High amine synthesis system and process
By using ethylenediamine as a raw material for catalytic dehydration condensation reaction, the problems of high raw material toxicity, severe equipment corrosion, and environmental pollution in traditional high-amine synthesis routes have been solved, realizing the green synthesis and flexible production of high value-added products, and reducing costs and environmental risks.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-09-16
- Publication Date
- 2026-04-17
AI Technical Summary
Traditional high-amine synthesis routes suffer from problems such as high toxicity of raw materials, severe equipment corrosion, serious environmental pollution, and inflexible product distribution.
Using ethylenediamine as a raw material, high-value-added ethylenediamine products are generated through catalytic dehydration condensation reaction. Environmentally friendly catalysts and optimized process conditions are used to reduce the generation of inorganic waste salts, reduce equipment corrosion, and achieve flexible control of product distribution.
It reduces process safety risks and environmental pollution, reduces equipment investment and maintenance costs, and achieves greater flexibility in product distribution and improved economic benefits.
Smart Images
Figure CN121869208A_ABST
Abstract
Description
Technical Field
[0001] This invention relates to the field of high amine synthesis technology, specifically to a high amine synthesis system and process. Background Technology
[0002] 1. Raw material toxicity and process safety defects Traditional route (ethane chloroform / hydrogen cyanide process): Uses ethane chloroform and hydrogen cyanide (HCN) as raw materials. Both substances are highly toxic, volatile, and extremely dangerous chemicals. Ethyl chloride is a flammable and explosive gas, while HCN is a highly toxic substance that can be fatal if inhaled. This places extremely high demands on the safety of raw material storage, transportation, and production processes, and carries very high risks.
[0003] 2. Environmentally unfriendly and deficiencies in the treatment of "three wastes" (waste gas, wastewater, and solid waste). Traditional Route: This route is a classic source of major "three wastes" (waste gas, wastewater, and solid waste). Waste residue: The reaction produces large amounts of inorganic salt byproducts (e.g., sodium chloride is produced when using ethane chloride). For every ton of product produced, several tons of waste salt may be generated. Treating this waste salt requires costly incineration or landfill, which easily causes environmental pollution. Wastewater: Process wastewater contains unreacted raw materials, byproduct salts, and organic impurities. It has high salt content, poor biodegradability, and is extremely difficult and costly to treat. Waste gas: It may contain volatile halogenated hydrocarbons or HCN, requiring complex absorption and destruction treatment equipment.
[0004] 3. Equipment corrosion and maintenance cost deficiencies Traditional approach: The reaction system typically contains chloride ions (from chlorinating agents such as chloroethane) or cyanide ions, which are extremely corrosive to reaction equipment and pipelines under high temperature and pressure conditions. This forces plants to use expensive special alloy materials (such as Hastelloy and duplex steel) to manufacture equipment, resulting in huge fixed asset investments. At the same time, equipment corrosion also leads to higher maintenance costs and shorter maintenance cycles.
[0005] 4. Product distribution flexibility deficiency Traditional route: While it may offer higher selectivity, its product distribution is constrained by the inherent characteristics of the chemical reaction itself, resulting in limited flexibility in adjusting product distribution (such as flexibly adjusting the DETA / TETA ratio). It typically requires changing the raw materials or reaction conditions, which may introduce new problems. Summary of the Invention
[0006] In view of the shortcomings of the prior art, the present invention provides a high-amine synthesis method and process, which effectively optimizes the product structure of the ethylenediamine device, better adapts to market trends, and produces high-value-added high-amine products from low-value-added ethylenediamine; and provides a more environmentally friendly and green high-amine synthesis route.
[0007] To achieve the above objectives, the present invention provides a high-amine synthesis system, characterized in that it includes a reactor, an ethylenediamine feed line, a circulating gas feed line, a liquid phase outlet line, a gas phase outlet line, a reducing gas circulation line, a venting pipeline, and a flare pipeline; the reactor is provided with a top side inlet, a top inlet, a bottom gas phase outlet, and a bottom liquid phase outlet. The ethylenediamine feed line is connected to the top inlet of the column, and an ethylenediamine heater is installed on the ethylenediamine feed line; the circulating gas feed line is connected to the top inlet of the column via a circulating gas compressor; one end of the liquid phase outlet line is connected to the bottom liquid phase outlet of the column, and the other end is connected to the polyamine separation system; one end of the gas phase outlet line is connected to the bottom gas phase outlet of the column, and the other end is connected to the polyamine separation system; one end of the reducing gas circulation line is connected to the liquid phase outlet line, and the other end is connected to the circulating gas feed line, and an outlet reducing gas heat exchanger, a start-up fan, an inlet reducing gas heat exchanger, and a reducing gas heater are sequentially installed on the reducing gas circulation line; the vent line is connected to the circulating gas feed line; one end of the flare line is connected to the vent line, and the other end is connected to the flare system.
