Absorption stabilizing system for crude oil processing

Abstract

The utility model relates to an absorption stabilizing system for crude oil processing, which adopts a two-stage condensation technology at the top of a main fractionating tower, so that the content of C4-component dissolved in primary oil can be effectively reduced, C3 + component can be more effectively absorbed, and the absorption effect and the dry gas quality are further improved; and moreover, the primary oil in the temperature interval is more suitable for returning to the tower as the tower top hot reflux of the main fractionating tower, so that the operation flexibility of the main fractionating tower is improved. Two products are respectively extracted from the lower part of the stabilization tower, and the tower bottom is extracted as a supplementary absorbent to be sent to the absorption tower to participate in circulation; and the middle and lower part of the stabilizing tower is provided with a side-draw product-stabilized gasoline stream. According to the method, all components can be clearly cut, and the absorption effect and the product value income are improved. A cold water circulation system is introduced, refrigerant water is produced by using low-temperature heat resources, and the stream related to the absorption reaction is adjusted to a more favorable low-temperature condition, so that the reaction effects of the absorption and re-absorption tower are improved, and the escape of C3 + components is reduced.

Description

TECHNICAL FIELD

[0001] The utility model relates to crude oil processing process technical field, specifically points to a kind of absorption stabilizing system of crude oil processing. BACKGROUND

[0002] Absorption stabilizing system is the important component part of catalytic cracking, delayed coking, hydrocracking and other crude oil processing devices in refinery. Its main equipment includes absorption tower, desorption tower, reabsorption tower and stabilizing tower etc., and main task is used for processing the crude gasoline and rich gas from the oil-gas separator of fractionating column top, separates dry gas (C1 and C2), and recovers liquefied gas (C3 and C4) and stable gasoline (C5+) qualified products.

[0003] The process flow of absorption stabilizing system is usually that oil gas from anti-re system enters main fractionating column, and product is generated from top to bottom in turn: tower top oil gas, light diesel oil, backfiring oil and oil slurry. Among them, tower top oil gas obtains rich gas, sour water and crude gasoline through oil-gas separation tank, and rich gas is sent to absorption stabilizing system for further separation after being pressurized by compressor, and crude gasoline is sent to absorption tower as absorbent;The light diesel oil after stripping is partly sent to reabsorption tower as reabsorbent, and the other part is sent out of device as product. After being pressurized, rich gas, absorption tower bottom oil, desorption tower top gas and sour water are mixed into three-phase separation tank before absorption tower after air cooling water cooling heat exchange, and gas-liquid separation is carried out, and the separated gas enters absorption tower, and contacts with absorbent crude gasoline and supplementary absorbent, and C3 and above components are absorbed into liquid phase. Absorption tower top gas enters reabsorption tower, and contacts with reabsorbent (i.e. light diesel oil from main fractionating column), and further absorbs C3 and above components, and reabsorption tower top dry gas and tower bottom rich absorption oil are obtained, and rich absorption oil is recycled to main fractionating column, and the oil phase separated by three-phase tank enters desorption tower, and C2 and below light components dissolved in oil phase are desorbed, and desorption tower bottom oil enters stabilizing tower, and desorption tower top gas is recycled to three-phase separation tank before absorption tower. Stable tower top oil gas is extracted, and tower top liquid phase product is liquefied petroleum gas (LPG). The discharge from stabilizing tower bottom is divided into two streams, one is as stable gasoline product and is sent out of device, and the other is as supplementary absorbent and is sent to absorption tower.

[0004] However, the existing catalytic absorption (stabilizing) system often has the following problems:

[0005] (1) It is easy to cause unqualified dry gas quality. When the ambient temperature is relatively high, it is not conducive to the progress of absorption reaction, which will cause more C3 and above components to enter dry gas, and then cause loss along with dry gas into gas system;

[0006] (2)Easy to cause the LPG and stable gasoline cut of stable column is not clear enough. It is easy to have C5+ component content in LPG too high, and too much C4- component into stable gasoline, thereby causing high value component mixed into low value product, stable gasoline vapor pressure too high phenomenon;

[0007] (3)Easy to cause unnecessary energy consumption loss. If the desorption tower is over desorbed, it is easy to increase the C3C4 component circulation in the absorption and desorption tower, and further increase the process energy consumption.

