Tert-butylamine synthesis reaction heat utilization system and tert-butylamine synthesis reaction heat utilization method

Abstract

The invention provides a tert-butylamine synthesis reaction heat utilization system. The tert-butylamine synthesis reaction heat utilization system comprises a heat exchange device and a heat utilization device, the heat exchange device comprises a shell pass heat exchange pipeline, the shell pass heat exchange pipeline is arranged in a tert-butylamine synthesis reactor, the tert-butylamine synthesis reactor is a tubular reactor, and the shell pass heat exchange pipeline is communicated with the shell pass heat exchange pipeline. The shell pass heat exchange pipeline is a shell pass of the tubular reactor, and a heat displacer is arranged in the shell pass heat exchange pipeline and is used for carrying out heat absorption on reaction heat of the tert-butylamine synthesis reactor; and the heat utilization device is communicated with the heat exchange device and is used for utilizing the heat absorbed by the heat displacer. The tert-butylamine synthesis reaction heat utilization system can reduce energy consumption.

Description

Technical Field

[0001] The invention belongs to the technical field of chemical engineering, and in particular relates to a tert-butylamine synthesis reaction heat utilization system and a tert-butylamine synthesis reaction heat utilization method. Background Art

[0002] Tert-butylamine is an organic synthesis intermediate, also known as "2-methyl-2-aminopropane". The chemical formula is (CH3)3CNH2. The molecular weight is 73.14. Tert-butylamine is a colorless, flammable liquid with an ammonia odor. It is irritating and corrosive to the human body. It is miscible with ethanol, water, and ether, and can form an explosive mixture with air. It is mainly used as a rubber additive, pesticide, fungicide, dye, medicine, etc.

[0003] Tert-butylamine has experienced a period of coexistence of multiple preparation methods. The tert-butyl alcohol-urea method, tert-butyl alcohol-hydrocyanic acid method, methyl tert-butyl ether-hydrocyanic acid method, and Riter reaction method have all been used as the main methods for producing acrylic acid and esters. However, these methods have been basically eliminated due to the high toxicity of raw materials, high risk, high energy consumption, low yield, and high cost. Currently, the most economical and environmentally friendly method for producing tert-butylamine is the direct amination of isobutylene.

[0004] In the current patented method for preparing tert-butylamine by direct catalytic amination of isobutylene, steam is generally used to heat and vaporize the raw liquid ammonia and isobutylene, and the heat release of the reactor is transferred by heat transfer oil. After the mixed raw gas and the reactor outlet product are heat-exchanged, they are heated to the reaction temperature by circulating heat transfer oil and passed into the reactor. The temperature of the reactor outlet product is still high after preheating the mixed raw gas, and is further cooled by a cooler, and then enters the downstream distillation system after gas-liquid separation. Since steam is needed to heat and vaporize the raw materials, and a cooler is needed to cool the reactor, the utilization rate of the heat generated by the reactor reaction is low, and the energy consumption generated by the steam and the cooler is high. Summary of the invention

[0005] In view of the above technical problems, the present invention provides a tert-butylamine synthesis reaction heat utilization system and a tert-butylamine synthesis reaction heat utilization method.

[0006] The objective of the present invention is achieved through the following technical solutions:

[0007] A tert-butylamine synthesis reaction heat utilization system, characterized by comprising:

[0008] A heat exchange device, wherein the heat exchange device comprises a shell-side heat exchange pipeline, wherein the shell-side heat exchange pipeline is arranged in a tert-butylamine synthesis reactor, wherein the tert-butylamine synthesis reactor is a shell-and-tube reactor, wherein the shell-side heat exchange pipeline is the shell side of the shell-and-tube reactor, and wherein a heat exchange agent is provided in the shell-and-tube heat exchange pipeline for absorbing the reaction heat of the tert-butylamine synthesis reactor;

[0009] A heat utilization device is connected to the heat exchange device and is used to utilize the heat absorbed by the heat replacement agent.

[0010] In one embodiment, the tert-butylamine synthesis reaction heat utilization system also includes the tert-butylamine synthesis reactor and a raw material vaporization mechanism, the heat utilization device includes a raw material vaporization heat exchange pipe, the raw material vaporization heat exchange pipe is connected to the heat exchange device, the raw material vaporization heat exchange pipe is connected to the raw material vaporization mechanism, and is used to heat the raw material vaporization mechanism, wherein the raw material vaporization mechanism is provided with a vaporized raw material outlet, and the vaporized raw material outlet is connected to the shell-and-tube reactor.

