A cyclohexanone oxime rearrangement reaction heat for tert-butyl alcohol recovery device

Abstract

The invention discloses a device for utilizing cyclohexanone oxime rearrangement reaction heat for tert-butyl alcohol recovery, belongs to the technical field of caprolactam, and addresses the problem of poor performance and effect of comprehensive utilization of cyclohexanone oxime Beckmann rearrangement reaction heat and tert-butyl alcohol recovery device. The device comprises a first tert-butyl alcohol recovery tower, a second tert-butyl alcohol recovery tower, a reflux unit, a first-stage rearrangement reactor, a spare circulating cooling unit, a first-stage rearrangement reaction unit and a discharging unit. According to the invention, materials in the kettle of the first tert-butyl alcohol recovery tower are pressurized by a first tert-butyl alcohol discharging pump and then transported to a cyclohexanone oxime rearrangement cooler via a pipeline to serve as a cold source instead of conventional circulating cooling water. The rearrangement cooler fully exchanges heat with a first-stage rearrangement reaction liquid to remove the cyclohexanone oxime rearrangement reaction heat. After heat exchange and temperature increase, the materials are transported to the upper middle portion of the second tert-butyl alcohol recovery tower via an insulated pipeline to carry out a tert-butyl alcohol evaporation recovery process, thereby reducing the circulating water cooling capacity required for reaction heat removal, saving circulating water and operating electricity costs, and reducing production costs.

Description

Technical Field

[0001] The invention belongs to the technical field of caprolactam, and particularly relates to a device for recovering tert-butyl alcohol using heat from the rearrangement reaction of cyclohexanone oxime. Background Art

[0002] Caprolactam (CPL) is a basic organic chemical raw material for the production of nylon 6 fiber and nylon 6 engineering plastics. Currently, the mainstream production processes for caprolactam are the cyclohexanone ammoximation method (cyclohexanone → cyclohexanone oxime) and the Beckmann liquid-phase rearrangement technique (cyclohexanone oxime → caprolactam). The cyclohexanone ammoximation method uses tert-butanol as a solvent and, in the presence of a catalyst, cyclohexanone directly reacts with ammonia and hydrogen peroxide to produce cyclohexanone oxime. Cyclohexanone oxime then undergoes Beckmann liquid-phase rearrangement to produce crude caprolactam, which is then refined to produce the caprolactam product.

[0003] Both the cyclohexanone ammoximation reaction and the Beckmann rearrangement reaction are highly exothermic reactions. Literature reports that the heat of reaction for cyclohexanone ammoximation is 300 kJ / mol oxime, and the heat of reaction for the rearrangement is 260 kJ / mol oxime. Comprehensive utilization of the reaction heat has important economic significance for energy conservation and consumption reduction, as well as carbon emission reduction.

[0004] At present, there is no search to find out that the heat of Beckmann rearrangement reaction is applied to the recovery of tert-butanol in the ammoximation unit, and there is no news of industrialization. The tert-butanol recovery unit of the reaction solvent is a major steam consumer in the ammoximation unit. Based on a 200,000 tons / year ammoximation unit, the low-pressure steam consumption of the tert-butanol recovery unit is more than 20t / h. Therefore, it is very necessary and meaningful for the caprolactam industry to improve and optimize the utilization method of the Beckmann rearrangement reaction heat of cyclohexanone oxime and design a device for recovering tert-butanol using the heat of cyclohexanone oxime rearrangement reaction. Summary of the Invention

[0005] The object of the present invention is to provide a device for recovering tert-butyl alcohol using heat from the rearrangement reaction of cyclohexanone oxime, so as to solve the problems raised in the above-mentioned background technology.