[0008] Therefore, for the current crude oil processing absorption stabilization system, further improvement is needed. Practical new type content

[0009] The technical problem to be solved by the present application is to provide a crude oil processing absorption stabilization system which can effectively improve the absorption effect and thereby improve the dry gas quality, clearly cut each component and thereby improve the product quality, and obtain maximum economic value.

[0010] The technical scheme adopted by the present application to solve the above technical problem is:

[0011] A crude oil processing absorption stabilization system, comprising:

[0012] A main fractionating column, provided with a reaction oil gas inlet at the side, an oil slurry outlet at the bottom, and an oil gas outlet at the top;

[0013] A primary knock-out drum, arranged downstream of the main fractionating column, for primary knock-out of oil gas output from the top of the main fractionating column; a branch pipeline for sending part of the liquid phase back to the main fractionating column is connected downstream of the primary knock-out drum;

[0014] A water segregator, arranged downstream of the primary knock-out drum, for knock-out treatment of part of the liquid phase output from the primary knock-out drum;

[0015] A secondary knock-out drum, for secondary knock-out of gas phase output from the primary knock-out drum;

[0016] An absorption tower, provided with an inlet for input of primary crude gasoline obtained by the water segregator and secondary crude gasoline obtained by the secondary knock-out drum, an outlet at the top for output of tower top gas, and an outlet at the bottom for output of tower bottom oil;

[0017] A re-absorption tower, provided with an inlet for input of tower top gas output from the absorption tower, an outlet at the top for output of dry gas, and an outlet at the bottom for output of rich absorption oil, which is communicated with the inlet of the main fractionating column;

[0018] A desorption tower, provided with an inlet for input of liquid phase, an outlet at the top for output of tower top gas, and an outlet at the bottom for output of tower bottom oil.

[0019] A stabilizing tower is provided downstream of the desorption tower, and is provided with an inlet for input of the desorption tower bottom oil, an outlet at the top for output of the tower top dry gas, an outlet at the bottom for output of the tower bottom oil, and an outlet at the side for output of the product gasoline.

[0020] Preferably, a hot water heat exchanger is provided between the main fractionating tower and the primary knock-out drum, for heat exchange of the oil gas from the main fractionating tower top to the primary knock-out drum.

[0021] Preferably, a branch pipeline is connected between the primary knock-out drum and the water trap, for input of the liquid phase from the primary knock-out drum bottom to the main fractionating tower.

[0022] Preferably, a first coolant water water cooler is provided between the water trap and the absorption tower, for heat exchange of the liquid phase output from the water trap.

[0023] Preferably, an air cooler and a second coolant water water cooler are provided between the primary knock-out drum and the secondary knock-out drum, and the top of the secondary knock-out drum is provided with a rich gas primary compressor for further processing of the rich gas output from the secondary knock-out drum, a compressor inter-stage coolant water water cooler, and a rich gas secondary compressor, downstream of which is provided an air cooler for heat exchange of the rich gas, compressor condensed oil, sour water, and desorption tower top gas, and downstream of the air cooler is a third coolant water water cooler for cooling of the absorption tower bottom oil and the above-mentioned mixture (rich gas, compressor condensed oil, sour water, and desorption tower top gas), downstream of the third coolant water water cooler is provided a three-phase knock-out drum, the top of which is provided with an outlet for output of the gas phase to the absorption tower, and the bottom of which is provided with a desorption tower feed heater for heating of the liquid phase output therefrom, which desorption tower feed heater is connected to the inlet of the desorption tower.

[0024] Preferably, a first stabilizing tower feed heat exchanger and a second stabilizing tower feed heat exchanger are provided on the feed pipeline of the desorption tower to the stabilizing tower, a first desorption tower middle section heat exchanger and a second desorption tower middle section heat exchanger are provided on the side of the desorption tower, and a side product output pipeline is provided on the side of the stabilizing tower, which side product output pipeline, after merging with the product gasoline output pipeline at the bottom of the stabilizing tower, is connected in turn to the first stabilizing tower feed heat exchanger, the first desorption tower middle section heat exchanger, and the inlet of the desorption tower feed heater, and the desorption tower feed heater has an outlet for output of the product stabilizing gasoline.

[0025] Preferably, the circulating gasoline at the bottom of the stabilizing tower is input in turn to a second stabilizing tower feed heat exchanger, a second desorption tower middle section heat exchanger, and a hot water / air cooling heat exchanger, downstream of which is provided a fourth coolant water water cooler, and the absorption tower is provided with an inlet for input of the circulating gasoline output from the fourth coolant water water cooler.

