CN102516007A - A process and device for processing hydrocarbons by utilizing liquefied gas - Google Patents

Abstract

The invention discloses a process for preparing hydrocarbon by processing liquefied gas and a device thereof, wherein the process comprises a cracking reaction process, an absorption stabilization process, an aromatization reaction process, a gas component feed gas concentration process and an aromatic hydrocarbon purification process; the device comprises a cracking reaction system, an absorption stabilizing system, an aromatization reaction system, a gas separation feed gas concentration system and an aromatic hydrocarbon purification system; the invention has the advantages that: the process has the advantages of low energy consumption, low requirement on equipment and heat energy, easiness in realization, simple device flow, easiness in operation and stability in operation, and can be used for stopping the operation of the deisobutanizer, treating 90kg of standard coal consumption for treating four carbon raw materials per ton, saving the energy consumption by 48.5%, increasing the propylene content of the gas component raw material gas from 15% of the original mass fraction to 50%.

Description

A process and device for processing hydrocarbons by utilizing liquefied gas

technical field

The invention relates to a liquefied gas deep processing technology, in particular to a technology and a device for processing hydrocarbons by utilizing liquefied gas, and belongs to the field of processing hydrocarbons by liquefied gas.

Background technique

There are many methods for the processing and separation of liquefied gas used in chemical production. At present, there is mainly one kind commonly used in the industry: first pretreatment of raw materials, the C2C3 components in the liquefied petroleum gas are extracted from the top of the depropanizer, and the mixed C4 components at the bottom of the tower enter the deisobutanizer , the isobutane is separated from the top of the deisobutanization tower, and the components with carbon four or more at the bottom of the tower enter the cracking reaction system for cracking reaction, and the obtained low-carbon hydrocarbons including propylene enter the absorption stabilization system; Absorption tower, desorption tower, and stabilization tower are used to separate the materials in a cycle, and finally the raw gas containing 15% propylene mass fraction is obtained from the top of the stabilization tower, the aromatics at the bottom of the stabilization tower, and the dry gas at the top of the absorption tower. Aromatic hydrocarbons and fuel gas are obtained after the aromatization reaction, and the raw material gas for gas separation is recovered after passing through the reflux pump of the stabilization tower, and sent to the gas separation device or the gas separation raw material tank for storage.

This method has high requirements on equipment and heat energy, especially when separating isobutane in the de-isobutanizer tower, 200 layers of trays are needed, the height of the whole tower reaches 160 meters, and the temperature at the top of the tower is not lower than 50°C. The thermal conditions are harsh, the energy consumption is high, accounting for 50% of the total energy consumption, the operation of the device is uncoordinated, and the quality of the isobutane product cannot meet the requirements; at the same time, the content of propylene in the raw gas produced is low, only 15%, resulting in the downstream gas The sub-device is unstable. At the same time, the content of aromatic hydrocarbon impurities after the aromatization reaction is high, the product market competitiveness is weak, and the price is low.

Contents of the invention

In order to solve the above problems, the present invention designs a process and device for processing hydrocarbons by utilizing liquefied gas. The process is simple, easy to operate, low in energy consumption, and high in product quality.

Technical scheme of the present invention is:

A process for producing hydrocarbons by using liquefied gas, including a cracking reaction process, an absorption stabilization process, an aromatization reaction process, a gas separation raw material gas concentration process and an aromatics purification process.

in:

(1) Cracking reaction process:

The C4 raw material liquefied gas in the cracking raw material tank is transported to the device area through the raw material pump, and the first heat exchanger and the second heat exchanger exchange heat with the cracking reaction product. After the heat exchange, the C4 raw material enters the heating furnace, and further Raise the temperature to 500°C, and the heated gas enters from the top of the cracking reactor to carry out the cracking reaction;

The pyrolysis reaction product passes through the second heat exchanger, the first heat exchanger, the hot water heat exchanger, and the pyrolysis product cooler from the bottom of the pyrolysis reactor to conduct heat exchange and cooling, until the temperature drops to 40°C, it enters the gas-liquid Separation tank for separation; the separated condensate is pumped into the absorption tower with the reaction liquid to further absorb the rich gas sent by the compressor; the separated gas is compressed and cooled by the rich gas compressor, and then sent to The absorption tower absorbs further.

(2) Absorption stabilization process:

The gas compressed by the rich gas compressor in the above process (1), together with the absorption oil from the bottom of the absorption tower and the desorbed gas from the top of the desorption tower, passes through the air cooler at the outlet of the compressor and the cooler at the outlet of the compressor in sequence, and is cooled to After 40°C, it enters the liquid separation tank at the outlet of the air compressor to separate oil and gas;

The rich gas is precipitated from the top of the liquid separation tank at the outlet of the air compressor and transported to the lower part of the absorption tower, where it is countercurrently contacted with the absorbent entering from the upper part of the absorption tower, and the lean gas after absorption enters the dry gas liquid separation from the top of the absorption tower tank for gas-liquid separation, the liquid flows into the stabilization tower for reflux, and the dry gas from the top of the dry gas separator tank is sent to the aromatization reactor;

In order to take away the heat released in the absorption tower, use the middle section pump of the absorption tower to pump out the gasoline that circulates back in the middle section of the absorption tower, cool down to 20°C through the cooler in the middle section of the absorption tower, and then return to the absorption tower;

The condensate coming out of the bottom of the separatory tank at the outlet of the pneumatic compressor is divided into two paths through the feed pump of the desorption tower: one path directly enters the top of the desorption tower, and the other path passes through the feed heat exchanger of the desorption tower to 70°C and enters the upper part of the desorption tower;

The desorbed gas escapes from the top of the tower and merges with the compressed rich gas of the rich gas compressor to enter the air cooler at the outlet of the compressor; the desorbed gasoline is pumped out from the bottom of the desorbed tower by the feed pump of the stabilized tower, and passes through the feed heat exchanger of the stabilized tower and the stabilized tower After the stabilized gasoline at the bottom is heated to 125°C, it enters the middle of the stabilizer tower;

The components of carbon 4 and lower than carbon 4 are distilled from the top of the stable tower, and enter the top reflux tank of the stable tower through the air cooler at the top of the stable tower and the condenser at the top of the stable tower. After the tower reflux pump is drawn out, it is divided into two paths: one path returns to the top of the stabilization tower as reflux, and the other path enters the feed preheater of the depropanizer tower;

The stabilized gasoline in the stabilization tower comes out from the bottom of the tower, and after being cooled to 30°C by the feed heat exchanger of the stabilization tower, the feed heat exchanger of the desorption tower, and the light hydrocarbon cooler, it is divided into two parts: one part enters the feed exchange of the stripping tower The light aromatics produced by the heater and the top of the stripping tower, that is, the product gasoline, enter the stripping tower after heat exchange, and the other part is pressurized by the absorption oil pump and cooled to 20°C by the absorption oil cooler to be sent to the top of the absorption tower as an absorbent.