[0006] To achieve the above-mentioned object, the present invention provides the following technical solution: a cyclohexanone oxime rearrangement reaction heat for tert-butanol recovery device, comprising a first tert-butanol recovery tower and a second tert-butanol recovery tower, wherein one side of the top of the first tert-butanol recovery tower is connected to an ammoximation reaction supernatant inlet pipeline, the top output end of the first tert-butanol recovery tower is connected to a tert-butanol condenser, the bottom output end of the first tert-butanol recovery tower is connected to a first reboiler, the output end of the first reboiler is connected to the bottom input end of the first tert-butanol recovery tower, and the input end of the first reboiler is connected to the top output end of the second tert-butanol recovery tower. A steam pipeline is provided, the other output end of the first reboiler is connected to a tert-butanol reflux tank, a reflux unit is provided between the output end of the tert-butanol reflux tank and the first tert-butanol recovery tower, a first-stage rearrangement reactor is provided on one side of the first tert-butanol recovery tower, a second-stage rearrangement reactor is connected to one side of the first-stage rearrangement reactor, a spare circulation cooling unit is provided on one side of the first-stage rearrangement reactor, a first-stage rearrangement reaction unit coordinated with the spare circulation cooling unit is provided between the first-stage rearrangement reactor and the second tert-butanol recovery tower, and a discharging unit is provided on one side of the second tert-butanol recovery tower.

[0007] It should be noted that the reflux unit includes:

[0008] A gas phase reflux pipe is connected between the gas phase output end of the tert-butanol reflux tank and the input end of the tert-butanol condenser;

[0009] a tert-butanol reflux pump, wherein the input end of the tert-butanol reflux pump is connected to the liquid phase output end of the tert-butanol reflux tank;

[0010] a tert-butanol cooler, wherein the input end of the tert-butanol cooler is connected to the output end of the tert-butanol reflux pump;

[0011] The liquid phase reflux pipeline is arranged between the output end of the tert-butanol cooler and the input end on one side of the tower top of the first tert-butanol recovery tower.

[0012] As a preferred embodiment, the gas phase output end of the tert-butanol cooler is connected to a tert-butanol absorption tower and a water ring vacuum pump.

[0013] It is further worth noting that the standby circulating cooling unit includes:

[0014] a first-stage rearrangement circulation pump, wherein the input end of the first-stage rearrangement circulation pump is connected to the liquid phase output end of the first-stage rearrangement reactor;

[0015] A circulating water cooler, wherein the input end of the circulating water cooler is connected to the output end of the first-stage rearrangement circulating pump;

[0016] The cooling reflux pipeline has two ends connected to the output end of the circulating water cooler and the input end of a first-stage rearrangement reactor respectively.

[0017] It should be further explained that the one-stage rearrangement reaction unit includes:

[0018] a nicotinic acid feed pipeline, wherein the output end of the nicotinic acid feed pipeline is connected to the input end of a first-stage rearrangement circulation pump;

[0019] A cyclohexanone oxime pipeline, wherein the output end of the cyclohexanone oxime pipeline is connected to the input end of a first-stage rearrangement reactor;

[0020] a rearrangement cooler, wherein an output end of the rearrangement cooler is connected to a top side of the second tert-butyl alcohol recovery tower;

[0021] a first tert-butanol discharge pump, wherein the input end of the first tert-butanol discharge pump is connected to the output end of the first tert-butanol recovery tower, and the output end of the first tert-butanol discharge pump is connected to the input end of the rearrangement cooler;

[0022] A rearrangement liquid feeding pipeline, wherein the input end of the rearrangement liquid feeding pipeline is connected to the output end of a stage rearrangement circulation pump, and the output end of the rearrangement liquid feeding pipeline is connected to the other input end of the rearrangement cooler;

[0023] The input end of the rearrangement liquid reflux pipeline is connected to the other output end of the rearrangement cooler, and the output end of the rearrangement liquid reflux pipeline is connected to a stage of the rearrangement reactor.

