Device and method for heating feed for cracking gasoline hydrogenation reaction

Abstract

The invention belongs to the technical field of oil refining and chemical industry, and discloses a device and method for heating a pyrolysis gasoline hydrogenation reaction feed, the device comprises a feed heater, a feed inlet and a feed outlet heat exchanger is arranged on the discharge pipeline of the hydrogenation reactor, the hydrogenation reaction feed pipeline is connected to the feed inlet of the feed heater through the feed inlet and a feed outlet heat exchanger, the discharge inlet of the feed heater is connected to the feed inlet of the hydrogenation reactor, the steam side inlet of the feed heater is connected to the high-pressure steam pipeline, two regulating valves, one large and one small, are arranged in parallel on the high-pressure steam pipeline, the steam side outlet of the feed heater is connected to the reboiler steam pipeline of the separation system through the secondary steam pipeline, and the secondary steam pipeline upstream of the separation system is connected to a medium-pressure steam main pipe. The device and method can meet the temperature requirements of the hydrogenation reaction feed, are environmentally friendly and can be flexibly adjusted.

Description

Technical Field

[0001] The invention belongs to the technical field of oil refining and chemical engineering, and in particular relates to a device and method for heating feed for a cracking gasoline hydrogenation reaction. Background Art

[0002] Pyrolysis gasoline (also known as "heavy pyrolysis gasoline (pygas)") is a liquid byproduct of the steam cracking process for producing ethylene and propylene. Pyrolysis gasoline is a mixture of highly unsaturated hydrocarbons (carbon range of about C5-C14) rich in dienes, olefins and aromatics, especially benzene, and also includes heteroatom-containing hydrocarbons, such as sulfur and nitrogen-containing compounds. If pyrolysis gasoline is not treated, it is usually degraded in the fuel system to produce gums and lacquers. In order to increase the utilization value of pyrolysis gasoline and make it usable as a gasoline blending stock, pyrolysis gasoline must be at least partially hydrogenated or hydrotreated to reduce the unsaturation and heteroatom-containing hydrocarbon content.

[0003] The hydrogenation saturation and desulfurization of pyrolysis gasoline are gas phase reactions. According to the principle of chemical reaction, the hydrogenation of unsaturated hydrocarbons is an exothermic reaction. The existing pyrolysis gasoline hydrogenation device is equipped with an inlet and outlet heat exchanger and a heating furnace at the inlet of the gas phase reactor. The inlet and outlet heat exchanger is used to recover the heat released by the hydrogenation reaction, and the heating furnace ensures that the feed temperature of the hydrogenation reaction reaches the starting temperature required by the reaction. In the initial stage of the device operation, the hydrogenation reaction has not yet started, the reaction heat release is small, and the heat load of the heating furnace is high; when the normal reaction temperature is reached, the heat release of the hydrogenation reaction increases, the inlet and outlet heat exchanger efficiently recovers the reaction heat, the external supplementary heat required by the system becomes smaller, and the heat load of the heating furnace is reduced. However, since the heating furnace does not have the low-load regulation characteristics, when the heat load is low and the fuel gas flow rate is small, it is easy to cause the burner of the heating furnace to flame out, which brings serious safety hazards to the device. At the same time, sulfur-containing and carbon dioxide-containing flue gas will also be generated during the combustion of the fuel gas, which will be directly discharged to cause environmental pollution.

[0004] Patent document CN104560161A discloses a method for heating the inlet material of the second-stage reactor of a cracking gasoline hydrogenation unit. The second-stage feed is heated by high-pressure steam instead of a heating furnace. The operating pressure of the high-pressure steam heat exchanger is greater than 6.0 MPaG, and the material is heated by the condensation latent heat of the high-pressure steam. The operating pressure is high and the safety is low. Heating the material by the condensation latent heat is not conducive to the regulation at low load and the operation is not flexible. Summary of the invention

[0005] In view of the above problems existing in the prior art, the purpose of the present invention is to provide a device and method for heating the feed of pyrolysis gasoline hydrogenation reaction, which can meet the environmental protection requirements and ensure flexible and reliable adjustment according to the use characteristics of the feed heater.