[0008] Furthermore, the ethylenediamine feed line is equipped with a steam pipeline and a condensate pipeline. The outlet of the steam pipeline is connected to the ethylenediamine heater, and the inlet of the condensate pipeline is connected to the ethylenediamine heater. A steam diaphragm valve is installed on the steam pipeline, and a flow meter is installed downstream of the steam diaphragm valve. A steam trap is installed on the condensate pipeline.
[0009] Furthermore, an inlet valve is provided upstream of the ethylenediamine heater, and an outlet valve is provided downstream of the heater. A flow meter is provided between the inlet valve and the ethylenediamine heater, and a temperature meter is provided downstream of the outlet valve.
[0010] Furthermore, a circulating gas inlet valve is provided on the circulating gas feed line, and a flow meter and a pressure gauge are sequentially provided downstream of the circulating gas inlet valve.
[0011] Furthermore, a liquid phase diaphragm valve is provided on the liquid phase outlet line, and a liquid phase drain valve is provided downstream of the liquid phase diaphragm valve.
[0012] Furthermore, a gas phase diaphragm valve is provided on the gas phase outlet line, and a gas phase drain valve is provided downstream of the gas phase diaphragm valve.
[0013] Furthermore, a reducing gas outlet valve is provided upstream of the outlet reducing gas heat exchanger; a reducing gas inlet valve is provided between the inlet reducing gas heat exchanger and the reducing gas heater; a reactor inlet valve is provided downstream of the reducing gas heater; a circulation branch line is provided on the reducing gas circulation line, one end of which is connected between the reducing gas heater and the reactor inlet valve, and the other end is connected to the polyamine reactor, and a polyamine inlet valve is provided on the circulation branch line.
[0014] Furthermore, a vent valve is installed on the vent pipeline; a pressure regulating valve is installed on the flare pipeline, and valves are installed upstream and downstream of the pressure regulating valve.
[0015] Furthermore, the reactor is equipped with a pressure gauge, a temperature gauge, and a crossbar, with a level gauge installed on the crossbar, which is located at the bottom of the reactor.
[0016] A process employing a high-amine synthesis system is characterized by comprising the following steps: S100, ethylenediamine feed line inputs ethylenediamine material; S200, steam pipeline input of 1.2 MPa steam; S300, ethylenediamine material and steam are heated in ethylenediamine heater, the ethylenediamine temperature is raised to 150℃-180℃ and then enters reactor; S400, the condensate produced by the ethylenediamine heater in step S300 above flows out through the condensate pipeline; S500: Compressed hydrogen and ammonia gas are fed into the reactor via the circulating gas feed line at a pressure of 10-13 MPaG. S600: Open the outlet reducing gas heat exchanger, start the blower, inlet reducing gas heat exchanger and reducing gas heater to heat up the catalyst in the reactor for reduction. The S700 reactor contains 60L of catalyst. Ethylenediamine, hydrogen, and ammonia enter the reactor and react with the catalyst to produce high-value-added ethylene amine products such as PIP, DETA, AEP, TETA, and TEPA. The mixture in the S800 reactor flows into the polyamine separation system through the gas phase outlet line and the liquid phase outlet line, respectively. S900. During the reaction process, if the pressure inside the reactor becomes too high, open the vent valve for emergency venting. S1000 During the reaction process, harmful gases generated in the reactor enter the flare system through the flare pipeline.