[0011] In one of the embodiments, the heat exchange device also includes a reaction gas pre-cooler, the reaction gas pre-cooler is formed with a heat exchange channel, and the heat exchange channel is connected to the vaporized raw material outlet; the shell-and-tube reactor is provided with a reaction gas outlet, and the reaction gas outlet is provided with a conveying pipeline, and the conveying pipeline is used for heat exchange with the reaction gas pre-cooler, and the conveying pipeline is used to communicate with the separation and distillation system.

[0012] In one embodiment, the heat exchange channel is a countercurrent heat exchange channel.

[0013] In one of the embodiments, the reaction gas pre-cooler is provided with a feed pipe, the feed pipe is connected to the shell-and-tube reactor, the feed pipe is provided with a temperature control mechanism, and the temperature control mechanism is electrically connected to the feed pipe.

[0014] In one embodiment, the tert-butylamine synthesis reaction heat utilization system further comprises a raw material preheating mechanism, wherein the raw material preheating mechanism is provided with a raw material inlet and a preheated raw material outlet; the raw material vaporization mechanism is further provided with a preheated raw material inlet, wherein the preheated raw material inlet is connected to the preheated raw material outlet;

[0015] The tubular reactor is provided with a vaporized raw material inlet, and the vaporized raw material inlet is connected to the heat exchange channel;

[0016] The conveying pipeline is also used for heat exchange with the raw material preheating mechanism.

[0017] In one embodiment, the raw material preheating mechanism includes an isobutylene preheater and a liquid ammonia preheater, the raw material inlet includes an isobutylene inlet and a liquid ammonia inlet, the preheated raw material outlet includes a preheated isobutylene outlet and a preheated liquid ammonia outlet, the isobutylene inlet and the preheated isobutylene outlet are both opened in the isobutylene preheater, the liquid ammonia inlet and the preheated liquid ammonia outlet are both opened in the liquid ammonia preheater; the conveying pipeline performs heat exchange with the isobutylene preheater and the liquid ammonia preheater in turn.

[0018] In one embodiment, the raw material vaporization mechanism includes an isobutylene vaporizer and a liquid ammonia vaporizer that are connected to each other, the preheated raw material inlet includes a preheated isobutylene inlet and a preheated liquid ammonia inlet, the preheated isobutylene inlet is connected to the preheated isobutylene outlet, and the preheated liquid ammonia inlet is connected to the preheated liquid ammonia outlet; the vaporized raw material outlet includes an ammonia outlet and a vaporized isobutylene outlet, the ammonia outlet is opened in the liquid ammonia vaporizer, and the vaporized isobutylene outlet is opened in the isobutylene vaporizer; the ammonia outlet and the vaporized isobutylene outlet are both connected to the vaporized raw material inlet.

[0019] In one of the embodiments, the shell-side heat exchange pipeline is provided with a circulation pump, and the circulation pump is used to circulate the heat exchange agent in the shell-side heat exchange pipeline.

[0020] A method for utilizing heat from a tert-butylamine synthesis reaction, which utilizes the heat from the tert-butylamine synthesis reaction using a system for utilizing heat from a tert-butylamine synthesis reaction as described in any of the above embodiments.

[0021] Compared with the prior art, the tert-butylamine synthesis reaction heat utilization system technology provided by the present invention has the following advantages or beneficial effects:

[0022] In the tert-butylamine synthesis reaction heat utilization system of the present invention, the heat displacer in the shell-side heat exchange pipeline absorbs the reaction heat of the tert-butylamine synthesis reactor, and the heat utilization device utilizes the heat absorbed by the heat displacer, that is, through heat coupling, the high-efficiency utilization of heat is improved and the energy consumption is reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Attached Figure 1 1 is a schematic structural diagram of a heat utilization system for tert-butylamine synthesis reaction according to Embodiment 1 of the present invention;

[0024] Attached Figure 2 It is a schematic structural diagram of a thermal steam production system for tert-butylamine synthesis reaction according to the second embodiment of the present invention. DETAILED DESCRIPTION

[0025] In order to make the purpose, technical solutions and advantages of the present invention clearer, the present invention is further described in detail below in conjunction with embodiments and drawings, so that the implementation process of how the present invention applies technical means to solve technical problems and achieve technical effects can be fully understood and implemented accordingly.

[0026] See also Figure 1, a tert-butylamine synthesis reaction heat utilization system of one embodiment includes a heat exchange device and a heat utilization device. The heat exchange device includes a shell-side heat exchange pipeline, the shell-side heat exchange pipeline is arranged in the tert-butylamine synthesis reactor, the tert-butylamine synthesis reactor is a shell-and-tube reactor 1, the shell-side heat exchange pipeline is the shell side of the shell-and-tube reactor 1, and the shell-side heat exchange pipeline has a heat displacement agent for absorbing the reaction heat of the tert-butylamine synthesis reactor; the heat utilization device is connected to the heat exchange device, and the heat utilization device is used to utilize the heat absorbed by the heat displacement agent. Specifically, the heat utilization device can be directly used for heating a heat source, can also be used for heat-to-work conversion, and can also be used as a heat pump.