[0006] The first aspect of the present invention provides a device for heating a feed for a pyrolysis gasoline hydrogenation reaction. The pyrolysis gasoline hydrogenation treatment device comprises a hydrogenation reactor and a separation system. The device comprises a feed heater. An inlet and outlet heat exchanger is arranged on the discharge pipeline of the hydrogenation reactor. The hydrogenation reaction feed pipeline is connected to a feed port of the feed heater through the inlet and outlet heat exchanger. The discharge port of the feed heater is connected to the feed port of the hydrogenation reactor. The steam side inlet of the feed heater is connected to a high-pressure steam pipeline. Two regulating valves, one large and one small, are arranged in parallel on the high-pressure steam pipeline. The steam side outlet of the feed heater is connected to a reboiler steam pipeline of a separation system through a secondary steam pipeline. The secondary steam pipeline upstream of the separation system is connected to a medium-pressure steam main pipe.

[0007] The second aspect of the present invention provides a method for heating a pyrolysis gasoline hydrogenation reaction feed using the above-mentioned device, the method comprising:

[0008] 1) Hydrogenation reaction start-up stage: first, medium-pressure steam is introduced from the secondary steam pipeline to preheat the feed heater and its steam side pipeline, then high-pressure steam is introduced from the high-pressure steam pipeline to heat the hydrogenation reaction feed through the feed heater, and the high-pressure steam is reduced in pressure and the steam flow is controlled through the regulating valve on the high-pressure steam pipeline. The secondary steam at the outlet of the steam side of the feed heater is used as a supplementary heat source for the separation system;

[0009] 2) After the hydroprocessing unit runs smoothly: If the temperature rise of the hydrogenation reaction is low, the temperature of the hydrogenation reaction feed after passing through the inlet and outlet heat exchanger is lower than the hydrogenation reaction temperature, the temperature switch that adjusts the opening of the bypass regulating valve of the inlet and outlet heat exchanger is adjusted to the outlet temperature of the cold side of the inlet and outlet heat exchanger, and the temperature of the hydrogenation reaction feed is controlled by adjusting the size regulating valve on the high-pressure steam pipeline, and the feed heater supplements heat for the system; If the temperature rise of the hydrogenation reaction is high, the temperature of the hydrogenation reaction feed can reach the hydrogenation reaction temperature after passing through the inlet and outlet heat exchanger, the temperature switch that adjusts the opening of the bypass regulating valve of the inlet and outlet heat exchanger is adjusted to the feed inlet temperature of the hydrogenation reactor, and the feed heater is disabled.

[0010] Compared with the prior art, the present invention has the following advantages:

[0011] (1) The present invention adopts a feed heater with steam as a heat source to replace the existing heating furnace to heat the hydrogenation reaction feed, while avoiding defects such as excessive operating pressure of the feed heater, poor safety and regulation performance, etc., to achieve timely response and stable regulation of process fluctuations, improve operational safety, and improve the environmental protection indicators of the device. It can not only achieve high-load external heat supplement to meet the needs of device start-up, but also achieve continuous operation of small-load heat supply, achieve the goal of zero smoke emission of the device, and low-carbon and environmentally friendly operation, which is more green and environmentally friendly.

[0012] (2) The feed heater uses high-temperature steam after decompression, and uses the sensible heat of steam to heat the hydrogenation reaction feed. The steam dosage can be adjusted from 0 to Fmax, with a wide adjustment range, which overcomes the difficulty that the fuel gas of the heating furnace cannot be adjusted from 0 to the lower limit of Fmax, thereby improving the flexibility and safety of the device operation.

[0013] (3) The present invention utilizes steam for two consecutive thermal utilizations: the first thermal utilization is to use the sensible heat of steam to heat the hydrogenation reaction feed, and the regulating valve accurately controls the steam dosage and adjusts the reaction feed temperature. The secondary steam after use enters the separation system again, and the latent heat of steam is used to heat the separation system materials. The steam condensate finally generated is discharged from the device; the two thermal utilizations not only meet the high-temperature heat demand, but also fully recover the calorific value of steam, thereby maintaining the advanced energy consumption of the device.

[0014] (4) The device and method of the present invention not only ensure that the heat load of the feed heater required for the hydrogenation reaction feed to be supplemented with heat during the start-up phase of the device is relatively high, but also solve the problem of low-load heat supplementation regulation when the heat release of the hydrogenation reaction is unstable, thereby improving the stability and safety of the device operation; the present invention replaces fuel gas with steam, thereby overcoming the problem that the open flame heating furnace cannot be adjusted at low load, and is easily affected by the environment under low load conditions, causing flameout and deflagration. The calorific value of steam is fully recovered through the secondary utilization of steam, thereby reducing the energy consumption of the device and improving environmental indicators.