[0026] Preferably, the side of the absorption tower is provided with two middle section reflux pipelines, and the fifth coolant water water-cooler and the sixth coolant water water-cooler are arranged on the two middle section reflux pipelines respectively.

[0027] Preferably, the downstream of the main fractionating tower is provided with a light diesel oil stripping tower, and the top of the light diesel oil stripping tower is provided with a pipeline for sending gas phase to the top of the main fractionating tower, and the bottom of the light diesel oil stripping tower is provided with an outlet for outputting liquid phase.

[0028] Preferably, the bottom of the light diesel oil stripping tower is further provided with a heat exchanger for heat exchange of liquid phase, and the bottom of the light diesel oil stripping tower is provided with a conveying pipeline for conveying the heat-exchanged part of the light diesel oil to the reabsorption tower.

[0029] Compared with the prior art, the utility model has the advantages that: the utility model adopts two-stage condensation technology to form two-stage absorbents on the top of the main fractionating tower, and the use positions are improved according to the respective component characteristics, thereby improving the absorption effect; through the control of the condensation temperature of the first oil, the content of the dissolved C4 component in the first oil can be reduced, so that the first oil can more effectively absorb C3+ component; and the first oil in this temperature range is also more suitable for being returned to the tower as the top heat reflux of the main fractionating tower, thereby further improving the operation flexibility of the main fractionating tower, the condensation extraction conditions of the secondary crude gasoline are the same as those of the traditional design, that is, the crude gasoline is extracted after air cooling and water cooling, which is favorable for clearly cutting the components, the content of the light component in the secondary crude gasoline is higher than that in the first oil, the product quality can be effectively improved, and the energy consumption can be reduced.

[0030] In addition, the utility model is provided with a product gasoline outlet on the side of the stabilizing tower, as many C4 components as possible are collected in the side line product gasoline to obtain more economic benefits; the tower bottom extraction oil is circulated to the absorption tower as a supplementary absorbent, the content of C4 and the components below C4 in the tower bottom extraction oil can be reduced to improve the absorption effect; according to the product quality requirements of the stable gasoline, the reasonable proportion of the side line stream and the tower bottom stream can be mixed to reach the quality card edge of the product stable gasoline; meanwhile, the different quality requirements of the product gasoline and the supplementary circulating gasoline to the content of C4 and the components below C4 are considered, the effective components are clearly cut, the absorption effect and the product value are improved; the utility model introduces a cold water circulation system, the coolant water is used to further cool part of the streams in the absorption and stabilization process, the relevant streams can be adjusted to more favorable low temperature conditions, thereby improving the reaction effect of the absorption and reabsorption towers and reducing the escape of C3+ component; the coolers involved in this improvement include the fractionating tower top crude gasoline cooler, the rich gas compressor interstage cooler, the compressed rich gas cooler, the absorption tower middle section cooler and the supplementary absorbent cooler. BRIEF DESCRIPTION OF DRAWINGS

[0031] Figure 1It is a structural schematic diagram of an embodiment of the present utility model. DETAILED DESCRIPTION

[0032] The present invention will be described in further detail below with reference to the accompanying drawings and embodiments.

[0033] like Figure 1 As shown, the absorption and stabilization system for crude oil processing of this embodiment includes:

[0034] The main fractionating tower 1 is provided with a reaction oil and gas inlet on the side, an oil slurry outlet at the bottom, and an oil and gas outlet at the top;

[0035] The first-stage liquid separation tank 10 is provided downstream of the main fractionating tower 1 and is used to perform a first-stage liquid separation on the oil and gas outputted from the top of the main fractionating tower 1; a branch pipeline for returning part of the liquid phase to the main fractionating tower 1 is connected downstream of the first-stage liquid separation tank 10;

[0036] The water separator 2 is provided downstream of the first-stage liquid separator 10 and is used to separate part of the liquid phase output from the first-stage liquid separator 10;

[0037] The secondary liquid separation tank 20 is used to perform secondary liquid separation on the gas phase output from the primary liquid separation tank 10;

[0038] The absorption tower 3 is provided with an inlet for the first-stage crude gasoline obtained from the water separator 2 and the second-stage crude gasoline obtained from the second-stage liquid separator 20, an outlet for the top gas is provided at the top of the tower, and an outlet for the bottom oil is provided at the bottom of the tower;