[0027] In the above-mentioned tert-butylamine synthesis reaction heat utilization system, the heat displacer in the shell-side heat exchange pipe absorbs the reaction heat of the tert-butylamine synthesis reactor, and the heat utilization device utilizes the heat absorbed by the heat displacer, that is, through heat coupling, the efficient utilization of heat is improved and the energy consumption is reduced.

[0028] See also Figure 1 In one embodiment, the tert-butylamine synthesis reaction heat utilization system includes the tert-butylamine synthesis reactor and the raw material vaporization mechanism, the heat utilization device includes a raw material vaporization heat exchange pipe, the raw material vaporization heat exchange pipe is connected to the heat exchange device, the raw material vaporization heat exchange pipe is connected to the raw material vaporization mechanism, and is used to heat the raw material vaporization mechanism, wherein the raw material vaporization mechanism is provided with a vaporization raw material outlet, and the vaporization raw material outlet is connected to the shell-and-tube reactor 1. It can be understood that the tert-butylamine synthesis reaction heat utilization system of the present application adopts direct amination of isobutylene to prepare tert-butylamine. The tert-butylamine synthesis reaction releases a large amount of heat. The heat released by the reaction is transferred to the raw material vaporization mechanism through the heat exchanger of the heat exchange device, which not only heats up and vaporizes the raw material isobutylene and liquid ammonia, but also cools the tert-butylamine. Through energy coupling, the efficient utilization of heat is improved, which not only avoids the problem of large steam consumption caused by the traditional tert-butylamine synthesis reaction heat utilization system needing to use steam heating to vaporize the raw material liquid ammonia and isobutylene, but also reduces the problem of large energy and cooling water consumption caused by the need for additional cooling equipment to be used for treatment of tert-butylamine before entering the separation and distillation system, thereby achieving energy saving. In other words, the heat utilization device is used to heat the raw material of the raw material vaporization mechanism.

[0029] See also Figure 1In one embodiment, the heat exchange device further comprises a reaction gas pre-cooler 3, the reaction gas pre-cooler 3 is formed with a heat exchange channel, and the heat exchange channel is connected to the vaporized raw material outlet; the shell-and-tube reactor 1 is provided with a reaction gas outlet, and the reaction gas outlet is provided with a delivery pipeline, the delivery pipeline is used for heat exchange with the reaction gas pre-cooler 3, and the delivery pipeline is used for communication with the separation and distillation system. It can be understood that the vaporized raw materials isobutylene and ammonia enter the reaction gas pre-cooler 3 from the vaporized raw material outlet, and the synthesis reaction gas carrying a large amount of heat synthesized by the shell-and-tube reactor 1 enters the delivery pipeline from the outlet of the shell-and-tube reactor 1, and the delivery pipeline exchanges heat with the reaction gas pre-cooler 3, that is, part of the heat of the reaction gas is transferred to the vaporized raw material of the reaction gas pre-cooler 3, which not only makes the raw materials isobutylene and liquid ammonia continue to heat up to a temperature close to the synthesis reaction temperature, but also makes the reaction gas cool down, which is beneficial to the subsequent reaction gas liquefaction, and improves the efficient use of heat through energy coupling. In this embodiment, the delivery pipeline is arranged in the shell side of the reaction gas pre-cooler 3. It can be understood that the conveying pipeline contains tert-butylamine at a relatively high temperature, and the tube side of the reaction gas primary cooler 3 contains vaporized raw materials at a relatively low temperature, so the conveying pipeline is arranged in the shell side of the reaction gas primary cooler 3 .

