 1.0MPa steam.
The main operation of the comparative examples and examples will be described below by taking a 480 ten thousand ton/year catalytic cracking unit and a 200 ten thousand ton/year gasoline hydrogenation unit as examples, and the quality indexes of the products are controlled to be constant in both the comparative examples and the examples.
Table 1 shows the rich gas compressor operation of the comparative example and the example.
Table 1 comparative and example rich gas compressor operating conditions
Figure BDA0002650980440000081
Figure BDA0002650980440000091
Based on isentropic compression efficiency 75%.
Table 2 shows the rich gas cooling duty of the comparative example and the example.
TABLE 2 comparative and example rich gas cooling duty
Figure BDA0002650980440000092
Table 3 is the make-up absorbent flow rates for the comparative examples and examples.
Table 3 comparative and example make-up absorbent flow rates
Figure BDA0002650980440000093
Table 4 shows the stripper reboiler runs for the comparative and example.
Table 4 comparative and example stripper reboiler runs
Figure BDA0002650980440000094
Table 5 shows the comparative example and example stabilizer column energy consumption.
Table 5 comparative and example energy consumption behavior of the stabilizer column
Figure BDA0002650980440000095
Figure BDA0002650980440000101
Table 6 shows the operation of the heat exchanger of the gasoline hydrogenation apparatus of the comparative example and example.
Table 6 comparative and example heat exchanger operation of gasoline hydrogenation apparatus
Figure BDA0002650980440000102
Table 7 is the stripper run for the comparative example and example.
Table 7 comparative and example stripper energy consumption runs
Figure BDA0002650980440000103
As can be seen from tables 1 to 7, the comparative ratios, examples:
1. the power consumption of the rich gas compressor is increased by 194.0kw and 4.0 percent, and the steam consumption of the driving turbine is increased by 0.4t/h under 3.5MPa
2. Increase of cooling load of rich gas 196.9X 104kcal/h, increase amplitude of 13.6%, according to circulating water temperature drop 6 ℃, consume circulating water 328.2 t/h;
3. the supplement absorbent is increased by 53 t/h;
4. reboiling load reduction of desorption tower 541.5 x 104kcal/h (1.0 MPa steam 10.2t/h), reduced amplitude 32.9%; the temperature of the bottom of the desorption tower is 100.2 ℃, the temperature is reduced by 16.2 ℃, and 0.35MPa steam (the saturation temperature is 148 ℃) can be used as a heat source;
5. Stabilized column reboil duty reduction 340.4 x 104kcal/h (3.5 MPa steam 6.4t/h), reduced amplitude 15.2%; stabilizing the bottom temperature of the tower at 131.0 deg.C, reducing the temperature by 42.0 deg.C, and changing to 1.0MPa steam (saturation temperature of 184.1 deg.C) as heat source; cooling load reduction of 488.6 x 10 for stabilizing tower4kcal/h, reduced amplitude 20.1Percent, cooling the circulating water by 6 ℃ and consuming 814.3t/h of the circulating water;
6. the load of the hydrofining raw material heating furnace is increased by 152.4 multiplied by 104kcal/h (calculated according to the furnace efficiency of 90 percent, the standard fuel oil consumption is 0.17t/h), and the amplification is 15.3 percent;
7. stripper reboil duty increase 393.4 x 104kcal/h (equivalent weight 1.0MPa steam 7.4t/h), reduced amplitude 57.2%; stripper cooling duty increase 448 x 104kcal/h, increase amplitude 68.5%, according to circulating water temperature drop 6 ℃, consume circulating water 746.7 t/h;
the total embodiment is calculated based on steam unit price of 3.5MPa of 300 yuan/t, steam unit price of 1.0MPa of 250 yuan/t, steam unit price of 0.35MPa of 200 yuan/t, standard fuel oil of 3000 yuan/t and circulating water treatment cost of 0.2 yuan/t, and the annual operation of the device is 8400 hours, so that the energy consumption cost of the embodiment is reduced by 3303.1 ten thousand yuan/year compared with that of the comparative embodiment.
The above embodiments are preferred embodiments of the present invention, but the present invention is not limited to the above embodiments, and any other changes, modifications, substitutions, combinations, and simplifications which do not depart from the spirit and principle of the present invention should be construed as equivalents thereof, and all such changes, modifications, substitutions, combinations, and simplifications are intended to be included in the scope of the present invention.