Further, in the desorption tower, heat is supplied to the tower from the reboiler of the desorption tower at the bottom of the tower.

Further, the stabilizing tower supplies heat to the tower from the stabilizing tower reboiler at the bottom of the tower.

(3) Aromatization reaction process:

The dry gas coming out of the top of the dry gas liquid separation tank in the above process (2) is combined with the fuel gas of the dry gas cycler and then divided into two parts: one part as the main line first enters the dry gas feed heat exchanger, and after the aromatization reaction The gas is exchanged for heat, and then the dry gas electric heater is further heated to 300°C, then enters from the top of the aromatization reactor, and contacts with the aromatization catalyst to carry out the aromatization reaction; the other part is to control the aromatization reactor The internal temperature directly enters the aromatization reactor from the middle to carry out the aromatization reaction without heat exchange;

The gas after the aromatization reaction comes out from the bottom of the aromatization reactor and enters the dry gas feed heat exchanger. After heat exchange with the raw material dry gas, it passes through the aromatization product cooler and the aromatization product deep cooler After 20°C, go to the aromatization product gas-liquid separation tank for gas-liquid separation. The gas phase is divided into two parts: one part enters the heating furnace as fuel gas, and the other part is compressed by the dry gas cycle machine and returns to the aromatization reactor; the liquid phase Aromatics, that is, naphtha, directly enters the feed heat exchanger of the stripper depending on the pressure difference between the aromatization reaction system and the stripper system.

(4) Raw material gas enrichment process for gas separation

From the gas separation in the above process (2), the raw material gas enters the feed preheater of the depropanizer directly from the bottom of the stabilizer top reflux tank through the stabilizer reflux pump partly relying on the pressure difference between the stabilizer tower and the depropanizer. Enter the depropanizer to separate C3 and C4 components;

The carbon three fraction, that is, the gas fraction, raw material gas is steamed from the top of the depropanizer tower, cooled by the air cooler and condenser at the top of the depropanizer tower, and then enters the reflux tank at the top of the depropanizer tower, and the condensate is drawn out by the reflux pump of the depropanizer tower and divided into two Part: one part is used as the reflux of the depropanizer, and the other part is sent to the gas separation device as the gas separation raw material or sent to the gas separation raw material tank for storage;

The carbon four components from the bottom of the depropanizer directly enter the MTBE unit as a raw material to participate in the reaction or are sent to the carbon four raw material tank for storage depending on the pressure difference.

Further, the depropanizer is supplied with heat from the reboiler of the depropanizer at the bottom of the tower, and the heat source is heat transfer oil.

(5) Aromatics purification process

The aromatics from the light hydrocarbon cooler of the stabilization tower in the above process (2) and the aromatization product gas-liquid separation tank in (3) pass through the feed heat exchanger, that is, the product cooler at the top of the tower and the gas phase at the top of the stripping tower. After heat exchange, enter the stripping tower from the middle section of the stripping tower;

The aromatics entering the stripping tower perform mass transfer and heat transfer with the original light aromatics in the tower, which is the product gasoline, and are divided into heavy components and light components;

The heavy components move down to the bottom of the tower and are further heated by the reboiler of the stripping tower. At the same time, part of the heavy components are extracted and sent to the heavy oil tank for storage after being boosted by the forced circulation pump;

The light component evaporates and rises, and is fully vaporized. After the rising light component escapes from the top of the tower to the feed heat exchanger, it is further cooled to 30°C by the condenser on the top of the tower, and then enters the reflux tank, and is boosted by the reflux pump. It is divided into two parts: one part is extracted as aromatic products and sent to the gasoline tank for storage, and the other part enters the stripping tower from the top of the tower as reflux.

The raw material directly enters the cracking reaction system for reaction, and the low-carbon hydrocarbons obtained after the cracking reaction are processed by the absorption stabilization system and then enter the depropanizer, and the raw material gas with the original propylene content of 15% is extracted from the top of the depropanizer; Separation of light and heavy components of aromatics obtained from aromatization and stabilization at the bottom of the tower to obtain light aromatics with relatively pure components. The low-carbon hydrocarbon liquefied gas obtained after the absorption and stabilization system enters the depropanizer, and the raw material gas is separated from the top of the tower, and the propylene content reaches 50%.

A device for realizing the above process of processing hydrocarbons by using liquefied gas, including a cracking reaction system, an absorption stabilization system, an aromatization reaction system, a gas separation raw material gas concentration system, and an aromatics purification system.

in,

The cracking reaction system includes: a raw material pump, a first heat exchanger, a second heat exchanger, a heating furnace, a cracking reactor, a reaction product cooler, a hot water heat exchanger, a gas-liquid separation tank, and a reaction liquid pump , rich gas compressor, air cooler at the outlet of the air compressor, cooler at the outlet of the air compressor, liquid separation tank at the outlet of the air compressor;

The outlet of the raw material pump is connected to the bottom nozzle of the shell side of the first heat exchanger, the top nozzle of the shell side of the first heat exchanger is connected to the bottom nozzle of the second heat exchanger shell side, and the top nozzle of the shell side of the second heat exchanger is respectively It is connected with the inlet of the heating furnace and the middle part of the cracking reactor; the outlet of the heating furnace is connected with the top of the cracking reactor;

The bottom of the cracking reactor is connected to the top nozzle of the second heat exchanger tube side, the bottom nozzle of the second heat exchanger tube side is connected to the top nozzle of the first heat exchanger tube side, and the bottom tube of the first heat exchanger tube side The nozzle is connected to the top nozzle of the hot water heat exchanger tube side, the bottom nozzle of the hot water heat exchanger tube side is connected to the top nozzle of the cracked product cooler shell side, and the bottom nozzle of the cracked product cooler shell side is connected to the gas-liquid separation tank The top inlet is connected, the bottom outlet of the gas-liquid separation tank is connected to the inlet of the reaction liquid pump; the outlet of the reaction liquid pump is connected to the upper part of the absorption tower; the gas phase outlet on the top of the gas-liquid separation tank is connected to the rich gas compressor; the rich gas compressor and air compressor outlet are air-cooled The air compressor outlet cooler, the air compressor outlet liquid separation tank are connected in turn; the gas phase outlet at the top of the air compressor outlet liquid separation tank is connected with the lower part of the absorption tower; the air pressure machine outlet liquid separation tank bottom outlet is connected with the desorption tower feed pump.