[0030] See also Figure 1In one embodiment, the heat exchange channel is a countercurrent heat exchange channel. It can be understood that the countercurrent heat exchange channel means that the flow direction of the heat exchange channel is different from the flow direction of the reaction gas in the shell side of the reaction gas pre-cooler where the delivery pipeline is arranged, which prolongs the heat exchange distance of the reaction gas pre-cooler 3, prolongs the heat exchange time between the vaporized raw material and the reaction gas, and ensures the utilization rate of heat. In this embodiment, the part where the delivery pipeline is arranged in the shell side of the reaction gas pre-cooler includes a first heat exchange section and a second heat exchange section, and the reaction gas flows from the first heat exchange section to the second heat exchange section. The inlet of the heat exchange channel is opened at the end of the second heat exchange section away from the first heat exchange section, and the outlet of the heat exchange channel is opened at the end of the first heat exchange section away from the second heat exchange section. Part of the heat of the reaction gas is transferred to the vaporized raw material, so that the temperature of the reaction gas gradually decreases from the first heat exchange section to the second heat exchange section, that is, in the part where the conveying pipeline is arranged in the shell side of the reaction gas pre-cooler, the temperature of the end of the first heat exchange section away from the second heat exchange section is the highest, and the temperature of the end of the second heat exchange section away from the first heat exchange section is the lowest. Similarly, the temperature of the vaporized raw material in the heat exchange channel is relatively low before heat exchange with the reaction gas, that is, in the heat exchange channel, the temperature at the inlet of the heat exchange channel is the lowest, and the temperature at the outlet of the heat exchange channel is the highest, so that the inlet of the heat exchange channel is opened at the end close to the second heat exchange section away from the first heat exchange section, so that the reaction gas is cooled to the maximum extent in the shell side of the reaction gas pre-cooler, that is, the cooling effect of the reaction gas is very good. Similarly, the outlet of the heat exchange channel is opened at the end close to the first heat exchange section away from the second heat exchange section, so that the vaporized raw material is heated to the maximum extent in the tube side of the reaction gas pre-cooler, that is, the heating effect of the vaporized raw material is very good, that is, better energy coupling is achieved, and energy utilization is improved.

[0031] See also Figure 1 In one embodiment, the reaction gas pre-cooler 3 is provided with a feed pipe, the feed pipe is connected to the shell-and-tube reactor 1, and the feed pipe is provided with a temperature control mechanism, and the temperature control mechanism is electrically connected to the feed pipe. It can be understood that the reaction gas is in the shell side of the reaction gas pre-cooler 3, and the vaporized raw material is in the tube side of the reaction gas pre-cooler 3. After part of the heat of the reaction gas is transferred to the vaporized raw material, the vaporized raw material is heated up, and the temperature is close to the reaction temperature. The temperature control mechanism detects and heats the vaporized raw material to achieve the purpose of precise temperature control, so that the vaporized raw material reaches the reaction temperature, improves the reaction efficiency and the conversion rate of tert-butylamine. In this embodiment, the temperature control mechanism is a temperature-controlled electric heater 2.

[0032] See also Figure 1, heat transfer oil can only transfer the reaction heat released during the synthesis of tert-butylamine. For the high-temperature fluid at the reactor outlet, a cooling device is required for further cooling. In order to improve the utilization rate of reaction heat, in one embodiment, the tert-butylamine synthesis reaction heat utilization system also includes a raw material preheating mechanism and a raw material vaporization mechanism, the raw material preheating mechanism is provided with a raw material inlet and a preheating raw material outlet; the raw material vaporization mechanism is also provided with a preheating raw material inlet, which is connected to the preheating raw material outlet; the shell-and-tube reactor 1 is provided with a vaporization raw material inlet, which is connected to the heat exchange channel; the delivery pipeline is also used for heat exchange with the raw material preheating mechanism. It can be understood that the raw materials enter the raw material preheating mechanism from the raw material inlet and perform heat exchange with the conveying pipeline, so that the raw materials are preheated and the reaction gas is further cooled and liquefied. No gas-liquid separation equipment is required, which reduces equipment investment and floor space. Then the preheated raw materials enter the raw material vaporization mechanism, and the heat exchanger in the shell-side heat exchange pipeline transfers the reaction heat of tert-butylamine synthesis to the raw material vaporization mechanism, vaporizes the raw materials, and cools the reaction gas, effectively reducing the use of steam and cooling water, that is, reducing energy consumption.

[0033] See also Figure 1 In one embodiment, the raw material preheating mechanism includes an isobutylene preheater 4 and a liquid ammonia preheater 5, the raw material inlet includes an isobutylene inlet and a liquid ammonia inlet, the preheated raw material outlet includes a preheated isobutylene outlet and a preheated liquid ammonia outlet, the isobutylene inlet and the preheated isobutylene outlet are both opened in the isobutylene preheater 4, the liquid ammonia inlet and the preheated liquid ammonia outlet are both opened in the liquid ammonia preheater 5; the delivery pipeline is heat-exchanged with the isobutylene preheater 4 and the liquid ammonia preheater 5 in sequence. It can be understood that compared with liquid ammonia, isobutylene is more difficult to vaporize, so the reaction gas in the delivery pipeline first heats the isobutylene when the temperature is high, and the reaction gas is easily liquefied in the isobutylene preheater 4, so as to be separated and distilled later, and then the liquid ammonia is heated when the reaction gas temperature is low, so that both isobutylene and liquid ammonia can be better heated.