[0017] The beneficial effects of this invention are as follows: This application uses monoethylenediamine (EDA) as a raw material. Although EDA is also corrosive and irritating, its toxicity and volatility are far lower than those of chloroethane and HCN, greatly reducing the inherent safety risks of the process and the safety hazards to operators; the reaction is a catalytic dehydration condensation between EDA molecules, theoretically producing no inorganic waste salts. This eliminates the largest source of pollution (waste salts) at the source, significantly reducing the load on waste treatment and making it more environmentally friendly; the reaction system does not contain highly corrosive halide ions, greatly reducing the corrosiveness to equipment, allowing the use of lower-grade materials (such as ordinary stainless steel), thereby significantly reducing equipment investment and maintenance costs; through catalyst screening and process condition optimization (such as temperature, pressure, space velocity, and raw material ratio), product distribution can be more flexibly controlled, making it more in line with the product structure optimization needs of existing ethylenediamine units, achieving flexible production of "producing more of what is needed," and improving overall economic efficiency. Attached Figure Description
[0018] Figure 1 This is a process flow diagram of the present invention; In the diagram: 100, reactor; 110, cross-line. 200. Ethylenediamine feed line; 210. Ethylenediamine heater; 220. Steam line; 221. Steam diaphragm valve; 230. Condensate line; 231. Steam trap; 240. Heater inlet valve; 250. Heater outlet valve. 300. Circulating gas feed line; 310. Circulating gas compressor; 320. Circulating gas inlet valve. 400. Liquid phase outlet line; 410. Liquid phase diaphragm valve; 420. Liquid phase drain valve. 500. Gas phase outlet line; 510. Gas phase diaphragm valve; 520. Gas phase drain valve. 600. Reducing gas circulation line; 610. Outlet reducing gas heat exchanger; 620. Start-up fan; 630. Inlet reducing gas heat exchanger; 640. Reducing gas heater; 650. Reducing gas outlet valve; 660. Reducing gas inlet valve; 670. Reactor inlet valve; 680. Circulation branch line; 681. Polyamine inlet valve. 700. Vent line; 710. Vent valve. 800. Flare line; 810. Pressure regulating valve. FI: Flow rate indicator, PI: Pressure indicator, TI: Temperature indicator, LI: Liquid level indicator. Detailed Implementation
[0019] To make the above-mentioned objects, features, and advantages of the present invention more apparent and understandable, specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings. Many specific details are set forth in the following description to provide a thorough understanding of the present invention. However, the present invention can be practiced in many other ways different from those described herein, and those skilled in the art can make similar modifications without departing from the spirit of the present invention. Therefore, the present invention is not limited to the specific embodiments disclosed below.
[0020] like Figure 1 As shown, this application relates to the self-reaction of ethylenediamine as a raw material. One embodiment of the present invention provides a high-amine synthesis system, characterized by comprising: a reactor 100, an ethylenediamine feed line 200, a circulating gas feed line 300, a liquid phase outlet line 400, a gas phase outlet line 500, a reducing gas circulation line 600, a vent line 700, and a flare outlet line 800; the reactor 100 is provided with a top-side inlet, a top-side inlet, a bottom gas phase outlet, and a bottom liquid phase outlet. The ethylenediamine feed line 200 is connected to the top inlet of the column, and an ethylenediamine heater 210 is installed on the ethylenediamine feed line 200; the circulating gas feed line 300 is connected to the top inlet of the column through a circulating gas compressor 310; one end of the liquid phase outlet line 400 is connected to the bottom liquid phase outlet of the column, and the other end is connected to the polyamine separation system; one end of the gas phase outlet line 500 is connected to the bottom gas phase outlet of the column, and the other end is connected to the polyamine separation system; one end of the reducing gas circulation line 600 is connected to the liquid phase outlet line 400, and the other end is connected to the circulating gas feed line 300, and an outlet reducing gas heat exchanger 610, a start-up fan 620, an inlet reducing gas heat exchanger 630, and a reducing gas heater 640 are sequentially installed on the reducing gas circulation line 600; the vent line 700 is connected to the circulating gas feed line 300; one end of the flare line 800 is connected to the vent line 700, and the other end is connected to the flare system.
[0021] It should be noted that the ethylenediamine gas supply system uses ethylenediamine and steam as the medium to heat the ethylenediamine and provide energy for the reaction to reach the required temperature, and is used for initial heating of the material entering reactor 100. Reactor 100 is a high-temperature and high-pressure vessel used for the reaction. The circulating gas compressor 310 compresses hydrogen and ammonia to protect the catalyst and control its temperature, providing energy for the material to enter the next stage. The reducing gas heater 640 provides heat to the reducing gas during catalyst reduction. The outlet reducing gas heat exchanger 610 and the inlet reducing gas heat exchanger 630 control the reducing gas temperature, preheating and cooling it. The start-up fan 620 provides the necessary energy for the transport gas during catalyst reduction. The polyamine separation system produces a mixed liquid product, which is transported to downstream units for further separation.