[0039] The reabsorption tower 4 is provided with an inlet for inputting the overhead gas output from the top of the absorption tower 3, an outlet for outputting the dry gas from the overhead gas is provided at the top of the tower, and an outlet for outputting the rich absorption oil is provided at the bottom of the tower, and the outlet is connected to the inlet of the main distillation tower 1;

[0040] The desorption tower 5 is provided with an inlet for inputting the liquid phase obtained after the bottom oil of the absorption tower 3 is separated, an outlet for outputting the top gas is provided at the top of the tower, and an outlet for outputting the bottom oil is provided at the bottom of the tower;

[0041] The stabilization tower 6 is located downstream of the desorption tower 5 and is provided with an inlet for inputting the bottom oil of the desorption tower 5, an outlet for outputting the top oil and gas at the top of the tower, and an outlet for outputting the bottom oil at the bottom of the tower.

[0042] In the above-described catalytic absorption system, a hot water heat exchanger is provided between the main fractionating tower 1 and the primary separator 10 to exchange heat with the oil and gas transported from the top of the main fractionating tower 1 to the primary separator 10. A branch pipeline 101 is connected between the primary separator 10 and the water separator 2 to supply a portion of the liquid phase obtained at the bottom of the primary separator 10 to the main fractionating tower 1.

[0043] A first refrigerant water cooler 01 for exchanging heat with the liquid phase output from the water separator 2 is provided between the water separator 2 and the absorption tower 3 .

[0044] In this embodiment, an air cooler and a second refrigerant water cooler 02 are provided between the first-stage liquid separator 10 and the second-stage liquid separator 20. A rich gas first-stage compressor 001, a compressor interstage refrigerant water cooler 002, and a rich gas second-stage compressor 003 are provided on the top of the second-stage liquid separator 20, which can further process the rich gas output by the second-stage liquid separator 20. An air cooler 004 capable of exchanging heat with a mixture of rich gas, compressor condensate oil, acidic water, and the top gas of the desorption tower 5 and an air cooler 006 located downstream of the rich gas second-stage compressor 003 are provided. Downstream of the air cooler 004 is a third refrigerant water cooler 03 for cooling the above-mentioned mixture (rich gas, compressor condensate oil, acidic water, desorption tower 5 top gas) and the bottom oil of the absorption tower 3. A three-phase liquid separator 7 is provided downstream of the third refrigerant water cooler 03. The top of the three-phase liquid separator 7 is provided with an outlet for supplying the gas phase to the absorption tower 3. The bottom of the three-phase liquid separator 7 is provided with a desorption tower feed heater 50 for heating the output liquid phase. The desorption tower feed heater 50 is connected to the inlet of the desorption tower 5.

[0045] The feeding pipeline from the desorption tower 5 to the stabilization tower 6 is provided with a first stabilization tower feed heat exchanger 61 and a second stabilization tower feed heat exchanger 62. A desorption tower middle section heat exchanger is provided on the side of the desorption tower 5. A side product output pipeline 63 is provided on the side of the stabilization tower 6. The side product output pipeline 63 is merged with the product gasoline output pipeline 64 at the bottom of the stabilization tower and is connected to the inlet of the desorption tower feed heater 50 through the first stabilization tower feed heat exchanger 61 and the first desorption tower middle section heat exchanger 511 in sequence. The desorption tower feed heater 50 has an outlet 501 for outputting product stabilized gasoline.

[0046] The circulating gasoline at the bottom of the stabilization tower 6 passes through the second stabilization tower feed heat exchanger 62 and the second desorption tower middle section heat exchanger 512 in sequence and then enters the hot water and air-cooled heat exchanger 005. A fourth refrigerant water cooler 04 is provided downstream of the hot water and air-cooled heat exchanger 005. The absorption tower 3 is provided with an inlet 301 for inputting the circulating gasoline output by the fourth refrigerant water cooler 04.

[0047] Two middle section reflux pipelines 006 are provided on the side of the absorption tower 3 , and a fifth refrigerant water cooler 05 and a sixth refrigerant water cooler 06 are respectively provided on the two middle section reflux pipelines 006 .