[0024] As a preferred embodiment, the discharging unit includes:

[0025] a tert-butanol circulation pump, wherein an input end of the tert-butanol circulation pump is connected to an output end of the kettle of the second tert-butanol recovery tower;

[0026] a second reboiler, wherein an input end of the second reboiler is connected to an output end of the tert-butyl alcohol circulation pump;

[0027] a circulation pipeline, the circulation pipeline being connected to one side of the bottom of the second tert-butyl alcohol recovery tower;

[0028] a low-pressure pipeline, the low-pressure pipeline being connected to a heat source input end of the second reboiler;

[0029] a steam condensate collecting pipeline, the steam condensate collecting pipeline being connected to a cold source output end of the second reboiler;

[0030] a second tert-butanol discharge pump, wherein an input end of the second tert-butanol discharge pump is connected to an output end of the second tert-butanol recovery tower;

[0031] The oxime water extraction and distillation pipeline has an input end connected to the output end of the second tert-butyl alcohol recovery tower.

[0032] Compared with the prior art, the present invention provides a method for using heat from the rearrangement reaction of cyclohexanone oxime for a tert-butyl alcohol recovery device, which has at least the following beneficial effects:

[0033] (1) The feed to the second tert-butyl alcohol recovery tower is preheated from 72°C to 90°C using the heat of the first-stage rearrangement reaction of cyclohexanone oxime, which can significantly reduce the low-pressure steam consumption of the second reboiler at the second tert-butyl alcohol recovery tower.

[0034] (2) The feed of the first tert-butanol recovery tower and the second tert-butanol recovery tower is used as a cold source to replace the conventional circulating cooling water. The heat of the cyclohexanone oxime rearrangement reaction is fully removed through heat exchange with the first-stage rearrangement reaction liquid through the rearrangement cooler, which can reduce the circulating water cooling capacity required for removing the reaction heat, save circulating water and its operating electricity costs, and reduce production costs.

[0035] (3) When the rearrangement reactor encounters abnormal conditions such as shutdown, the second tert-butanol recovery tower can increase the low-pressure steam flow of its second reboiler to ensure the stability of the tower top kettle temperature, without affecting the normal operation of the first tert-butanol recovery tower and the second tert-butanol recovery tower; when the first tert-butanol recovery tower or the second tert-butanol recovery tower encounters abnormal conditions such as shutdown, the cold source of the rearrangement cooler can be switched to circulating water, without affecting the normal operation of the cyclohexanone oxime rearrangement reaction unit. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] Figure 1 It is a schematic diagram of the process structure of the reflux unit and the discharging unit of the present invention;

[0037] Figure 2 It is a schematic diagram of the process structure of the standby circulating cooling unit and the first-stage rearrangement reaction unit of the present invention.

[0038] In the figure: 1. First tert-butyl alcohol recovery tower; 2. Second tert-butyl alcohol recovery tower; 3. Ammoximation reaction supernatant inlet pipeline; 4. Tert-butyl alcohol condenser; 5. First reboiler; 6. Steam pipeline; 7. Tert-butyl alcohol reflux tank; 8. Reflux unit; 81. Gas reflux pipe; 82. Tert-butyl alcohol reflux pump; 83. Tert-butyl alcohol cooler; 84. Liquid reflux pipeline; 9. First stage rearrangement reactor; 10. Second stage rearrangement reactor; 11. Spare circulating cooling unit; 111. First stage rearrangement circulating pump; 112. Circulating water cooler; 113. Cooling reflux pipeline; 12. One-stage rearrangement reaction unit; 121. Nicotinic acid feed pipeline; 122. Cyclohexanone oxime pipeline; 123. Rearrangement cooler; 124. First tert-butanol discharge pump; 125. Rearrangement liquid feed pipeline; 126. Rearrangement liquid reflux pipeline; 13. Discharge unit; 131. tert-butanol circulation pump; 132. Second reboiler; 133. Circulation pipeline; 134. Low-pressure pipeline; 135. Steam condensate collection pipeline; 136. Second tert-butanol discharge pump; 137. Oxime water extraction and distillation pipeline; 14. tert-butanol absorption tower; 15. Water ring vacuum pump. DETAILED DESCRIPTION

[0039] The present invention will be further described below with reference to the embodiments.