[0022] In one embodiment, the ethylenediamine feed line 200 is provided with a steam line 220 and a condensate line 230. The outlet of the steam line 220 is connected to the ethylenediamine heater 210, and the inlet of the condensate line 230 is connected to the ethylenediamine heater 210. A steam diaphragm valve 221 is provided on the steam line 220, and a flow meter is provided downstream of the steam diaphragm valve 221. A steam trap 231 is provided on the condensate line 230.
[0023] In one embodiment, a heater inlet valve 240 is provided upstream of the ethylenediamine heater 210, and a heater outlet valve 250 is provided downstream. A flow meter is provided between the heater inlet valve 240 and the ethylenediamine heater 210, and a temperature meter is provided downstream of the heater outlet valve 250.
[0024] In one embodiment, a circulating gas inlet valve 320 is provided on the circulating gas feed line 300, and a flow meter and a pressure gauge are sequentially provided downstream of the circulating gas inlet valve 320.
[0025] In one embodiment, a liquid phase diaphragm valve 410 is provided on the liquid phase outlet line 400, and a liquid phase drain valve 420 is provided downstream of the liquid phase diaphragm valve 410.
[0026] In one embodiment, a gas phase diaphragm valve 510 is provided on the gas phase outlet line 500, and a gas phase drain valve 520 is provided downstream of the gas phase diaphragm valve 510.
[0027] It should be noted that the gas phase drain valve 520 and the liquid phase drain valve 420 are used for sampling and analyzing the composition of reaction products.
[0028] In one embodiment, a reducing gas outlet valve 650 is provided upstream of the outlet reducing gas heat exchanger 610; a reducing gas inlet valve 660 is provided between the inlet reducing gas heat exchanger 630 and the reducing gas heater 640; a reactor 100 inlet valve is provided downstream of the reducing gas heater 640; a circulation branch line 680 is provided on the reducing gas circulation line 600, one end of which is connected between the reducing gas heater 640 and the reactor inlet valve 670, and the other end is connected to the polyamine reactor 100, and a polyamine inlet valve is provided on the circulation branch line 680.
[0029] In one embodiment, a vent valve 710 is provided on the vent line 700; a pressure regulating valve 810 is provided on the flare line 800, and valves are provided upstream and downstream of the pressure regulating valve 810.
[0030] In one embodiment, the reactor 100 is provided with a pressure gauge, a temperature gauge and a cross-line 110, the cross-line 110 is provided with a liquid level gauge and the cross-line 110 is located at the bottom of the reactor 100.
[0031] It should be noted that: 1. There are currently no patents related to the synthesis of high-amine compounds using monoethylenediamine as a raw material; 2. This research mainly aims to optimize the product structure and subsequent products of the ethylene amine unit, synthesizing high-value-added ethylene amine products such as diethylenetriamine and triethylenetetramine from monoethylenediamine; 3. Currently, the main reaction to generate diethylenetriamine is through reactions with chloroethane and hydrogen cyanide. Although this method has high selectivity for diethylenetriamine, it causes serious problems such as waste, equipment corrosion, and other issues. The monoethylenediamine synthesis method is more environmentally friendly, and the product distribution is more in line with the requirements of the existing ethylene amine unit's product distribution.
[0032] A process employing a high-amine synthesis system is characterized by comprising the following steps: S100, ethylenediamine feed line 200 inputs ethylenediamine material; S200, steam pipeline 220 inputs 1.2 MPa steam; S300, ethylenediamine material and steam are heated in ethylenediamine heater 210, the ethylenediamine temperature is raised to 150℃-180℃, and then enters reactor 100; S400, the condensate generated by the ethylenediamine heater 210 in step S300 above flows out through the condensate pipeline 230; S500, the circulating gas feed line 300 inputs compressed hydrogen and ammonia gas into reactor 100, the pressure is 10-13 MPaG; S600, open outlet reducing gas heat exchanger 610, start-up fan 620, inlet reducing gas heat exchanger 630 and reducing gas heater 640 to heat up and reduce the catalyst in reactor 100; S700, reactor 100 contains 60L of catalyst. Ethylenediamine, hydrogen, ammonia and catalyst enter reactor 100 and undergo catalytic reaction to produce high value-added ethylene amine products such as PIP, DETA, AEP, TETA and TEPA. It should be noted that the catalyst in reactor 100 is a rhenium-based catalyst, whose main components are rhenium, nickel, and boron; The mixture in S800 and reactor 100 flows into the polyamine separation system through gas phase outlet line 500 and liquid phase outlet line 400, respectively. S900. During the reaction process, if the pressure inside reactor 100 is too high, open vent valve 710 for emergency venting. S1000 During the reaction process, harmful gases generated in reactor 100 enter the flare system through flare line 800.