[0048] Downstream of the main fractionation tower 1 is a light diesel stripper 8. A top pipeline 81 is provided at the top of the light diesel stripper 8 for returning the gaseous phase to the main fractionation tower 1. A liquid phase outlet is provided at the bottom of the light diesel stripper 8. A heat exchanger for exchanging heat with the liquid phase is also provided at the bottom of the light diesel stripper 8. A delivery pipeline 82 is provided at the bottom of the light diesel stripper 8 for transferring a portion of the heat-exchanged light diesel to the reabsorption tower 4.

[0049] The main fractionating tower top oil and gas of the present embodiment adopts two-stage condensation technology. The liquid phase separated by the first-stage separator is divided into two streams. One stream is returned to the main fractionating tower as the tower top heat reflux. The other stream of first-stage crude gasoline is first delivered to the top feed of the absorption tower as an absorbent after removing most of the water through a water separator. The gas of the first-stage separator enters the second-stage separator at the top of the fractionating tower. The liquid phase separates the second-stage crude gasoline and delivers it to the upper feed of the absorption tower, also as an absorbent. The gaseous product rich gas enters the two-stage rich gas compressor. The compression interstage also adopts a refrigerant water cooler to be cooled to about 10-35 ℃. The compressed rich gas is mixed with the acid water from the fractionating tower, the desorption tower overhead gas and the first-stage condensed oil of the compressor. After being cooled by an air cooler, it is merged with the oil at the bottom of the absorption tower. After continuing to be cooled to about 10-35 ℃ by a refrigerant water cooler, it enters the three-phase separator. The separated gas enters the absorption tower from the bottom of the tower and contacts with the absorbent two-stage crude gasoline from the top of the main fractionating tower and the supplementary absorbent from the stabilization tower. The absorption tower is also equipped with two mid-section refluxes for heat extraction. The mid-section reflux uses a refrigerant water cooler to reduce the return tower temperature to about 10-35°C. The overhead gas from the absorption tower enters the reabsorption tower, where it comes into contact with the reabsorbent light diesel from the main fractionation tower, absorbing the gasoline components therein. Dry gas from the reabsorption tower is discharged from the top of the tower, and rich absorption oil is discharged from the bottom of the tower and returns to the main fractionation tower. The oil phase separated from the three-phase separation tank is preheated by the desorption tower feed heater with the product stabilized gasoline as the heat source before entering the desorption tower. The desorption tower is equipped with a mid-section heating system. The heat source for the mid-section heating is the stabilization tower side product gasoline and the tower bottom supplementary absorbent stream. A reboiler is provided at the bottom of the desorption tower. The bottom oil produced at the bottom of the tower is preheated by the stabilization tower side product gasoline and the tower bottom supplementary absorbent before entering the stabilization tower. The oil and gas at the top of the stabilization tower are cooled in air and circulating water coolers, respectively, before entering a separator tank for gas-liquid separation. The gas exits the device as dry gas from the top of the stabilization tower, while the liquid is split into two streams: one as the product liquefied petroleum gas (LPG) and the other as overhead reflux, returning to the stabilization tower. A liquid sideline is installed 1-4 plates below the bottom of the stabilization tower to produce a gasoline product stream. The bottom of the stabilization tower is drawn off in three streams: one is heated in a bottom reboiler and returned to the tower; the second is used to replenish absorbent; and the third is used to replenish the product stabilized gasoline. The stabilized gasoline product from the stabilization tower sideline passes through the second stabilization tower feed heat exchanger, the second desorber mid-stage heat exchanger, and the desorber feed heater before exiting the device. The replenished absorbent at the bottom of the stabilization tower passes through the first stabilization tower feed heat exchanger, the first desorber mid-stage heat exchanger, a hot water cooler, and an air cooler. It is then cooled to 10-35°C in a refrigerant water heat exchanger before being pumped to the absorption tower.

[0050] Specifically:

[0051] The overhead oil gas of the main fractionating column in this embodiment is cooled initially (about 70-100°C) and then enters a primary knockout drum at the top of the fractionating column. The gas phase in the primary knockout drum is further cooled to a lower temperature (about 20-50°C) and then enters a secondary knockout drum at the top of the fractionating column, separating out rich gas and secondary crude gasoline. The liquid phase obtained from the primary knockout drum is divided into two streams, one of which is returned to the fractionating column as hot reflux, and the other of which is used as an absorbent, first passing through a water trap to remove excess water, and then being cooled to a lower temperature (about 20-50°C) to obtain primary crude gasoline with better absorption effect. The two grades of crude gasoline are sent to different positions in the absorption tower for absorption.