The absorption stabilization system includes: absorption tower, absorption tower mid-section pump, absorption tower mid-section cooler, absorption tower bottom oil pump, desorption tower, desorption tower feed pump, desorption tower feed heat exchanger, desorption tower reboiler , Stabilizing Tower, Stabilizing Tower Feed Pump, Stabilizing Tower Feed Heat Exchanger, Stabilizing Tower Reboiler, Stabilizing Tower Top Air Cooler, Stabilizing Tower Top Cooler, Stabilizing Tower Top Reflux Tank, Stabilizing Tower Reflux Pump, Light Hydrocarbon Cooling device, absorption oil pump, absorption oil cooler, dry gas separator tank;

The bottom of the absorption tower is connected to the inlet of the air cooler at the outlet of the air compressor through the oil pump at the bottom of the absorption tower, and the top of the absorption tower is connected to the dry gas liquid separation tank; the top of the dry gas liquid separation tank is connected to the bottom nozzle of the shell side of the dry gas feed heat exchanger connected; the bottom of the dry gas separator tank is connected to the inlet of the stabilizer reflux pump; the outlet of the stabilizer reflux pump is respectively connected to the upper part of the stabilizer tower and the bottom nozzle of the feed preheater tube side of the depropanizer;

In the middle of the absorption tower, the pump in the middle of the absorption tower and the cooler in the middle of the absorption tower are sequentially connected in parallel;

The desorption tower feed pump is connected to the top of the desorption tower, and the desorption tower feed pump is also connected to the upper part of the desorption tower through the desorption tower feed heat exchanger;

Both the desorption tower and the rich gas compressor are connected to the outlet air cooler of the compressor; the bottom of the desorption tower is connected to the middle of the stabilization tower through the feed pump of the stabilization tower and the feed heat exchanger of the stabilization tower;

The top of the stabilizing tower, the air cooler at the top of the stabilizing tower, the condenser of the stabilizing tower, and the reflux tank at the top of the stabilizing tower are connected in sequence; connected to the preheater;

The bottom of the stabilization tower, the feed heat exchanger of the stabilization tower, the feed heat exchanger of the desorption tower, and the light hydrocarbon cooler are connected in sequence; the light hydrocarbon cooler is connected with the feed heat exchanger of the stripping tower, and the light hydrocarbon cooler is also connected in sequence It is connected to the top of the absorption tower through the absorption oil pump and the absorption oil cooler.

Further, the desorption tower is provided with a desorption tower reboiler at the bottom of the tower.

Further, the stable tower is provided with a stable tower reboiler at the bottom of the tower.

The aromatization reaction system includes: dry gas feed heat exchanger, dry gas electric heater, aromatization reactor, aromatization product cooler, aromatization product deep cooler, aromatization product Gas-liquid separation tank, dry gas cycle machine;

The top nozzle of the shell side of the dry gas feed heat exchanger is connected to the top of the aromatization reactor in turn through the dry gas electric heater; the top nozzle of the tube side of the dry gas feed heat exchanger is also connected to the bottom of the aromatization reactor connected; the bottom of the dry gas feed heat exchanger, the aromatized product cooler, the aromatized product deep cooler, and the aromatized product gas-liquid separation tank are connected in sequence; the top of the dry gas liquid separation tank is connected with the dry gas circulation The machine is connected to the middle part of the aromatization reactor;

The top of the aromatization product gas-liquid separation tank is connected to the heating furnace, and the aromatization product gas-liquid separation tank also passes through the dry gas cycler, dry gas feed heat exchanger, dry gas electric heater and aromatization reactor in sequence connected.

The gas separation raw material gas concentration system includes: a depropanizer feed preheater, a depropanizer, a depropanizer reboiler, a depropanizer top air cooler, a depropanizer top condenser, a depropanizer Item reflux tank, depropanizer reflux pump;

The tank bottom of the stabilizer top reflux tank is connected to the feed preheater of the depropanizer and the depropanizer in sequence through the stabilizer reflux pump;

The top of the depropanizer tower is connected with the depropanizer overhead air cooler, depropanizer overhead condenser, depropanizer overhead reflux tank, and depropanizer overhead reflux pump in order to form a loop; the depropanizer overhead reflux pump is also connected to the gas The device is connected.

Further, in the depropanizer, the reboiler of the depropanizer at the bottom of the tower supplies heat to the inside of the tower, and the heat source is heat transfer oil.

The light hydrocarbon purification system includes: feed heat exchanger, electric heater, stripper, stripper reboiler, stripper top condenser, stripper top reflux tank, stripper reflux pump , forced circulation pump;

The stripper feed heat exchanger is connected to the stripper; the forced circulation pump is connected to the heavy oil tank;

The top of the stripper is connected with the feed heat exchanger of the stripper, the condenser at the top of the stripper, the reflux tank of the stripper, and the reflux pump of the stripper in order to form a loop; the reflux pump of the stripper is also connected with the gasoline tank .

Further, the stripping tower is provided with a stripping tower reboiler at the bottom of the tower.

Compared with the existing hydrocarbon production process, the present invention removes the deisobutanizer and its auxiliary equipment, does not pretreat the raw materials, and directly enters the cracking reaction system for reaction, and the low-carbon hydrocarbons after the reaction are absorbed and stabilized After the system is processed, it enters the depropanizer tower to concentrate the raw material gas, so that the propylene gas with a weight content of ≥15% is extracted from the top of the depropanizer tower; the aromatization is carried out through the stripping tower in the aromatics purification process The aromatics obtained at the bottom of the stable tower are separated from light and heavy components, and further enriched, so as to obtain light aromatics with relatively pure components, and the content of propylene reaches 50% by weight.

The advantages of the present invention are:

(1) Low energy consumption: when using the existing de-isobutanizer process, 175kg of standard coal is consumed per ton of raw material C4. Raw materials consume 90kg of standard coal, saving energy consumption by 48.5%;

(2) The propylene content of the raw material gas is high, and the mass fraction content is increased from the original 15% to 50%;

(3) Low requirements on equipment and heat energy, easy to realize, simple installation process, easy to control, and stable operation.

The present invention will be further described below in conjunction with drawings and embodiments.