[0015] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] The accompanying drawings are used to provide further understanding of the present invention and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present invention, but do not constitute a limitation of the present invention.

[0017] Figure 1 The present invention is a schematic diagram of a process flow of a device for heating feed for pyrolysis gasoline hydrogenation reaction according to a specific embodiment of the present invention.

[0018] Figure 2 The invention is a process flow diagram of a pyrolysis gasoline hydrogenation reaction feed heating device used in the prior art.

[0019] Description of Reference Numerals

[0020] 1 Inlet and outlet heat exchanger; 2 Feed heater; 3 Hydrogenation reactor; 4 Steam trap group; 5 Separation system; 6 Heating furnace; S-1 Hydrogenation reaction feed pipeline; S-2 High-pressure steam pipeline; S-3 Secondary steam pipeline; S-4 Steam condensate pipeline; S-5 Steam condensate discharge pipeline; S-6 Fuel gas pipeline; S-7 Medium-pressure steam main. DETAILED DESCRIPTION

[0021] In order to make the present invention more easily understood, the present invention will be described in detail below in conjunction with the embodiments and the accompanying drawings. These embodiments are only for illustration and are not intended to limit the present invention.

[0022] According to a first aspect of the present invention, the present invention provides a device for heating a feed for a pyrolysis gasoline hydrogenation reaction. The pyrolysis gasoline hydrogenation treatment device comprises a hydrogenation reactor and a separation system. The device comprises a feed heater. An inlet and outlet heat exchanger is provided on the discharge pipeline of the hydrogenation reactor. The hydrogenation reaction feed pipeline is connected to a feed port of the feed heater through the inlet and outlet heat exchanger. The discharge port of the feed heater is connected to the feed port of the hydrogenation reactor. The steam side inlet of the feed heater is connected to a high-pressure steam pipeline. Two regulating valves, one large and one small, are provided in parallel on the high-pressure steam pipeline. The steam side outlet of the feed heater is connected to a reboiler steam pipeline of a separation system through a secondary steam pipeline. A medium-pressure steam main is connected to the secondary steam pipeline upstream of the separation system.

[0023] According to the present invention, there are two regulating valves, one large and one small, on the high-pressure steam pipeline. The large regulating valve is used for flow regulation when the steam consumption is high. In particular, the large regulating valve is used for flow regulation during the start-up phase of the hydrogenation reactor. The small regulating valve is used for flow regulation under conditions of low steam consumption. In particular, under conditions where a small amount of heat needs to be supplemented during normal operation of the hydrogenation reactor.

[0024] In the present invention, a feed inlet and feed outlet heat exchanger bypass regulating valve is provided on the discharge pipeline of the hydrogenation reactor, and the feed inlet and feed outlet heat exchanger and the feed inlet and feed outlet heat exchanger bypass regulating valve are arranged in parallel; the opening of the feed inlet and feed outlet heat exchanger bypass regulating valve is adjusted by selecting the cold side outlet temperature of the feed inlet and feed outlet of the hydrogenation reactor through a temperature switch.

[0025] Preferably, the opening of the regulating valve on the high-pressure steam pipeline is adjusted by the hydrogenation reaction feed temperature at the cold side outlet of the feed heater.

[0026] Preferably, the steam side outlet of the feed heater is provided with a condensate discharge pipeline connected in parallel with the secondary steam pipeline, and the condensate discharge pipeline is connected to the steam condensate pipeline through a steam trap group. The secondary steam pipeline is set up to use the secondary steam of the high-pressure steam as a supplementary heat source for the separation system in the device. The condensate discharge pipeline is set up to introduce medium-pressure steam to preheat and drain the steam side equipment and pipelines during the start-up phase. In addition, it should be noted that the medium-pressure steam outlet of the medium-pressure steam main is located between the separation system and the condensate inlet of the condensate discharge pipeline, and is close to the separation system. Preheating is provided by the medium-pressure steam main connected to the secondary steam pipeline to provide medium-pressure steam. In the preheating stage, the flow direction of the medium-pressure steam is opposite to that of the secondary steam. For this reason, a one-way valve in parallel with the valve controlling the flow direction of the secondary steam on the secondary steam pipeline can be set to control the flow direction of the medium-pressure steam.