[0040] See also Figure 1-2 The present invention provides a tert-butanol recovery device for using heat from the rearrangement reaction of cyclohexanone oxime, comprising a first tert-butanol recovery tower 1 and a second tert-butanol recovery tower 2. The top side of the first tert-butanol recovery tower 1 is connected to an ammoximation reaction supernatant liquid inlet pipeline 3, the top output end of the first tert-butanol recovery tower 1 is connected to a tert-butanol condenser 4, the bottom output end of the first tert-butanol recovery tower 1 is connected to a first reboiler 5, the output end of the first reboiler 5 is connected to the bottom input end of the first tert-butanol recovery tower 1, the input end of the first reboiler 5 is connected to the top output end of the second tert-butanol recovery tower 2 via a steam pipeline 6, and the bottom output end of the first tert-butanol recovery tower 1 is connected to a steam pipeline 6. The other output end of the reboiler 5 is connected to a tert-butanol reflux tank 7, a reflux unit 8 is provided between the output end of the tert-butanol reflux tank 7 and the first tert-butanol recovery tower 1, a first-stage rearrangement reactor 9 is provided on one side of the first tert-butanol recovery tower 1, a second-stage rearrangement reactor 10 is provided on one side of the first-stage rearrangement reactor 9, a spare circulating cooling unit 11 is provided on one side of the first-stage rearrangement reactor 9, a first-stage rearrangement reaction unit 12 coordinated with the spare circulating cooling unit 11 is provided between the first-stage rearrangement reactor 9 and the second tert-butanol recovery tower 2, and a discharging unit 13 is provided on one side of the second tert-butanol recovery tower 2.

[0041] Further as Figure 1 As shown, it is worth noting that the reflux unit 8 includes a gas phase reflux pipe 81, which is connected between the gas phase output end of the tert-butanol reflux tank 7 and the input end of the tert-butanol condenser 4;

[0042] a tert-butanol reflux pump 82, wherein the input end of the tert-butanol reflux pump 82 is connected to the liquid phase output end of the tert-butanol reflux tank 7;

[0043] a tert-butanol cooler 83, wherein the input end of the tert-butanol cooler 83 is connected to the output end of the tert-butanol reflux pump 82;

[0044] The liquid reflux pipeline 84 is provided between the output end of the tert-butanol cooler 83 and the input end on the top side of the first tert-butanol recovery tower 1 .

[0045] Further as Figure 1 As shown, it is worth noting that the gas phase output end of the tert-butanol cooler 83 is connected to the tert-butanol absorption tower 14 and the water ring vacuum pump 15.

[0046] It is worth noting that: the cyclohexanone ammoximation reaction supernatant enters the first tert-butanol recovery tower 1 through the ammoximation reaction supernatant liquid inlet pipeline 3 to begin evaporation and condensation to recover tert-butanol. The first tert-butanol recovery tower 1 uses the top of the second tert-butanol recovery tower 2 as a heat source, wherein the top vapor of the second tert-butanol recovery tower 2 is cooled after heat exchange in the first reboiler 5 and enters the tert-butanol reflux tank 7. The material in the tert-butanol reflux tank 7 enters the tert-butanol cooler 83 through the tert-butanol reflux pump 82 for further cooling, wherein the liquid phase refluxes into the top of the first tert-butanol recovery tower 1, and the uncondensed gas phase enters the tert-butanol absorption tower 14 and the water ring vacuum pump 15 for further absorption.

[0047] Further as Figure 2 As shown, it is worth noting that the standby circulating cooling unit 11 includes a first stage rearrangement circulating pump 111, and the input end of the first stage rearrangement circulating pump 111 is connected to the liquid phase output end of the first stage rearrangement reactor 9;

[0048] A circulating water cooler 112, the input end of the circulating water cooler 112 is connected to the output end of a first-stage rearrangement circulating pump 111;

[0049] The cooling reflux pipeline 113 has two ends connected to the output end of the circulating water cooler 112 and the input end of the first stage rearrangement reactor 9 respectively.