[0034] See also Figure 1 In one embodiment, the raw material vaporization mechanism includes an isobutylene vaporizer 8 and a liquid ammonia vaporizer 7 that are connected to each other, the preheated raw material inlet includes a preheated isobutylene inlet and a preheated liquid ammonia inlet, the preheated isobutylene inlet is connected to the preheated isobutylene outlet, and the preheated liquid ammonia inlet is connected to the preheated liquid ammonia outlet; the vaporized raw material outlet includes an ammonia outlet and a vaporized isobutylene outlet, the ammonia outlet is opened in the liquid ammonia vaporizer 7, and the vaporized isobutylene outlet is opened in the isobutylene vaporizer 8; the ammonia outlet and the vaporized isobutylene outlet are both connected to the vaporized raw material inlet.

[0035] See also Figure 1In one embodiment, the shell side heat exchange pipeline is a heat transfer oil furnace 6, and the heat exchange agent is heat transfer oil. It can be understood that the heat transfer oil has high heat transfer efficiency, fast heat dissipation, and good thermal stability, and can be recycled. After the heat transfer oil transfers the heat of the reactor to the raw material vaporization mechanism, the temperature of the heat transfer oil is low, and the heat transfer oil flows back to the reactor shell side and performs the next round of heat transfer.

[0036] See also Figure 1 In one of the embodiments, the shell-side heat exchange pipeline is provided with a circulation pump, and the circulation pump is used to circulate the heat exchange agent in the shell-side heat exchange pipeline, and the circulation pump improves the fluidity and heat transfer efficiency of the heat transfer oil.

[0037] See also Figure 1 In one embodiment, the temperature of the shell-and-tube reactor 1 is 150° C. to 300° C. It can be understood that 150° C. to 300° C. is a suitable temperature for the synthesis reaction of tert-butylamine, which is conducive to the synthesis of tert-butylamine.

[0038] See also Figure 1 In one embodiment, the shell-and-tube reactor 1 is formed with a synthesis reaction chamber, and the pressure of the synthesis reaction chamber is 1.0 MPaG to 15 MPaG. It can be understood that 1.0 MPaG to 15 MPaG is a suitable pressure for the synthesis reaction of tert-butylamine, which is conducive to the synthesis of tert-butylamine.

[0039] See also Figure 1In the raw material preheating mechanism, the reaction gas passes through the isobutylene preheater 4 and the liquid ammonia preheater 5 in sequence, preheating the raw material liquid phase isobutylene with a temperature of 25°C to 80°C and a pressure of 5MPaG to 15MPaG to 140°C to 180°C, and preheating the liquid ammonia with a temperature of 25°C to 80°C and a pressure of 5MPaG to 15MPaG to 100°C to 140°C. In the raw material vaporization mechanism, the preheated isobutylene and liquid ammonia are respectively in the isobutylene vaporizer 8 and the liquid ammonia vaporizer 7, and the heat transferred by the heat transfer oil furnace 6 completely vaporizes the isobutylene and liquid ammonia. The raw material temperature control section includes a reaction gas primary cooler 3 and a temperature control electric heater 2. The temperature of the mixed raw material gas after vaporization is 150°C to 200°C, which is close to the reaction feed temperature after heat exchange in the reactor primary cooler. By setting the temperature control electric heater 2, the temperature of the mixed raw material gas is controlled at 240°C to 260°C before entering the shell-and-tube reactor 1. The heat released in the shell-and-tube reactor 1 is transferred by heat transfer oil. The temperature of the heat transfer oil after leaving the shell-and-tube reactor 1 is 235°C to 255°C. The outlet temperature of the heat transfer oil furnace 6 is set to 250°C to 270°C. After heat exchange with the liquid ammonia vaporizer 7 and the isobutylene vaporizer 8, the temperature is reduced to 220°C to 240°C, and returns to the shell-and-tube reactor 1 for reaction heat transfer, completing the heat transfer oil system circulation process. The temperature of the reaction gas at the outlet of the shell-and-tube reactor 1 is 240°C to 260°C. After the mixed raw material gas is heated in the reactor pre-cooler, the temperature is reduced to 160°C to 200°C. After the raw material is preheated in the isobutylene preheater 4 and the liquid ammonia preheater 5 in the raw material preheating mechanism, the temperature is reduced to 90°C to 110°C and liquefied, and then passed into the downstream separation and distillation system.