[0033] It should be noted that: 1. The reaction is carried out in a fixed-bed reactor 100. Ethylenediamine enters from the top side of the reactor 100, and hydrogen circulation gas enters from the top. The hydrogen plays a role in protecting the catalyst. The gaseous material at the bottom of the reactor 100 enters the low-pressure separation tank of the existing polyethylene polyamine unit through the bottom side opening. The reaction mixture at the bottom of the reactor 100 enters the low-pressure separation tank of the existing polyethylene polyamine unit through the bottom pipeline. 2. The entire reaction mixture is fed into the existing polyethylene polyamine unit for subsequent separation. The products and unreacted raw materials are all existing materials in the current ethylene amine unit, and the subsequent separation of the high-amine project meets the requirements. 3. This invention is the first to use ethylenediamine to produce high-amine products such as diethylenetriamine, triethylenetetramine, piperazine, aminoethylpiperazine, and tetraethylenepentamine.
[0034] In the aforementioned high-amine synthesis system and process, ethylenediamine is used as the raw material for the high-amine project. The diverted ethylenediamine is heated to 160°C via an ethylenediamine heater 210 and then enters reactor 100. The reaction conditions are hydrogen-bearing, 160°C, and 11 MPaG. High-value-added ethylene amine products such as PIP, DETA, AEP, TETA, and TEPA are generated through a catalytic reaction. The reaction mixture is fed into the low-pressure separation tank of an existing polyethylene polyamine project via pressure control (gas phase) and level control (liquid phase), respectively. The reactants are separated using the existing fractionation system.
[0035] It should be noted that "hydrogen-in-place" refers to fresh hydrogen gas with a purity of 99.5%-99.9%, pressurized to 11.0 MPa, which is applied to the surface of the catalyst to form a protective layer, protecting the catalyst molecular sieve from clogging.
[0036] Parameter description: 1. Reaction temperature: 160℃-180℃; 2. Reaction pressure: 10-13 MPaG; 3. Catalyst loading capacity: 60L; 4. Product Distribution (Estimated) compound Reactor feed kg / h Reactor output kg / h Raw material conversion rate Product Distribution EDA 35.91 20.39 43.2% H2 (60% of the circulating gas) 0.51 0.51 NH3 (40% in circulating gas) 2.90 5.91 13.84% PIP (piperazine) 2.58 17.76% DETA (triamine) 6.67 45.93% AEP (aminoethylpiperazine) 0.41 2.82% TETA (tetraamine) 2.36 16.27% TEPA (pentamine) 0.45 3.11% PEHA (hexamethylenetetramine) 0.03 0.21% Other amines 0.01 0.07% total 39.32 39.32 In the description of this invention, it should be understood that the terms "center," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," and "circumferential" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.
[0037] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.
[0038] In this invention, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.
[0039] In this invention, unless otherwise explicitly specified and limited, "above" or "below" a second feature can mean that the first and second features are in direct contact, or that they are in indirect contact through an intermediate medium. Furthermore, "above," "over," and "on top" of a second feature can mean that the first feature is directly above or diagonally above the second feature, or simply that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" a second feature can mean that the first feature is directly below or diagonally below the second feature, or simply that the first feature is at a lower horizontal level than the second feature. It should be noted that when an element is referred to as "fixed to" or "set on" another element, it can be directly on the other element or there may be an intermediate element present. When an element is considered to be "connected" to another element, it can be directly connected to the other element or there may be an intermediate element present. The terms "vertical," "horizontal," "above," "below," "left," "right," and similar expressions used herein are for illustrative purposes only and do not represent the only possible embodiments.