[0052] The products obtained from the bottom of the stabilizing column in this embodiment are used in two ways, one of which is as a stable gasoline product leaving the device, and the other of which is as a supplementary absorbent going to the absorption tower. The quality control target for the supplementary absorbent is to control the content of C4 and below as low as possible, and the target for the stable gasoline product is to meet the saturated vapor pressure index quality card (i.e., to accommodate as much C4 component as possible under the premise of meeting the saturated vapor pressure requirement) to obtain economic benefits. Considering the different quality requirements for the content of C4 and below in the product gasoline and the supplementary circulating gasoline, two products are obtained from the lower part of the stabilizing column in this embodiment, one of which is the supplementary absorbent sent to the absorption tower for circulation, and the other of which is the stable gasoline stream obtained from the side line of the lower part of the stabilizing column. Depending on the quality requirements of the stable gasoline product, the stable gasoline obtained from the side line can be mixed with part of the bottom stream to form the product stable gasoline. The product stable gasoline and the supplementary circulating gasoline are in turn heat exchanged with the stabilizing column feed and the middle stream of the desorption tower to recover useful heat. The above scheme can improve the quality of the gasoline at the bottom of the stabilizing column, which is conducive to improving the absorption effect, and can also reasonably mix the side stream and the bottom stream while ensuring that the quality of the product stable gasoline meets the requirements.

[0053] A cold water circulation system is introduced in this embodiment to adjust the relevant streams of the absorption reaction to a more favorable low temperature condition, so as to improve the reaction effect of the absorption and resorption towers and reduce the escape of C3+ components. In this embodiment, a refrigeration unit is introduced, low-temperature heat resources are used to produce refrigerant water, which is supplied to the absorption and stabilization system to reduce the temperature of the absorption process, effectively utilizing the waste heat of the device while improving the absorption efficiency. Typical absorption refrigeration processes include lithium bromide refrigeration and ammonia water refrigeration, which can produce refrigerant water at a temperature lower than normal temperature (about 5-30°C). Further cooling of part of the streams in the absorption and stabilization process using the refrigerant water can further cool the relevant streams to a temperature lower than normal temperature (about 10-35°C), improving the absorption effect.

[0054] The absorption stabilizing system of the embodiment can reduce the total flow of dry gas, reduce the loss of C3+ components, recycle C3 components into product LPG, recycle C4 and C5 components into product gasoline, and improve the economic value of effective materials. The embodiment replaces part of the cooling medium of the heat exchanger (replaces circulating water with chilled water), adds some heat exchange equipment and two-stage condensation at the top of the fractionating column, reallocates the load to be borne by different cooling media, and the transformation operation of opening the side line of the stabilizing column can reduce the circulation amount of the stabilizing gasoline under the premise of not losing product yield, and further reduce the original cooling load on the material.

Claims

1. An absorption and stabilization system for crude oil processing, characterized by: include The main fractionating tower is provided with a reaction oil and gas inlet on the side, an oil slurry outlet at the bottom, and an oil and gas outlet at the top; A first-stage liquid separation tank is provided downstream of the main fractionating tower, and is used for performing first-stage liquid separation on the oil and gas outputted from the top of the main fractionating tower; a branch pipeline for returning part of the liquid phase to the main fractionating tower is connected downstream of the first-stage liquid separation tank; A water separator is provided downstream of the first-stage liquid separator, and is used for separating the liquid phase outputted from the first-stage liquid separator; A secondary liquid separation tank, used for performing secondary liquid separation on the gas phase output from the primary liquid separation tank; The absorption tower is provided with an inlet for inputting the first-stage crude gasoline obtained from the water separator and the second-stage crude gasoline obtained from the second-stage liquid separator, an outlet for outputting the overhead gas is provided at the top of the tower, and an outlet for outputting the bottom oil is provided at the bottom of the tower; The reabsorption tower is provided with an inlet for inputting the overhead gas output from the top of the absorption tower, an outlet for outputting the dry gas from the overhead gas is provided at the top of the tower, and an outlet for outputting the rich absorption oil is provided at the bottom of the tower, and the outlet is connected to the inlet of the main distillation tower; The desorption tower is provided with an inlet for inputting the liquid phase obtained after the bottom oil of the absorption tower is separated, an outlet for outputting the top gas is provided at the top of the tower, and an outlet for outputting the bottom oil is provided at the bottom of the tower; as well as The stabilization tower is arranged downstream of the desorption tower, and is provided with an inlet for inputting the bottom oil of the desorption tower, an outlet for outputting the top oil and gas, and an outlet for outputting the bottom oil.