[0040] See also Figure 1 Preferably, the heat exchange channel in the reaction gas pre-cooler 3 is a countercurrent heat exchange channel, the reaction gas temperature at the outlet of the shell-and-tube reactor 1 is 250°C, and the temperature of the reaction gas drops to 183°C after heating the mixed raw gas in the reaction gas pre-cooler 3. The temperature of the mixed raw gas before heating in the reaction gas pre-cooler 3 is 172°C, and the temperature after heating is 240°C.

[0041] In one embodiment, a tert-butylamine synthesis reaction heat utilization system comprises a heat exchange device, a heat utilization device, a tert-butylamine synthesis reactor, a raw material vaporization mechanism and a raw material preheating mechanism; the heat exchange device comprises a shell-side heat exchange pipeline and a reaction gas precooler, the shell-side heat exchange pipeline is arranged in the tert-butylamine synthesis reactor, the tert-butylamine synthesis reactor is a shell-and-tube reactor, the shell-side heat exchange pipeline is the shell side of the shell-and-tube reactor, the shell-side heat exchange pipeline has a heat displacement agent for absorbing the reaction heat of the tert-butylamine synthesis reactor; the shell-side heat exchange pipeline is provided with a circulation pump, and the circulation pump is used to circulate the heat displacement agent in the shell-side heat exchange pipeline; the reaction gas precooler is formed with a heat exchange agent. a heat channel, the heat exchange channel is connected to the vaporized raw material outlet; the shell-and-tube reactor is provided with a reaction gas outlet, the reaction gas outlet is provided with a delivery pipeline, the delivery pipeline is used for heat exchange with the reaction gas pre-cooler, and the delivery pipeline is used for communicating with the separation and distillation system; the heat exchange channel is a countercurrent heat exchange channel; the reaction gas pre-cooler is provided with a feed pipe, the feed pipe is connected to the shell-and-tube reactor, the feed pipe is provided with a temperature control mechanism, and the temperature control mechanism is electrically connected to the feed pipe; the heat utilization device is connected to the heat exchange device, the heat utilization device is used to utilize the heat absorbed by the heat displacement agent; the heat utilization device includes a raw material vaporization heat exchange pipe, the raw material vaporization heat exchange The heat pipe is connected to the heat exchange device, and the raw material vaporization heat exchange pipe is connected to the raw material vaporization mechanism for heating the raw material vaporization mechanism, wherein the raw material vaporization mechanism is provided with a vaporization raw material outlet, and the vaporization raw material outlet is connected to the shell-and-tube reactor; the shell-and-tube reactor is provided with a vaporization raw material inlet, and the vaporization raw material inlet is connected to the heat exchange channel; the raw material preheating mechanism includes an isobutylene preheater and a liquid ammonia preheater, the raw material inlet includes an isobutylene inlet and a liquid ammonia inlet, the preheated raw material outlet includes a preheated isobutylene outlet and a preheated liquid ammonia outlet, the isobutylene inlet and the preheated isobutylene outlet are both provided in the isobutylene preheater, and the liquid ammonia inlet and the preheated The preheated liquid ammonia outlets are all opened in the liquid ammonia preheater; the conveying pipeline performs heat exchange with the isobutylene preheater and the liquid ammonia preheater in sequence; the raw material vaporization mechanism includes an isobutylene vaporizer and a liquid ammonia vaporizer that are connected, the preheated raw material inlet includes a preheated isobutylene inlet and a preheated liquid ammonia inlet, the preheated isobutylene inlet is connected to the preheated isobutylene outlet, and the preheated liquid ammonia inlet is connected to the preheated liquid ammonia outlet; the vaporized raw material outlet includes an ammonia outlet and a vaporized isobutylene outlet, the ammonia outlet is opened in the liquid ammonia vaporizer, and the vaporized isobutylene outlet is opened in the isobutylene vaporizer; the ammonia outlet and the vaporized isobutylene outlet are both connected to the vaporized raw material inlet.

[0042] The present application also provides a method for utilizing heat from a tert-butylamine synthesis reaction, which utilizes the heat from the tert-butylamine synthesis reaction using a system for utilizing heat from a tert-butylamine synthesis reaction as described in any of the above embodiments.

[0043] In the above-mentioned method for utilizing the reaction heat of tert-butylamine synthesis, after the raw materials generate reaction heat in synthesizing tert-butylamine, the reaction heat carried by the reaction gas is used to preheat and vaporize the raw materials, so that the raw materials reach the reaction temperature while reducing additional energy consumption, and the reaction gas is cooled and liquefied, thereby reducing the use of cooling equipment and gas-liquid separation equipment, that is, reducing energy consumption and equipment investment.