[0050] Further as Figure 1 and Figure 2 As shown, it is worth noting that the first stage rearrangement reaction unit 12 includes a nicotinic acid feed pipeline 121, and the output end of the nicotinic acid feed pipeline 121 is connected to the input end of the first stage rearrangement circulation pump 111;

[0051] A cyclohexanone oxime pipeline 122, wherein the output end of the cyclohexanone oxime pipeline 122 is connected to the input end of the first-stage rearrangement reactor 9;

[0052] A rearrangement cooler 123, wherein the output end of the rearrangement cooler 123 is connected to the top side of the second tert-butyl alcohol recovery tower 2;

[0053] a first tert-butanol discharge pump 124, wherein the input end of the first tert-butanol discharge pump 124 is connected to the output end of the first tert-butanol recovery tower 1, and the output end of the first tert-butanol discharge pump 124 is connected to the input end of the rearrangement cooler 123;

[0054] The input end of the rearrangement liquid feeding pipeline 125 is connected to the output end of the first stage rearrangement circulation pump 111, and the output end of the rearrangement liquid feeding pipeline 125 is connected to the other input end of the rearrangement cooler 123;

[0055] The input end of the rearrangement liquid reflux pipeline 126 is connected to the other output end of the rearrangement cooler 123 , and the output end of the rearrangement liquid reflux pipeline 126 is connected to a stage of the rearrangement reactor 9 .

[0056] It should be noted that the rearrangement cooler 123 uses a high-efficiency heat exchanger to break the laminar bottom layer of the fluid inside and outside the tube, thereby enhancing the heat transfer efficiency. Compared with an ordinary shell-and-tube heat exchanger, the heat transfer efficiency is greatly improved.

[0057] Further as Figure 1 As shown, it is worth noting that the discharge unit 13 includes a tert-butanol circulation pump 131, and the input end of the tert-butanol circulation pump 131 is connected to the output end of the bottom of the second tert-butanol recovery tower 2;

[0058] a second reboiler 132 , wherein an input end of the second reboiler 132 is connected to an output end of the tert-butyl alcohol circulation pump 131 ;

[0059] A circulation line 133 is connected to the bottom of the second tert-butyl alcohol recovery tower 2;

[0060] A low-pressure pipeline 134 is connected to the heat source input end of the second reboiler 132;

[0061] The steam condensate collecting pipeline 135 is connected to the cold source output end of the second reboiler 132;

[0062] a second tert-butanol discharge pump 136, wherein the input end of the second tert-butanol discharge pump 136 is connected to the output end of the second tert-butanol recovery tower 2;

[0063] The oxime water extraction and distillation pipeline 137 has an input end connected to the output end of the second tert-butanol recovery tower 2 .

[0064] This solution has the following working process: the temperature of the bottom of the first tert-butanol recovery tower 1 is 72°C, and the oxime / tert-butanol / water and other materials in the bottom of the tower are pressurized by the first tert-butanol discharge pump 124 and then transported to the cyclohexanone oxime rearrangement cooler 123 through a pipeline. The branch pipeline of the original circulating water cooler 112 is retained as a standby as a cold source to replace the conventional circulating cooling water. The rearrangement cooler 123 fully exchanges heat with the first stage of rearrangement reaction liquid to remove the heat of the cyclohexanone oxime rearrangement reaction. After heat exchange and temperature increase, the materials are heated to 90°C and transported to the upper middle part of the second tert-butanol recovery tower 2 through an insulated pipeline to continue the tert-butanol evaporation recovery process;

[0065] The bottom material of the second tert-butanol recovery tower 2 is transported through the tert-butanol circulation pump 131 and the second reboiler 132, where it is heated with low-pressure steam as a heat source and then returned to the bottom of the tower. The tert-butanol in the bottom material is continuously evaporated while providing a heat source for the first tert-butanol recovery tower 1. Another portion of the bottom material of the second tert-butanol recovery tower 2 is transported through the discharge pump of the second tert-butanol recovery tower 2 to the oxime water extraction and distillation pipeline 137, and enters the subsequent process to obtain high-purity cyclohexanone oxime through a toluene extraction device and an oxime distillation device.