Description of drawings

Fig. 1 is a schematic diagram of equipment connection of a liquefied gas processing and hydrocarbon production device according to an embodiment of the present invention;

In the figure: 1-raw material pump, 2-first heat exchanger, 3-second heat exchanger, 4-heating furnace, 5-cracking reactor, 6-reaction product cooler, 7-hot water heat exchanger, 8-gas-liquid separation tank, 9-reactive liquid pump, 10-rich gas compressor, 11-air cooler at the outlet of the air compressor, 12-cooler at the outlet of the air compressor, 13-liquid separation tank at the outlet of the air compressor, 14-absorption tower, 15-Absorption tower mid-section pump, 16-Absorption tower mid-section cooler, 17-Absorption tower bottom oil pump, 18-Desorption tower, 19-Desorption tower feed pump, 20-Desorption tower feed heat exchanger, 21-Desorption tower weight Boiler, 22-stabilized tower, 23-stabilized tower feed pump, 24-stabilized tower feed heat exchanger, 25-stabilized tower reboiler, 26-stabilized tower top air cooler, 27-stabilized tower top condenser, 28-stabilizing tower top reflux tank, 29-stabilizing tower reflux pump, 30-light hydrocarbon cooler, 31-absorbing oil pump, 32-absorbing oil cooler, 33-dry gas liquid separation tank, 34-dry gas feed heat exchange Device, 35-Dry gas electric heater, 36-Aromatization reactor, 37-Aromatization product cooler, 38-Aromatization product cryogenic cooler, 39-Aromatization product gas-liquid separation tank, 40- Dry gas cycler, 41-depropanizer feed preheater, 42-depropanizer, 43-depropanizer reboiler, 44-depropanizer overhead air cooler, 45-depropanizer overhead condenser, 46 - Depropanizer reflux tank, 47- Depropanizer reflux pump, 48- Stripper feed heat exchanger, 49- Electric heater, 50- Stripper, 51- Stripper reboiler, 52- Stripping tower top condenser, 53-stripping tower top reflux tank, 54-stripping tower reflux pump, 55-forced circulation pump.

Detailed ways

Example 1

A process for producing hydrocarbons by utilizing liquefied gas, including the following steps:

(1) Cracking reaction process:

The C4 raw material in the cracking raw material tank is transported to the device area by the raw material pump, and exchanges heat with the pyrolysis reaction product through the first heat exchanger and the second heat exchanger. After the heat exchange, the C4 raw material enters the heating furnace to further raise the temperature To 500°C, the heated gas enters from the top of the cracking reactor to carry out the cracking reaction;

From the bottom of the cracking reactor, the cracking reaction product passes through the second heat exchanger, the first heat exchanger, the hot water heat exchanger, and the cracking product cooler (reaction condenser) for heat exchange and cooling until the temperature drops to 40 After ℃, it enters the gas-liquid separation tank for separation (the cracking reaction product conducts heat exchange with the C4 raw material in the second heat exchanger and the first heat exchanger; it is separated from the hot water and circulating water in the hot water heat exchanger and the cracking product respectively. Cooler for heat exchange); the separated condensate is pumped into the absorption tower with the reaction liquid to further absorb the rich gas sent by the compressor; the separated gas is compressed and cooled by the rich gas compressor, Sent to the absorption tower for further absorption;

(2) Absorption stabilization process:

The gas compressed by the rich gas compressor in the above process (1), together with the absorption oil from the bottom of the absorption tower and the desorbed gas from the top of the desorption tower, passes through the air cooler at the outlet of the compressor and the cooler at the outlet of the compressor in sequence, and is cooled to After 40°C, it enters the liquid separation tank at the outlet of the air compressor to separate oil and gas;

The rich gas is precipitated from the top of the liquid separation tank at the outlet of the air press and transported to the lower part of the absorption tower. In the absorption tower, it is countercurrently contacted with the absorbent (such as stable gasoline) that enters from the upper part of the absorption tower. The absorbed lean gas flows from the top of the absorption tower Enter the dry gas liquid separation tank for gas-liquid separation, the liquid flows into the stabilization tower for reflux, and the dry gas from the top of the dry gas liquid separation tank is sent to the aromatization reactor;

In order to take away the heat released in the absorption tower, use the middle section pump of the absorption tower to pump out the gasoline that circulates back in the middle section of the absorption tower, cool down to 20°C through the cooler in the middle section of the absorption tower, and then return to the absorption tower;

The condensate coming out of the bottom of the separatory tank at the outlet of the pneumatic compressor is divided into two paths through the feed pump of the desorption tower: one path directly enters the top of the desorption tower, and the other path passes through the feed heat exchanger of the desorption tower to 70°C and enters the upper part of the desorption tower;

The desorption tower is supplied with heat by the desorption tower reboiler at the bottom of the tower; the desorption gas escapes from the top of the tower, and merges with the compressed rich gas of the rich gas compressor into the air cooler at the outlet of the compressor; the desorption gasoline is used for self-desorption at the bottom of the desorption tower The feed pump of the stabilizing tower pumps out the stabilized gasoline through the feed heat exchanger of the stabilizing tower and the stable gasoline at the bottom of the stabilizing tower to 125°C, and then enters the middle of the stabilizing tower;

The stabilizing tower is supplied with heat by the stabilizing tower reboiler at the bottom of the tower; the components with carbon four and below are distilled from the top of the stabilizing tower, and enter the stabilizing tower overhead reflux through the stabilizing tower top air cooler and the stabilizing tower top condenser Tank, gas separation Raw gas is drawn from the tank bottom of the stabilizing tower reflux tank through the stabilizing tower reflux pump and divided into two paths: one path returns to the top of the stabilizing tower, and the other path enters the feed preheater of the depropanizer;

The stabilized gasoline in the stabilization tower comes out from the bottom of the tower, and after being cooled to 30°C by the feed heat exchanger of the stabilization tower, the feed heat exchanger of the desorption tower, and the light hydrocarbon cooler, it is divided into two parts: one part enters the feed exchange of the stripping tower The heat exchanger (that is, the overhead product cooler) exchanges heat with the light aromatics produced by the reflux at the top of the stripper, that is, the product gasoline, and then enters the stripper, and the other part is pressurized by the absorption oil pump and cooled to 20°C by the absorption oil cooler. The top of the absorption tower is used as absorbent;

(3) Aromatization reaction process:

The dry gas from the top of the dry gas liquid separation tank in the above process (2) is combined with the fuel gas of the dry gas cycler (screw compressor) and then divided into two parts: one part enters the dry gas feed heat exchanger as the main line first, and the other part enters the dry gas feed heat exchanger as the main line, and The gas after the aromatization reaction is exchanged for heat, and then heated to 300°C by the dry gas electric heater, enters from the top of the aromatization reactor, and contacts with the aromatization catalyst for aromatization reaction; the other part is the control The internal temperature of the aromatization reactor directly enters the aromatization reactor from the middle to carry out the aromatization reaction without heat exchange;