2. The absorption and stabilization system for crude oil processing according to claim 1, characterized in that: A hot water heat exchanger is provided between the main fractionating tower and the first-stage liquid separator tank, for exchanging heat between the oil and gas transported from the top of the main fractionating tower to the first-stage liquid separator tank.

3. The absorption and stabilization system for crude oil processing according to claim 1, characterized in that: A branch pipeline for supplying part of the liquid phase obtained at the bottom of the first-stage liquid separator to the main distillation tower is connected between the first-stage liquid separator and the water separator.

4. The absorption and stabilization system for crude oil processing according to claim 1, characterized in that: A first refrigerant water cooler is provided between the water separator and the absorption tower for exchanging heat with the liquid phase outputted from the water separator.

5. The absorption and stabilization system for crude oil processing according to claim 1, characterized in that: An air cooler and a second refrigerant water cooler are arranged between the first-level liquid separator tank and the second-level liquid separator tank. A rich gas first-level compressor, a compressor inter-stage refrigerant water cooler, and a rich gas second-level compressor are arranged on the top of the second-level liquid separator tank, which can further process the rich gas output by the second-level liquid separator tank. An air cooler capable of exchanging heat with a mixture of rich gas, compressor condensed oil, acidic water, and desorption tower top gas and a third refrigerant water cooler located downstream of the air cooler for cooling the above mixture and the absorption tower bottom oil are arranged downstream of the third refrigerant water cooler. A three-phase liquid separator tank is arranged at the downstream of the third refrigerant water cooler. The top of the three-phase liquid separator tank is provided with an outlet for supplying the gas phase to the absorption tower, and the bottom of the three-phase liquid separator tank is provided with a desorption tower feed heater for heating the liquid phase output therefrom, and the desorption tower feed heater is communicated with the inlet of the desorption tower.

6. The absorption and stabilization system for crude oil processing according to claim 5, characterized in that: The feeding pipeline from the desorption tower to the stabilization tower is provided with a first stabilization tower feed heat exchanger and a second stabilization tower feed heat exchanger, the side of the desorption tower is provided with a desorption tower middle section heat exchanger, and the side of the stabilization tower is provided with a side line product output pipeline, which is merged with the product gasoline output pipeline at the bottom of the stabilization tower and then connected to the inlet of the desorption tower feed heater in sequence through the first stabilization tower feed heat exchanger, the desorption tower middle section heat exchanger, and the desorption tower feed heater has an outlet for outputting product stabilized gasoline.

7. The absorption and stabilization system for crude oil processing according to claim 6, characterized in that: The circulating gasoline at the bottom of the stabilization tower passes through the second stabilization tower feed heat exchanger and the desorption tower middle section heat exchanger in sequence and then enters the hot water and air-cooled heat exchanger. A fourth refrigerant water-water cooler is provided downstream of the hot water and air-cooled heat exchanger, and the absorption tower is provided with an inlet for inputting the circulating gasoline output by the fourth refrigerant water-water cooler.

8. The absorption and stabilization system for crude oil processing according to any one of claims 1 to 7, characterized in that: Two middle section reflux pipelines are provided on the side of the absorption tower, and a fifth refrigerant water cooler and a sixth refrigerant water cooler are respectively provided on the two middle section reflux pipelines.

9. The absorption and stabilization system for crude oil processing according to any one of claims 1 to 7, characterized in that: A light diesel stripping tower is provided downstream of the main fractionating tower. A tower top pipeline for supplying gas phase back to the main distillation tower is provided at the top of the light diesel stripping tower. A liquid phase output outlet is provided at the bottom of the light diesel stripping tower.

10. The absorption and stabilization system for crude oil processing according to claim 9, characterized in that: A heat exchanger for exchanging heat with the liquid phase is further provided at the bottom of the light diesel stripping tower. A delivery pipeline for delivering part of the light diesel after heat exchange to the reabsorption tower is provided at the bottom of the light diesel stripping tower.

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