[0027] In the present invention, a steam condensate discharge pipeline is provided on the separation system.

[0028] System components not limited in the present invention can be conventionally selected according to the existing technology and belong to conventional technical means, such as valves provided on the condensate discharge pipeline and the secondary steam pipeline.

[0029] According to a second aspect of the present invention, the present invention provides a method for heating a pyrolysis gasoline hydrogenation reaction feed using the above-mentioned device, the method comprising:

[0030] 1) Hydrogenation reaction start-up stage: first, medium-pressure steam is introduced from the secondary steam pipeline to preheat the feed heater and its steam side pipeline, then high-pressure steam is introduced from the high-pressure steam pipeline to heat the hydrogenation reaction feed through the feed heater, and the high-pressure steam is reduced in pressure and the steam flow is controlled through the regulating valve on the high-pressure steam pipeline. The secondary steam at the outlet of the steam side of the feed heater is used as a supplementary heat source for the separation system;

[0031] 2) After the hydroprocessing unit runs smoothly: If the temperature rise of the hydrogenation reaction is low, the temperature of the hydrogenation reaction feed after passing through the inlet and outlet heat exchanger is lower than the hydrogenation reaction temperature, the temperature switch that adjusts the opening of the bypass regulating valve of the inlet and outlet heat exchanger is adjusted to the outlet temperature of the cold side of the inlet and outlet heat exchanger, and the temperature of the hydrogenation reaction feed is controlled by adjusting the size regulating valve on the high-pressure steam pipeline, and the feed heater supplements heat for the system; If the temperature rise of the hydrogenation reaction is high, the temperature of the hydrogenation reaction feed can reach the hydrogenation reaction temperature after passing through the inlet and outlet heat exchanger, the temperature switch that adjusts the opening of the bypass regulating valve of the inlet and outlet heat exchanger is adjusted to the feed inlet temperature of the hydrogenation reactor, and the feed heater is disabled.

[0032] According to the present invention, the medium-pressure steam has a temperature of 150-300° C. and a pressure of 1.0-1.8 MPaG. The medium-pressure steam is introduced to preheat the feed heater and its steam-side pipeline.

[0033] Preferably, the temperature of the high-pressure steam is 320-420° C. and the pressure is greater than 2.0 MPaG.

[0034] Preferably, the operating pressure on the steam side of the feed heater is 1.0-1.8 MPaG.

[0035] Preferably, the pressure of the secondary steam is 1.0-1.8 MPaG, and the temperature of the secondary steam is at least 10° C. higher than the saturation temperature at the corresponding pressure.

[0036] In the present invention, the hydrogenation reaction temperature may be 200-350°C.

[0037] The process parameters not limited in the present invention can be conventionally set according to the prior art.

[0038] The present invention will be described in detail below by way of examples.

[0039] Example

[0040] This embodiment is used to illustrate the device and method for heating the feed of the pyrolysis gasoline hydrogenation reaction of the present invention.

[0041] like Figure 1 As shown, the present invention provides a device for heating a pyrolysis gasoline hydrogenation reaction feed, the device comprising a feed heater 2, an inlet and outlet heat exchanger 1 is arranged on the discharge pipeline of the hydrogenation reactor 3, the hydrogenation reaction feed pipeline S-1 is connected to the feed port of the feed heater 2 through the inlet and outlet heat exchanger 1, the discharge port of the feed heater 2 is connected to the feed port of the hydrogenation reactor 3, the steam side inlet of the feed heater 2 is connected to the high-pressure steam pipeline S-2, two regulating valves, one large and one small, are arranged in parallel on the high-pressure steam pipeline S-2, the steam side outlet of the feed heater 2 is connected to the reboiler steam pipeline of the separation system 5 through the secondary steam pipeline S-3, and the secondary steam pipeline S-3 upstream of the separation system 5 is connected to a medium-pressure steam main pipe S-7.