The gas after the aromatization reaction comes out from the bottom of the aromatization reactor and enters the dry gas feed heat exchanger. After heat exchange with the raw material dry gas, it passes through the aromatization product cooler and the aromatization product deep cooler After 20°C, go to the aromatization product gas-liquid separation tank for gas-liquid separation. The gas phase is divided into two parts: one part enters the heating furnace as fuel gas, and the other part is compressed by the dry gas cycle machine and returns to the aromatization reactor; the liquid phase Aromatics, that is, naphtha, directly enters the feed heat exchanger of the stripper depending on the pressure difference between the aromatization reaction system and the stripper system;

(4) Raw material gas enrichment process for gas separation

From the gas separation in the above process (2), the raw material gas enters the feed preheater of the depropanizer directly from the bottom of the stabilizer top reflux tank through the stabilizer reflux pump partly relying on the pressure difference between the stabilizer tower and the depropanizer. Enter the depropanizer to separate C3 and C4 components;

The carbon three fraction, that is, the gas fraction, raw material gas is steamed from the top of the depropanizer tower, cooled by the air cooler and condenser at the top of the depropanizer tower, and then enters the reflux tank at the top of the depropanizer tower, and the condensate is drawn out by the reflux pump of the depropanizer tower and divided into two Part: one part is used as the reflux of the depropanizer, and the other part is sent to the gas separation device as the gas separation raw material or sent to the gas separation raw material tank for storage;

The C4 component from the bottom of the depropanizer directly enters the MTBE (methyl tert-butyl ether) device as a raw material to participate in the reaction or is sent to the C4 raw material tank for storage by virtue of the pressure difference;

The depropanizer is supplied with heat by the reboiler of the depropanizer at the bottom of the tower, and the heat source is heat transfer oil

(5) Aromatics purification process

The aromatics from the light hydrocarbon cooler of the stabilization tower in the above process (2) and the aromatization product gas-liquid separation tank in (3) pass through the feed heat exchanger, that is, the product cooler at the top of the tower and the gas phase at the top of the stripping tower. After heat exchange, enter the stripping tower from the middle section of the stripping tower;

The aromatics entering the stripping tower perform mass transfer and heat transfer with the original light aromatics in the tower, which is the product gasoline, and are divided into heavy components and light components;

The heavy components move down to the bottom of the tower and are further heated by the reboiler of the stripping tower. At the same time, part of the heavy components are extracted and sent to the heavy oil tank for storage after being boosted by the forced circulation pump;

The light component evaporates and rises, and is fully vaporized. After the rising light component escapes from the top of the tower to the feed heat exchanger, it is further cooled to 30°C by the condenser on the top of the tower, and then enters the reflux tank, and is boosted by the reflux pump. It is divided into two parts: one part is extracted as aromatic products and sent to the gasoline tank for storage, and the other part enters the stripping tower from the top of the tower as reflux.

Results: 90kg of standard coal was consumed per ton of C4 raw material, saving energy consumption by 48.5%; the content of propylene in the raw material gas was increased to 50% by mass fraction.

Example 2

As shown in Figure 1, a device for realizing the process of utilizing liquefied gas to process hydrocarbons as described in Example 1, including a cracking reaction system, an absorption stabilization system, an aromatization reaction system, a gas separation raw material gas concentration system, and aromatics purification system. the

The cracking reaction system includes: raw material pump 1, first heat exchanger 2, second heat exchanger 3, heating furnace 4, cracking reactor 5, reaction product cooler 6, hot water heat exchanger 7, gas Liquid separation tank 8, reaction liquid pump 9, rich gas compressor 10, air compressor outlet air cooler 11, air compressor outlet cooler 12, air compressor outlet liquid separation tank 13;

The outlet of raw material pump 1 is connected to the bottom nozzle of the shell side of the first heat exchanger 2, the top nozzle of the shell side of the first heat exchanger 2 is connected to the bottom nozzle of the shell side of the second heat exchanger 3, and the shell side of the second heat exchanger 3 The nozzle at the top of the process is connected to the middle part of the heating furnace 4 inlet and the cracking reactor 5 respectively; the heating furnace 4 outlet is connected to the top of the cracking reactor 5;

The bottom of the cracking reactor 5 is connected to the top nozzle of the second heat exchanger 3 tubes, the bottom nozzle of the second heat exchanger 3 tubes is connected to the top nozzle of the first heat exchanger 2 tubes, and the first heat exchanger The bottom nozzle of the 2 tube side is connected with the top nozzle of the hot water heat exchanger 7 tube side, the bottom nozzle of the hot water heat exchanger 7 tube side is connected with the top nozzle of the pyrolysis product cooler 6 shell side, and the pyrolysis product cooler 6 shell The nozzle at the bottom of the process is connected to the inlet of the top of the gas-liquid separation tank 8, and the outlet of the bottom of the gas-liquid separation tank 8 is connected to the inlet of the reaction liquid pump 9; the outlet of the reaction liquid pump 9 is connected to the upper part of the absorption tower 14; The rich gas compressor 10 is connected; the rich gas compressor 10, the air cooler 11 at the outlet of the air compressor, the cooler 12 at the outlet of the air compressor, and the liquid separator tank 13 at the outlet of the air compressor are connected in sequence; the gas phase outlet at the top of the liquid separator tank 13 at the outlet of the air compressor is connected to the absorption tower The lower part of 14 is connected;

The absorption stabilization system includes: absorption tower 14, absorption tower middle section pump 15, absorption tower middle section cooler 16, absorption tower bottom oil pump 17, desorption tower 18, desorption tower feed pump 19, desorption tower feed heat exchanger 20. Desorption tower reboiler 21, stabilization tower 22, stabilization tower feed pump 23, stabilization tower feed heat exchanger 24, stabilization tower reboiler 25, stabilization tower top air cooler 26, stabilization tower top cooler 27, Stabilizing tower top reflux tank 28, stabilizing tower reflux pump 29, light hydrocarbon cooler 30, absorption oil pump 31, absorption oil cooler 32, dry gas separator tank 33;

The bottom of the absorption tower 14 is connected to the air compressor outlet air cooler 11 inlet through the absorption tower bottom oil pump 17, and the top of the absorption tower 14 is connected to the dry gas liquid separation tank 33; the top of the dry gas liquid separation tank 33 exchanges heat with the dry gas feed The bottom nozzle of the shell side of the device 34 is connected; the bottom of the dry gas separator tank 33 is connected with the inlet of the stabilizing tower reflux pump 29; connected to the nozzle at the bottom of the process;

In the middle of the absorption tower 14, the absorption tower middle section pump 15 and the absorption tower middle section cooler 16 are connected in parallel successively;

The desorption tower feed pump 19 links to each other with the top of the desorption tower 18, and the desorption tower feed pump 19 also links to each other with the top of the desorption tower 18 through the desorption tower feed heat exchanger 20;