Claims (1)

1. A catalytic cracking crude gasoline hydrorefining process is characterized in that the process flow of the original catalytic cracking device and the original gasoline hydrorefining device is improved as follows:
crude gasoline at the top of the main fractionating tower is changed from the original crude gasoline entering an absorption tower to the crude gasoline directly entering a catalytic gasoline hydrofining device, and the flow of other pipelines is unchanged;
the process flow of the catalytic cracking device and the gasoline hydrofining device is as follows:
reaction oil gas from a reaction unit enters the lower part of a herringbone baffle of a main fractionating tower (1), is in countercurrent contact with circulating slurry oil flowing downwards from the upper part of the herringbone baffle from bottom to top, enters a fractionating part after being washed and desuperheated, and sequentially obtains recycle oil, diesel oil, crude gasoline and gas through fractionation, and excess heat is taken away by a tower top cooling system, a top circulating reflux, a middle-section reflux and slurry oil circulating reflux;
the gas at the top of the main fractionating tower (1) is cooled to 40 ℃ by a fractionating tower top oil-gas-hot water heat exchanger (2), an air cooler (3) and a circulating water cooler (4), enters a gas-liquid separation tank (5), is separated into non-condensable gas and condensed crude gasoline, the non-condensable gas is mixed with the gas at the top of a stripping tower (38) after being compressed by a rich gas compressor (6/1), is cooled by a compressor primary outlet circulating water cooler (10), is sent to a compressor primary outlet gas-liquid separation tank (11), is separated into non-condensable gas and tank bottom oil, is compressed to 1.3MPaG by a rich gas compressor (6/2), is mixed with the gas at the top of a desorption tower (19), is cooled by an air cooler (13), and is mixed with the oil at the bottom of an absorption tower (17) pumped by a bottom oil pump (18) and the oil at the bottom of the compressor primary outlet gas-liquid separation tank (11) pumped by a tank bottom oil pump (12), after being cooled by a circulating water cooler (14), the mixture enters a condensation oil tank (15) at the temperature of 40 ℃; the condensed crude gasoline is pressurized by a crude gasoline pump (7) and then is sent to a reactant-raw material heat exchanger (44) of a gasoline hydrofining device;
The side diesel automatically flows into a diesel stripping tower (8) from the 16 th layer of the main fractionating tower (1), is extracted by a lean diesel pump (9) after being stripped, and then is divided into product diesel and lean diesel, and the lean diesel is further cooled and then is sent to the top of a reabsorption tower (36);
the operation pressure of the absorption tower (17) is 1.2MPaG, gas from a condensation oil tank (15) enters the lower part, stable gasoline serving as a supplementary absorbent from a stabilizing tower (24) enters the top part, and the gas and the stable gasoline are in countercurrent contact to finish mass transfer and heat transfer, and an intermediate circulating water cooler helps to realize heat balance; the lean gas coming out from the top of the absorption tower (17) is sent to the bottom of a reabsorption tower (36) and is in countercurrent contact with the lean diesel oil to absorb the C or more carried by the lean diesel oil3The components, namely, the product dry gas is discharged from the top of the tower, and the rich diesel oil at the bottom of the tower is fed into a main fractionating tower (1);
condensed oil is pressurized from a condensed oil tank (15) through a feed pump (16) of a desorption tower, then exchanges heat with stable gasoline through a condensed oil-stable gasoline heat exchanger (32) and enters the upper part of the desorption tower (19) at 50 ℃, reboilers (20) and (21) at the bottom of the desorption tower respectively exchange heat through reflux in a first main fractionating tower and steam of 1.0MPa, a reboiler (30) in the middle of the desorption tower secondarily supplies heat through stable gasoline, deethanized gasoline at the bottom of the desorption tower (19) is pressurized through a feed pump (22) of the stabilization tower, then exchanges heat with stable gasoline through a deethanized gasoline-stable gasoline heat exchanger (23) and enters a stabilization tower (24), a reboiler (29) at the bottom of the stabilization tower supplies heat through reflux in a second main fractionating tower, LPG light components are distilled from the top of the tower and condensed and cooled to 40 ℃ through a cooler (25) of the stabilization tower to enter a gas-liquid separation tank (26) at the top of the stabilization tower, and a part of liquefied gas is pressurized as cold reflux through a reflux pump (27) at the top of the stabilization tower, one part of the liquefied gas is pressurized by a liquefied gas product pump (28) and is taken as a product delivery device; the stable gasoline at the bottom of the tower is sequentially cooled to 40 ℃ by a deethanized gasoline-stable gasoline heat exchanger (23), a middle reboiler (30) of a desorption tower, a deoxygenated water heat exchanger (31), a condensed oil-stable gasoline heat exchanger (32), an air cooler (33) and a circulating water cooler (34) and is subjected to pressure increase by a supplementary absorbent pump (35) and then divided into two paths, wherein one path is used as a supplementary absorbent and sent to an absorption tower (17), and the other path is used as raw material stable gasoline and sent to a gasoline hydrofining device;
Raw material stabilized gasoline, crude gasoline from a main fractionating tower (1) and external hydrogen are mixed and sequentially enter a reactant-raw material heat exchanger (44) and a hydrofining raw material heating furnace (43), the mixture enters a pre-hydrogenation reactor (37) after heat exchange and temperature rise, the generated reactant enters a stripping tower (38) after heat exchange through the reactant-raw material heat exchanger (44), light components are distilled off from the tower top, the light components are condensed and cooled through a stripping tower cooler (39) and then enter a stripping tower top gas-liquid separation tank (40), non-condensable gas and liquid are separated, the non-condensable gas is directly sent to a compressor primary outlet circulating water cooler (10) through a pipeline, the liquid is pressurized through a stripping tower top reflux pump (41) and then serves as cold reflux, refined gasoline is produced at the tower bottom, and a stripping tower bottom reboiler (42) is heated by 1.0MPa steam.
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