[0044] See also Figure 1 In one embodiment, isobutylene and liquid ammonia are used as raw materials, and the raw materials are preheated, vaporized, and heated again in the heat exchange channel of the reaction gas primary cooler 3 in sequence, and then the temperature-controlled electric heater 2 detects and heats the vaporized raw materials to achieve the purpose of precise temperature control, so that the vaporized raw materials reach the reaction temperature, and then enter the reactor to generate tert-butylamine reaction gas and release a large amount of heat. At the same time, the heat transfer oil transfers the heat released by the reaction to the raw material vaporization mechanism to heat and vaporize the raw materials, and then the heat transfer oil with reduced temperature returns to the shell side of the shell-and-tube reactor 1 through the circulation pump, and the reaction gas in the shell-and-tube reactor 1 first exchanges heat with the vaporized raw materials in the reaction gas primary cooler 3 through the conveying pipeline, so that the vaporized raw materials are further heated, and then the reaction gas exchanges heat with the raw material preheating mechanism through the conveying pipeline, so that the reaction gas is cooled and liquefied and then enters the separation and distillation system.

[0045] Furthermore, after the tert-butylamine synthesis reaction occurs in the shell-and-tube reactor 1 to generate reaction heat, the preheating and vaporization of the raw materials are both provided by the reaction heat, which effectively reduces the heat consumption.

[0046] See also Figure 2 The present application also provides a tert-butylamine synthesis reaction heat steam production system. The above-mentioned steam production system includes a raw material vaporization mechanism, a mixer 9, a compressor system 10, a reaction gas pre-cooler 3, a shell-and-tube reactor 1, a heat transfer circulation mechanism and a steam drum 11. The raw material vaporization mechanism is connected to the mixer 9, and the mixer 9 and the shell-and-tube reactor 1 are both connected to the reaction gas pre-cooler 3. The compressor system 10 is used to pressurize the reaction gas pre-cooler 3. The heat transfer circulation mechanism includes a heat transfer oil furnace 6 and a circulation pump. The circulation pump is used to circulate the heat transfer oil in the heat transfer oil furnace 6. The heat transfer oil furnace 6 is used to transfer the heat of the shell-and-tube reactor 1 to the steam drum 11, and the steam drum 11 is used to heat and vaporize the raw material vaporization mechanism. The above-mentioned steam production system also includes a temperature control electric heater, which is used to control the temperature of the vaporized raw material at the air inlet of the shell-and-tube reactor 1.

[0047] In the above-mentioned steam production device, the low-pressure raw material liquid ammonia and the low-pressure raw material isobutylene are respectively heat exchanged with the reaction gas in the liquid ammonia vaporizer 7 and the isobutylene vaporizer 8 and completely vaporized. After the reaction gas is cooled, it goes to the downstream separation and distillation system. The vaporized raw materials are mixed in the mixer 9 and pressurized to the reaction target pressure by the compressor system 10. After pressurization, the raw gas and the outlet reaction gas are heat exchanged in the reaction gas primary cooler 3. In order to ensure the temperature of the reactor inlet raw gas, a temperature-controlled electric heater is used to control the temperature of the raw gas to meet the reaction requirements. The tert-butylamine synthesis reactor uses heat transfer oil to transfer heat, which reduces the energy and cooling water consumed by the additional cooling and liquefaction of the tert-butylamine reaction gas. The heat transfer oil is circulated after passing through the heat transfer oil circulation pump, and the boiler water is used to absorb the heat of the heat transfer oil in the heat transfer oil cooler and generate steam, which can be used to supply energy for the vaporization of the raw materials.

[0048] The tubular reactor 1 uses ammonia and gaseous isobutylene as raw materials, and obtains the product tert-butylamine through high-pressure reaction. The outlet reaction gas contains tert-butylamine and unreacted ammonia and isobutylene.

[0049] The compressor system 10 is a system that uses multi-stage compression to pressurize low-pressure raw gas to the reaction target pressure.

[0050] The heat transfer oil cooler utilizes boiler water to cool the heat transfer oil, removes the reaction heat, and produces steam as a byproduct.

[0051] The operating conditions of the shell-and-tube reactor 1 include but are not limited to 150° C. to 300° C. and 5.0 MPaG to 15 MPaG.

[0052] The raw material inlet pressure of the compressor system 10 includes but is not limited to 0.1 MPaG to 5 MPaG, and the outlet pressure includes but is not limited to 1 MPaG to 15 MPaG.

[0053] It should also be noted that the above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention. It should be noted that similar numbers and letters represent similar items in the following drawings, so once an item is defined in one drawing, it does not need to be further defined and explained in the subsequent drawings.