The desorption tower 18 is provided with a desorption tower reboiler 21 at the bottom of the tower; the desorption tower 18 and the rich gas compressor 10 are all connected to the outlet air cooler 11 of the air compressor; Feed heat exchanger 24 links to each other with the middle part of stabilizing tower 22;

Stabilizing tower 22 is provided with stabilizing tower reboiler 25 at the bottom of the tower; The tank bottom of the tank 28 is respectively connected to the top of the stabilizing tower 22 and the feed preheater 41 of the depropanizer tower through a stabilizing tower top reflux pump 29;

The tower bottom of the stabilizing tower 22, the stabilizing tower feed heat exchanger 24, the desorption tower feed heat exchanger 20, and the light hydrocarbon cooler 30 are connected successively; the light hydrocarbon cooler 30 is connected with the stripping tower feed heat exchanger 48, The light hydrocarbon cooler 30 is also connected to the top of the absorption tower 14 via an absorption oil pump 31 and an absorption oil cooler 32 in sequence.

The aromatization reaction system includes: dry gas feed heat exchanger 34, dry gas electric heater 35, aromatization reactor 36, aromatization product cooler 37, aromatization product deep cooler 38 , aromatization product gas-liquid separation tank 39, dry gas cycler 40;

The top nozzle of the dry gas feed heat exchanger 34 is connected to the top of the aromatization reactor 36 through the dry gas electric heater 35; the top nozzle of the dry gas feed heat exchanger 34 is also connected to the aromatization reactor 34 The bottom of the reactor 36 is connected; the bottom of the tube side of the dry gas feed heat exchanger 34, the aromatization product cooler 37, the aromatization product deep cooler 38, and the aromatization product gas-liquid separation tank 39 are connected in sequence; the dry gas The top of the liquid separator tank 33 is connected to the middle part of the dry gas cycler 40 and the aromatization reactor 36 respectively;

The aromatization product gas-liquid separation tank 39 is connected to the heating furnace 4, and the aromatization product gas-liquid separation tank 39 also passes through the dry gas cycler 40, the dry gas feed heat exchanger 34, the dry gas electric heater 35 and the aromatization product in sequence. The texturization reactor 36 is connected.

The gas separation raw material gas concentration system includes: depropanizer feed preheater 41, depropanizer 42, depropanizer reboiler 43, depropanizer top air cooler 44, depropanizer top condenser 45. Depropanizer reflux tank 46, depropanizer reflux pump 47;

The tank bottom of the stabilizing tower top reflux tank 28 is connected successively with the depropanizer feed preheater 41 and the depropanizer 42 through the stabilizing tower reflux pump 29;

The top of the depropanizer 42 is connected in sequence with the depropanizer overhead air cooler 44, the depropanizer overhead condenser 45, the depropanizer overhead reflux tank 46, and the depropanizer overhead reflux pump 47 to form a loop; the depropanizer overhead reflux Pump 47 is also connected with gas separation device;

The depropanizer 42 is supplied with heat from the depropanizer reboiler 43 at the bottom of the tower, and the heat source is heat transfer oil.

The light hydrocarbon purification system includes: feed heat exchanger 48, electric heater 49, stripper 50, stripper reboiler 51, stripper top condenser 52, stripper top reflux tank 53 , stripper reflux pump 54, forced circulation pump 55;

The stripper feed heat exchanger 48 is connected to the stripper 50; the forced circulation pump 55 is connected to the heavy oil tank;

The stripper 50 is provided with a stripper reboiler 51 at the bottom of the column. The stripper 50 tower top is connected successively with the stripper feed heat exchanger 48, the stripper top condenser 52, the stripper top reflux tank 53, and the stripper reflux pump 54, and forms a loop; the stripper reflux The pump 54 is also connected to the gasoline tank.

It should be noted that the various equipment used in the present invention are all conventional equipment used in the production process in this field, and the operation and parameters of each equipment are all carried out according to conventional operations, and there is nothing special about them.

Claims (10)

1. A process for preparing hydrocarbon by utilizing liquefied gas comprises a cracking reaction process, an absorption stabilization process and an aromatization reaction process, and is characterized in that: also comprises a gas separation raw material gas concentration process and an aromatic hydrocarbon purification process;

wherein, the gas separation feed gas concentration process comprises the following steps:

the gas component feed gas in the absorption stabilization procedure enters a depropanizing tower feeding preheater from the bottom of a stabilization tower top reflux tank through a part of a stabilization tower reflux pump to be heated and then enters the depropanizing tower to separate carbon three and carbon four components;

the carbon three fraction is evaporated from the top of the depropanizing tower, cooled by a depropanizing tower top air cooler and a condenser and then enters a depropanizing tower top reflux tank, and condensate is divided into two parts after being pumped by a depropanizing tower reflux pump: one part is used as the reflux of the depropanizing tower, and the other part is used as the gas component raw material and sent to a gas component device or a gas component raw material tank for storage;

and (3) feeding the four carbon components discharged from the bottom of the depropanizing tower into an MTBE device to be used as raw materials to participate in reaction or feeding the raw materials into a four carbon raw material tank for storage.

2. The process for preparing hydrocarbons by processing liquefied gas according to claim 1, wherein the aromatic hydrocarbon purification process comprises:

aromatic hydrocarbon discharged from a light hydrocarbon cooler of a stabilizing tower in the absorption stabilizing procedure and an aromatization product gas-liquid separation tank in the aromatization reaction procedure exchanges heat with the gas phase at the top of a stripping tower through a feeding heat exchanger, and then enters the stripping tower from the middle section of the stripping tower;

the aromatic hydrocarbon entering the stripping tower and the original gasoline light aromatic hydrocarbon in the tower carry out mass transfer and heat transfer and are divided into a heavy component and a light component;

the heavy component moves down to the bottom of the tower and is further heated, and meanwhile, part of the heavy component is extracted and sent to a heavy oil tank for storage after being subjected to pressure increase by a forced circulation pump;

the light components are evaporated and lifted and fully vaporized, the lifted light components escape from the tower top to the feeding heat exchanger, are further cooled to 30 ℃ by a tower top condenser, enter a reflux tank, and are divided into two parts after being pressurized by a reflux pump: one part is extracted as an aromatic hydrocarbon product and sent to a gasoline tank for storage, and the other part enters a stripping tower from the top of the tower as reflux.