[0042] The discharge pipeline of the hydrogenation reactor 3 is provided with an inlet and outlet heat exchanger bypass regulating valve, and the inlet and outlet heat exchanger 1 is arranged in parallel with the inlet and outlet heat exchanger bypass regulating valve; the opening of the inlet and outlet heat exchanger bypass regulating valve is adjusted by selecting the cold side outlet temperature of the inlet and outlet heat exchanger 1 or the feed inlet temperature of the hydrogenation reactor 3 through the temperature switch. The opening of the regulating valve on the high-pressure steam pipeline S-2 is adjusted by the hydrogenation reaction feed temperature at the cold side outlet of the feed heater 2. The steam side outlet of the feed heater 2 is provided with a condensate discharge pipeline in parallel with the secondary steam pipeline S-3, and the condensate discharge pipeline is connected to the steam condensate pipeline S-4 through the steam trap group 4. The separation system 5 is provided with a steam condensate discharge pipeline S-5.

[0043] Taking a 400,000 t / a pyrolysis gasoline hydrogenation unit as an example, a method for heating feed for pyrolysis gasoline hydrogenation reaction using the above-mentioned unit comprises:

[0044] 1) Hydrogenation reaction start-up stage: first, medium-pressure steam is introduced from the secondary steam pipeline S-3, the temperature of the medium-pressure steam is 300°C and the pressure is 1.3MPaG, the feed heater 2 and its steam side pipeline are preheated, and then high-pressure steam is introduced from the high-pressure steam pipeline S-2, the temperature of the high-pressure steam is 420°C and the pressure is 3.4MPaG, the feed for hydrogenation reaction is heated by the feed heater 2, the operating pressure of the steam side of the feed heater is 1.35MPaG, the operating temperature is 406°C, the high-pressure steam is decompressed and the steam flow rate is controlled by the regulating valve on the high-pressure steam pipeline S-2 to ensure the feed temperature of hydrogenation reaction, the secondary steam at the steam side outlet of the feed heater 2 is used as a supplementary heat source for the separation system 5, the pressure of the secondary steam is 1.3MPaG, and the temperature of the secondary steam is 280°C;

[0045] 2) After the hydroprocessing unit runs smoothly: If the temperature rise of the hydrogenation reaction is low, the temperature of the hydrogenation reaction feed after passing through the inlet and outlet heat exchanger 1 is lower than the hydrogenation reaction temperature, and the hydrogenation reaction temperature is 240°C, the temperature switch for adjusting the opening of the bypass regulating valve of the inlet and outlet heat exchanger is adjusted to the cold side outlet temperature of the inlet and outlet heat exchanger 1, and the temperature of the hydrogenation reaction feed is controlled by adjusting the size regulating valve on the high-pressure steam pipeline S-2, and the feed heater 2 supplements heat for the system; If the temperature rise of the hydrogenation reaction is high, the temperature of the hydrogenation reaction feed can reach the hydrogenation reaction temperature after passing through the inlet and outlet heat exchanger, the temperature switch for adjusting the opening of the bypass regulating valve of the inlet and outlet heat exchanger is adjusted to the feed inlet temperature of the hydrogenation reactor 3, and the feed heater 2 is disabled.

[0046] Comparative Example

[0047] like Figure 2 As shown, a pyrolysis gasoline hydrogenation reaction feed heating device is currently used in the industry, and a heating furnace 6 is used to heat the feed in the hydrogenation reaction feed pipeline S-1.

[0048] At the initial stage of the device operation, the hydrogenation reaction in the hydrogenation reactor 3 has not yet started, the reaction heat release is small, and the heat load of the heating furnace 6 is high; when the normal reaction temperature is reached, the heat release of the hydrogenation reaction increases, the inlet and outlet heat exchanger 1 efficiently recovers the reaction heat, the external supplementary heat required by the system becomes smaller, and the heat load of the heating furnace 6 is reduced. However, since the heating furnace 6 does not have the low-load regulation characteristics, when the heat load is low and the fuel gas flow in the fuel gas pipeline S-6 is small, it is easy to cause the heating furnace burner to flame out, which brings serious safety hazards to the device. At the same time, sulfur-containing and carbon dioxide-containing flue gases will also be generated during the combustion of the fuel gas, which will be directly discharged to cause environmental pollution.

[0049] The characteristics of the embodiments and comparative examples are compared in Table 1.