Claims
1. A high-amine synthesis system, characterized in that: include The reactor is equipped with a top side inlet, a top inlet, a bottom gas phase outlet, and a bottom liquid phase outlet. An ethylenediamine feed line is connected to the top side inlet of the tower, and an ethylenediamine heater is installed on the ethylenediamine feed line; The circulating gas feed line is connected to the top inlet of the tower via a circulating gas compressor; The liquid phase outlet line is connected at one end to the bottom liquid phase outlet of the tower and at the other end to the polyamine separation system; The gas phase outlet line is connected at one end to the bottom gas phase outlet of the tower and at the other end to the polyamine separation system. The reducing gas circulation line is connected at one end to the liquid phase outlet line and at the other end to the circulating gas feed line. The reducing gas circulation line is sequentially equipped with an outlet reducing gas heat exchanger, a start-up fan, an inlet reducing gas heat exchanger, and a reducing gas heater. The vent line is connected to the circulating gas feed line; The flare line is connected at one end to the vent line and at the other end to the flare system.
2. The high-amine synthesis system according to claim 1, characterized in that: The ethylenediamine feed line is equipped with a steam pipeline and a condensate pipeline. The outlet of the steam pipeline is connected to the ethylenediamine heater, and the inlet of the condensate pipeline is connected to the ethylenediamine heater. A steam diaphragm valve is installed on the steam pipeline, and a flow meter is installed downstream of the steam diaphragm valve. A steam trap is installed on the condensate pipeline.
3. The high-amine synthesis system according to claim 1, characterized in that: The ethylenediamine heater is provided with an inlet valve upstream and an outlet valve downstream. A flow meter is provided between the inlet valve and the ethylenediamine heater, and a temperature meter is provided downstream of the outlet valve.
4. The high-amine synthesis system according to claim 1, characterized in that: A circulating gas inlet valve is installed on the circulating gas feed line, and a flow meter and a pressure gauge are installed downstream of the circulating gas inlet valve in sequence.
5. The high-amine synthesis system according to claim 1, characterized in that: A liquid phase diaphragm valve is installed on the liquid phase outlet line, and a liquid phase drain valve is installed downstream of the liquid phase diaphragm valve.
6. The high-amine synthesis system according to claim 1, characterized in that: A gas phase diaphragm valve is installed on the gas phase outlet line, and a gas phase drain valve is installed downstream of the gas phase diaphragm valve.
7. The high-amine synthesis system according to claim 1, characterized in that: A reducing gas outlet valve is provided upstream of the outlet reducing gas heat exchanger; a reducing gas inlet valve is provided between the inlet reducing gas heat exchanger and the reducing gas heater; a reactor inlet valve is provided downstream of the reducing gas heater; a circulation branch line is provided on the reducing gas circulation line, one end of which is connected between the reducing gas heater and the reactor inlet valve, and the other end is connected to the polyamine reactor, and a polyamine inlet valve is provided on the circulation branch line.
8. The high-amine synthesis system according to claim 1, characterized in that: A vent valve is installed on the venting pipeline; a pressure regulating valve is installed on the flare pipeline, and valves are installed upstream and downstream of the pressure regulating valve.
9. The high-amine synthesis system according to claim 1, characterized in that: The reactor is equipped with a pressure gauge, a temperature gauge, and a crossbar. A level gauge is installed on the crossbar, which is located at the bottom of the reactor.
10. A process for synthesizing a high-amine system according to any one of claims 1-9, characterized in that: Including steps S100, ethylenediamine feed line inputs ethylenediamine material; S200, steam pipeline input of 1.2 MPa steam; S300, ethylenediamine material and steam are heated in ethylenediamine heater, the ethylenediamine temperature is raised to 150℃-180℃ and then enters reactor; S400, the condensate produced by the ethylenediamine heater in step S300 above flows out through the condensate pipeline; S500: Compressed hydrogen and ammonia gas are fed into the reactor via the circulating gas feed line at a pressure of 10-13 MPaG. S600: Open the outlet reducing gas heat exchanger, start the blower, inlet reducing gas heat exchanger and reducing gas heater to heat up the catalyst in the reactor for reduction. The S700 reactor contains 60L of catalyst. Ethylenediamine, hydrogen, and ammonia enter the reactor and react with the catalyst to produce high-value-added ethylene amine products such as PIP, DETA, AEP, TETA, and TEPA. The mixture in the S800 reactor flows into the polyamine separation system through the gas phase outlet line and the liquid phase outlet line, respectively. S900. During the reaction process, if the pressure inside the reactor becomes too high, open the vent valve for emergency venting. S1000 During the reaction process, harmful gases generated in the reactor enter the flare system through the flare pipeline.