3. The process for producing hydrocarbons using liquefied gas according to claim 1, wherein the cracking reaction comprises:

a carbon four liquefied gas raw material in a cracking raw material tank passes through a raw material pump, sequentially passes through a first heat exchanger and a second heat exchanger to exchange heat with a cracking reaction product, the heat-exchanged carbon four raw material enters a heating furnace, the temperature is further raised to 500 ℃, and the gas with the raised temperature enters a cracking reactor from the top of the cracking reactor to perform cracking reaction;

the pyrolysis reaction product sequentially passes through a second heat exchanger, a first heat exchanger, a hot water heat exchanger and a pyrolysis product cooler from the bottom of the pyrolysis reactor for heat exchange and cooling until the temperature is reduced to 40 ℃, and then enters a gas-liquid separation tank for separation; the condensate obtained by separation is pumped into an absorption tower by a reaction liquid pump; and compressing and cooling the separated gas by a rich gas compressor.

4. The process for producing hydrocarbons using liquefied gas according to claim 1, wherein the absorption stabilization step comprises:

the gas compressed by the rich gas compressor in the cracking reaction process, the absorption oil from the bottom of the absorption tower and the desorption gas from the top of the desorption tower sequentially pass through an air cooler at the outlet of the gas compressor and a cooler at the outlet of the gas compressor, are cooled to 40 ℃ and then enter a liquid separation tank at the outlet of the gas compressor, so that the oil and the gas are separated;

separating out rich gas from the top of the liquid separating tank at the outlet of the gas compressor and conveying the rich gas to the lower part of the absorption tower, wherein the rich gas is in countercurrent contact with an absorbent entering from the upper part of the absorption tower in the absorption tower, the absorbed lean gas enters the dry gas liquid separating tank from the top of the absorption tower for gas-liquid separation, the liquid flows into a stabilizing tower for reflux, and the dry gas coming out from the top of the dry gas liquid separating tank is conveyed to an aromatization reactor;

pumping gasoline which circularly reflows from the middle section of the absorption tower by using a middle section pump of the absorption tower, cooling to 20 ℃ by a middle section cooler of the absorption tower, and returning to the absorption tower;

the condensate coming out of the bottom of the liquid separating tank at the outlet of the gas compressor is divided into two paths by a feeding pump of the desorption tower: one path directly enters the top of the desorption tower, and the other path enters the upper part of the desorption tower after heat exchange is carried out to 70 ℃ by a feeding heat exchanger of the desorption tower;

the desorption gas escapes from the tower top and is merged with the compressed rich gas of the rich gas compressor to enter an air cooler at the outlet of the gas compressor; the desorbed gasoline is pumped out from the bottom of the desorption tower by a stabilizing tower feed pump, exchanges heat with the stabilized gasoline at the bottom of the stabilizing tower through a stabilizing tower feed heat exchanger to 125 ℃, and then enters the middle part of the stabilizing tower;

and C4, distilling out the components of C four and C four from the top of the stabilizing tower, passing through an air cooler at the top of the stabilizing tower and a condenser at the top of the stabilizing tower, entering a reflux tank at the top of the stabilizing tower, and pumping the gas component feed gas from the bottom of the reflux tank at the top of the stabilizing tower through a reflux pump of the stabilizing tower to divide the gas component feed gas into two paths: one path of the reflux returns to the top of the stabilizing tower, and the other path of the reflux enters a feed preheater of the depropanizing tower;

the stabilized gasoline of the stabilizing tower is discharged from the bottom of the tower, and is cooled to 30 ℃ by a stabilizing tower feeding heat exchanger, a desorption tower feeding heat exchanger and a light hydrocarbon cooler in sequence, and then is divided into two parts: one part enters a feeding heat exchanger of the stripping tower to exchange heat with the product gasoline light aromatic hydrocarbon extracted by reflux at the top of the stripping tower, and then enters the stripping tower, and the other part is pressurized by an absorption oil pump, cooled to 20 ℃ by an absorption oil cooler and then sent to the top of the absorption tower to be used as an absorbent.

5. The process for producing hydrocarbons by using liquefied gas as claimed in claim 1, wherein the aromatization reaction comprises the following steps:

the dry gas from the top of the dry gas liquid separation tank in the absorption stabilization procedure is merged with the fuel gas of the dry gas circulator and then is divided into two parts: one part of the main line firstly enters a dry gas feeding heat exchanger to exchange heat with the gas after aromatization reaction, then enters the aromatization reactor from the top of the aromatization reactor after being further heated to 300 ℃ by a dry gas electric heater to contact with an aromatization catalyst for aromatization reaction; the other part of the mixture directly enters an aromatization reactor to carry out aromatization reaction;

the gas after aromatization reaction comes out from the bottom of the aromatization reactor and enters a dry gas feeding heat exchanger to exchange heat with raw dry gas, and then is cooled to 20 ℃ through an aromatization product cooler and an aromatization product deep cooler, and then enters an aromatization product gas-liquid separation tank to be subjected to gas-liquid separation, wherein the gas phase is divided into two parts: one part of the mixture enters a heating furnace to be used as fuel gas, and the other part of the mixture is compressed by a dry gas circulator and then returns to the aromatization reactor; the liquid phase enters a stripper feed heat exchanger.

6. An apparatus for implementing a process for preparing hydrocarbons by processing liquefied gas according to claim 1, comprising a cracking reaction system, an absorption stabilization system, an aromatization reaction system, a gas component feed gas concentration system, an aromatic hydrocarbon purification system which are sequentially communicated;

wherein, gas divides feed gas concentration system, include: a depropanizing tower feeding preheater (41), a depropanizing tower (42), a depropanizing tower top air cooler (44), a depropanizing tower top condenser (45), a depropanizing tower top reflux tank (46) and a depropanizing tower reflux pump (47);

the bottom of a reflux tank (28) at the top of the stabilizing tower is sequentially connected with a feed preheater (41) of a depropanizing tower and a depropanizing tower (42) through a reflux pump (29) of the stabilizing tower;

the top of the depropanizing tower (42) is connected with a depropanizing tower top air cooler (44), a depropanizing tower top condenser (45), a depropanizing tower top reflux tank (46) and a depropanizing tower top reflux pump (47) in sequence to form a loop; the top reflux pump (47) of the depropanization tower is also connected with a gas separation device.

7. An apparatus for processing hydrocarbons using liquefied gas according to claim 6, wherein:

the light hydrocarbon purification system comprises: a feeding heat exchanger (48), an electric heater (49), a stripping tower (50), a stripping tower top condenser (52), a stripping tower top reflux tank (53), a stripping tower reflux pump (54) and a forced circulation pump (55);

the stripper column feed heat exchanger (48) is connected with the stripper column (50); the forced circulation pump (55) is connected with the heavy oil tank;

the top of the stripping tower (50) is connected with a stripping tower feeding heat exchanger (48), a stripping tower top condenser (52), a stripping tower top reflux tank (53) and a stripping tower reflux pump (54) in sequence to form a loop; the stripper return pump (54) is also connected to the gasoline tank.