Claims

1. A tert-butylamine synthesis reaction heat utilization system, characterized in that: include: A heat exchange device, wherein the heat exchange device comprises a shell-side heat exchange pipeline, wherein the shell-side heat exchange pipeline is arranged in a tert-butylamine synthesis reactor, wherein the tert-butylamine synthesis reactor is a shell-and-tube reactor, wherein the shell-side heat exchange pipeline is the shell side of the shell-and-tube reactor, and wherein a heat exchange agent is provided in the shell-and-tube heat exchange pipeline for absorbing the reaction heat of the tert-butylamine synthesis reactor; A heat utilization device is connected to the heat exchange device and is used to utilize the heat absorbed by the heat replacement agent.

2. The tert-butylamine synthesis reaction heat utilization system according to claim 1, characterized in that: The tert-butylamine synthesis reaction heat utilization system also includes the tert-butylamine synthesis reactor and a raw material vaporization mechanism. The heat utilization device includes a raw material vaporization heat exchange pipe, which is connected to the heat exchange device. The raw material vaporization heat exchange pipe is connected to the raw material vaporization mechanism for heating the raw material vaporization mechanism, wherein the raw material vaporization mechanism is provided with a vaporization raw material outlet, and the vaporization raw material outlet is connected to the shell-and-tube reactor.

3. The tert-butylamine synthesis reaction heat utilization system according to claim 2, characterized in that: The heat exchange device further comprises a reaction gas primary cooler, wherein the reaction gas primary cooler is formed with a heat exchange channel, and the heat exchange channel is connected to the vaporized raw material outlet; The shell-and-tube reactor is provided with a reaction gas outlet, and the reaction gas outlet is provided with a delivery pipeline, and the delivery pipeline is used for heat exchange with the reaction gas pre-cooler, and the delivery pipeline is used for communication with the separation and distillation system.

4. The tert-butylamine synthesis reaction heat utilization system according to claim 3, characterized in that: The heat exchange channel is a countercurrent heat exchange channel.

5. The tert-butylamine synthesis reaction heat utilization system according to claim 3, characterized in that: The reaction gas primary cooler is provided with a feed pipe, the feed pipe is connected to the tube-in-tube reactor, the feed pipe is provided with a temperature control mechanism, and the temperature control mechanism is electrically connected to the feed pipe.

6. The tert-butylamine synthesis reaction heat utilization system according to claim 3, characterized in that: The tert-butylamine synthesis reaction heat utilization system further comprises a raw material preheating mechanism, which is provided with a raw material inlet and a preheated raw material outlet; the raw material vaporization mechanism is also provided with a preheated raw material inlet, which is connected to the preheated raw material outlet; The tubular reactor is provided with a vaporized raw material inlet, and the vaporized raw material inlet is connected to the heat exchange channel; The conveying pipeline is also used for heat exchange with the raw material preheating mechanism.

7. The tert-butylamine synthesis reaction heat utilization system according to claim 6, characterized in that: The raw material preheating mechanism includes an isobutylene preheater and a liquid ammonia preheater, the raw material inlet includes an isobutylene inlet and a liquid ammonia inlet, the preheated raw material outlet includes a preheated isobutylene outlet and a preheated liquid ammonia outlet, the isobutylene inlet and the preheated isobutylene outlet are both opened in the isobutylene preheater, the liquid ammonia inlet and the preheated liquid ammonia outlet are both opened in the liquid ammonia preheater; the conveying pipeline performs heat exchange with the isobutylene preheater and the liquid ammonia preheater in turn.

8. The tert-butylamine synthesis reaction heat utilization system according to claim 7, characterized in that: The raw material vaporization mechanism includes an isobutylene vaporizer and a liquid ammonia vaporizer which are connected to each other, the preheated raw material inlet includes a preheated isobutylene inlet and a preheated liquid ammonia inlet, the preheated isobutylene inlet is connected to the preheated isobutylene outlet, and the preheated liquid ammonia inlet is connected to the preheated liquid ammonia outlet; The vaporized raw material outlet includes an ammonia outlet and a vaporized isobutylene outlet, the ammonia outlet is opened in the liquid ammonia vaporizer, and the vaporized isobutylene outlet is opened in the isobutylene vaporizer; The ammonia outlet and the vaporized isobutylene outlet are both connected to the vaporized raw material inlet.

9. The tert-butylamine synthesis reaction heat utilization system according to claim 1, characterized in that: The shell-side heat exchange pipeline is provided with a circulation pump, and the circulation pump is used to circulate the heat replacement agent in the shell-side heat exchange pipeline.

10. A method for utilizing heat from a tert-butylamine synthesis reaction, comprising utilizing the heat from a tert-butylamine synthesis reaction system as claimed in any one of claims 1 to 9.

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