[0050] Table 1

[0051]

[0052]

[0053] The embodiments of the present invention have been described above, and the above description is exemplary, not exhaustive, and is not limited to the disclosed embodiments. Many modifications and variations will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. A method for heating feed for pyrolysis gasoline hydrogenation reaction, characterized in that: The method adopts a device for heating the feed of the pyrolysis gasoline hydrogenation reaction, the device comprises a feed heater, the pyrolysis gasoline hydrogenation treatment device comprises a hydrogenation reactor and a separation system, an inlet and outlet heat exchanger is arranged on the discharge pipeline of the hydrogenation reactor, the hydrogenation reaction feed pipeline is connected to the feed port of the feed heater through the inlet and outlet heat exchanger, the discharge port of the feed heater is connected to the feed port of the hydrogenation reactor, the steam side inlet of the feed heater is connected to the high-pressure steam pipeline, two regulating valves, one large and one small, are arranged in parallel on the high-pressure steam pipeline, the steam side outlet of the feed heater is connected to the reboiler steam pipeline of the separation system through a secondary steam pipeline, and the secondary steam pipeline upstream of the separation system is connected to a medium-pressure steam main pipe; The discharge pipeline of the hydrogenation reactor is provided with an inlet and outlet heat exchanger bypass regulating valve, and the inlet and outlet heat exchanger and the inlet and outlet heat exchanger bypass regulating valve are arranged in parallel; The method includes: 1) Hydrogenation reaction start-up stage: first, medium-pressure steam is introduced from the secondary steam pipeline to preheat the feed heater and its steam side pipeline, then high-pressure steam is introduced from the high-pressure steam pipeline, and the feed for hydrogenation reaction is heated through the feed heater. The high-pressure steam is depressurized and the steam flow rate is controlled through the regulating valve on the high-pressure steam pipeline. The secondary steam at the outlet of the steam side of the feed heater is used as a supplementary heat source for the separation system; the temperature of the high-pressure steam is 320-420°C and the pressure is greater than 2.0MPaG; the operating pressure of the steam side of the feed heater is 1.0-1.8MPaG; the temperature of the medium-pressure steam is 150-300°C and the pressure is 1.0-1.8MPaG; the pressure of the secondary steam is 1.0-1.8MPaG, and the temperature of the secondary steam is at least 10°C higher than the saturation temperature at the corresponding pressure; 2) After the hydroprocessing unit runs smoothly: If the temperature rise of the hydrogenation reaction is low, the temperature of the hydrogenation reaction feed after passing through the inlet and outlet heat exchangers is lower than the hydrogenation reaction temperature, the temperature switch that adjusts the opening of the bypass regulating valve of the inlet and outlet heat exchangers is adjusted to the outlet temperature of the cold side of the inlet and outlet heat exchangers, and the temperature of the hydrogenation reaction feed is controlled by adjusting the size regulating valves on the high-pressure steam pipeline, and the feed heater supplements heat for the system; If the temperature rise of the hydrogenation reaction is high, the temperature of the hydrogenation reaction feed can reach the hydrogenation reaction temperature after passing through the inlet and outlet heat exchangers, the temperature switch that adjusts the opening of the bypass regulating valve of the inlet and outlet heat exchangers is adjusted to the feed inlet temperature of the hydrogenation reactor, and the feed heater is disabled.

2. The method for heating feed for pyrolysis gasoline hydrogenation reaction according to claim 1, wherein: The opening of the regulating valve on the high-pressure steam pipeline is adjusted by the hydrogenation reaction feed temperature at the cold side outlet of the feed heater; the opening of the inlet and outlet heat exchanger bypass regulating valve is adjusted by selecting the cold side outlet temperature of the inlet and outlet heat exchanger or the feed inlet temperature of the hydrogenation reactor through the temperature switch.

3. The method for heating feed for pyrolysis gasoline hydrogenation reaction according to claim 1, wherein: The steam side outlet of the feed heater is provided with a condensate discharge pipeline connected in parallel with the secondary steam pipeline, and the condensate discharge pipeline is connected to the steam condensate pipeline through a steam trap group.

4. The method for heating feed for pyrolysis gasoline hydrogenation reaction according to claim 1, wherein: The separation system is provided with a steam condensate discharge pipeline.

5. The method for heating feed for pyrolysis gasoline hydrogenation reaction according to claim 1, wherein: The hydrogenation reaction temperature is 200-350°C.

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