8. An apparatus for processing hydrocarbons using liquefied gas according to claim 6, wherein:

the cracking reaction system comprises: the system comprises a raw material pump (1), a first heat exchanger (2), a second heat exchanger (3), a heating furnace (4), a cracking reactor (5), a reaction product cooler (6), a hot water heat exchanger (7), a gas-liquid separation tank (8), a reaction liquid pump (9), a rich gas compressor (10), a gas compressor outlet air cooler (11), a gas compressor outlet cooler (12) and a gas compressor outlet liquid separation tank (13);

an outlet of the raw material pump (1) is connected with a shell pass bottom pipe orifice of the first heat exchanger (2), a shell pass top pipe orifice of the first heat exchanger (2) is connected with a shell pass bottom pipe orifice of the second heat exchanger (3), and a shell pass top pipe orifice of the second heat exchanger (3) is respectively connected with an inlet of the heating furnace (4) and the middle part of the cracking reactor (5); the outlet of the heating furnace (4) is connected with the top of the cracking reactor (5);

the bottom of the cracking reactor (5) is connected with a tube side top pipe orifice of the second heat exchanger (3), a tube side bottom pipe orifice of the second heat exchanger (3) is connected with a tube side top pipe orifice of the first heat exchanger (2), a tube side bottom pipe orifice of the first heat exchanger (2) is connected with a tube side top pipe orifice of the hot water heat exchanger (7), a tube side bottom pipe orifice of the hot water heat exchanger (7) is connected with a shell side top pipe orifice of the cracking product cooler (6), a shell side bottom pipe orifice of the cracking product cooler (6) is connected with a top inlet of the gas-liquid separation tank (8), and a bottom outlet of the gas-liquid separation tank (8) is connected with an inlet of a reaction liquid pump (9); the outlet of the reaction liquid pump (9) is connected with the upper part of the absorption tower (14); a gas phase outlet at the top of the gas-liquid separation tank (8) is connected with a rich gas compressor (10); the rich gas compressor (10), the air cooler (11) at the outlet of the aerostatic press, the cooler (12) at the outlet of the aerostatic press and the liquid separation tank (13) at the outlet of the aerostatic press are connected in sequence; a gas phase outlet at the top of the gas compressor outlet liquid separation tank (13) is connected with the lower part of the absorption tower (14); the outlet at the bottom of the liquid separation tank (13) at the outlet of the gas compressor is connected with a feed pump (19) of the desorption tower.

9. An apparatus for processing hydrocarbons using liquefied gas according to claim 6, wherein:

the absorption stabilization system comprises: the device comprises an absorption tower (14), an absorption tower middle-section pump (15), an absorption tower middle-section cooler (16), an absorption tower bottom oil pump (17), a desorption tower (18), a desorption tower feed pump (19), a desorption tower feed heat exchanger (20), a stabilization tower (22), a stabilization tower feed pump (23), a stabilization tower feed heat exchanger (24), a stabilization tower top air cooler (26), a stabilization tower top cooler (27), a stabilization tower top reflux tank (28), a stabilization tower reflux pump (29), a light hydrocarbon cooler (30), an absorption oil pump (31), an absorption oil cooler (32) and a dry gas liquid separation tank (33);

the bottom of the absorption tower (14) is connected with the inlet of an air cooler (11) at the outlet of the air compressor through an oil pump (17) at the bottom of the absorption tower, and the top of the absorption tower (14) is connected with a dry gas liquid separation tank (33); the top of the dry gas liquid separation tank (33) is connected with a shell pass bottom pipe orifice of a dry gas feeding heat exchanger (34); the bottom of the dry gas liquid separation tank (33) is connected with the inlet of a reflux pump (29) of the stabilizing tower; the outlet of the stabilizing tower reflux pump (29) is connected with the upper part of the stabilizing tower (22) and the pipe orifice at the bottom of the pipe pass of the depropanizing tower feeding preheater (41);

an absorption tower middle section pump (15) and an absorption tower middle section cooler (16) are sequentially connected in parallel in the middle of the absorption tower (14);

a desorption tower feed pump (19) is connected with the top of the desorption tower (18), and the desorption tower feed pump (19) is also connected with the upper part of the desorption tower (18) through a desorption tower feed heat exchanger (20);

the desorption tower (18) and the rich gas compressor (10) are both connected with an air cooler (11) at the outlet of the gas compressor; the bottom of the desorption tower (18) is connected with the middle part of the stabilizing tower (22) through a stabilizing tower feeding pump (23) and a stabilizing tower feeding heat exchanger (24) in sequence;

the top of the stabilizer (22) is connected with a reflux tank (28) at the top of the stabilizer through an air cooler (26) at the top of the stabilizer and a condenser (27) at the top of the stabilizer in sequence; the bottom of the stabilizing tower top reflux tank (28) is respectively connected with the top of the stabilizing tower (22) and a depropanizer feeding preheater (41) through a stabilizing tower top reflux pump (29);

the bottom of the stabilizer (22) is connected with the stabilizer feeding heat exchanger (24), the desorber feeding heat exchanger (20) and the light hydrocarbon cooler (30) in sequence: the light hydrocarbon cooler (30) is connected with the feeding heat exchanger (48) of the stripping tower, and the light hydrocarbon cooler (30) is also connected with the top of the absorption tower (14) through the absorption oil pump (31) and the absorption oil cooler (32) in sequence.

10. An apparatus for processing hydrocarbons using liquefied gas according to claim 6, wherein: the aromatization reaction system comprises: a dry gas feeding heat exchanger (34), a dry gas electric heater (35), an aromatization reactor (36), an aromatization product cooler (37), an aromatization product deep cooler (38), an aromatization product gas-liquid separation tank (39) and a dry gas circulating machine (40);

a shell side top pipe orifice of the dry gas feeding heat exchanger (34) is connected with the top of the aromatization reactor (36); the tube side top orifice of the dry gas feeding heat exchanger (34) is connected with the bottom of the aromatization reactor (36); the bottom of the tube pass of the dry gas feeding heat exchanger (34) is connected with an aromatization product cooler (37), an aromatization product deep cooler (38) and an aromatization product gas-liquid separation tank (39) in sequence; the top of the dry gas liquid separation tank (33) is respectively connected with the dry gas circulator (40) and the middle part of the aromatization reactor (36);

the aromatization product gas-liquid separation tank (39) is connected with the heating furnace (4), and the aromatization product gas-liquid separation tank (39) is also connected with the aromatization reactor (36) through a dry gas circulator (40).

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