[0066] After filtration, pure cyclohexanone oxime directly enters the first-stage rearrangement reactor 9 through a pipeline. Nicotinic acid, another raw material for the rearrangement reaction, enters the front-end branch line of the inlet of the first-stage rearrangement circulation pump 111 through the nicotinic acid feed pipeline 121 and enters the rearrangement liquid pipeline. The rearrangement liquid is pressurized by the first-stage rearrangement circulation pump 111 and then enters the rearrangement cooler 123. The rearrangement liquid and the discharge from the bottom of the first tert-butanol recovery tower 1 are fully heat-exchanged through the rearrangement cooler 123 and then circulated back to the first-stage rearrangement reactor 9. The rearrangement reaction heat is transferred, and the heated tert-butanol / oxime water material enters the top of the second tert-butanol recovery tower 2. The cyclohexanone oxime in the rearrangement liquid undergoes a partial rearrangement reaction in the first-stage rearrangement reactor 9. Thereafter, the rearrangement liquid enters the second-stage rearrangement reactor 10 through the discharge port of the first-stage rearrangement reactor 9 under the action of pressure difference for further reaction to obtain a rearrangement liquid containing a large amount of caprolactam, and finally enters the rearrangement liquid buffer tank.

[0067] The circulating water cooling branch pipeline composed of the circulating water cooler 112 and the cooling return pipeline 113 serves as a backup pipeline.

[0068] According to the above working process, the material in the bottom of the first tert-butanol recovery tower 1 is pressurized by the first tert-butanol discharge pump 124 and then transported to the cyclohexanone oxime rearrangement cooler 123 via a pipeline. The cyclohexanone oxime rearrangement reaction heat is removed by sufficient heat exchange with the first stage rearrangement reaction liquid in the rearrangement cooler 123. After heat exchange and temperature increase, the material is transported to the upper middle part of the second tert-butanol recovery tower 2 via an insulated pipeline to continue the tert-butanol evaporation recovery process.

[0069] The feed to the second tert-butanol recovery tower 2 is preheated from 72°C to 90°C using the heat of the first-stage rearrangement reaction of cyclohexanone oxime, which can significantly reduce the low-pressure steam consumption of the second reboiler 132 at the second tert-butanol recovery tower 2;

[0070] The feeds from the first tert-butanol recovery tower 1 and the second tert-butanol recovery tower 2 are used as a cold source to replace conventional circulating cooling water. The heat of the cyclohexanone oxime rearrangement reaction is fully exchanged with the first-stage rearrangement reaction liquid through the rearrangement cooler 123, thereby reducing the circulating water cooling capacity required for removing the reaction heat, saving circulating water and operating electricity costs, and reducing production costs.

[0071] It should be noted that the low-pressure steam consumption at the second reboiler 132 saves more than 50% of the energy consumption ratio compared to the conventional process;

[0072] When the rearrangement reactor stops or encounters abnormal conditions, the second tert-butanol recovery tower 2 can increase the low-pressure steam flow rate of its second reboiler 132 to ensure the stability of the tower top and bottom temperature without affecting the normal operation of the first tert-butanol recovery tower 1 and the second tert-butanol recovery tower 2;

[0073] When the first tert-butanol recovery tower 1 or the second tert-butanol recovery tower 2 stops or encounters abnormal conditions, the cold source of the rearrangement cooler 123 can be switched to circulating water without affecting the normal operation of the cyclohexanone oxime rearrangement reaction unit.

Claims

1. A cyclohexanone oxime rearrangement reaction heat for tert-butanol recovery device, comprising a first tert-butanol recovery tower (1) and a second tert-butanol recovery tower (2), characterized in that: One side of the top of the first tert-butanol recovery tower (1) is connected to an ammoximation reaction clear liquid inlet pipeline (3), the top output end of the first tert-butanol recovery tower (1) is connected to a tert-butanol condenser (4), the bottom output end of the first tert-butanol recovery tower (1) is connected to a first reboiler (5), the output end of the first reboiler (5) is connected to the bottom input end of the first tert-butanol recovery tower (1), the input end of the first reboiler (5) is connected to the top output end of the second tert-butanol recovery tower (2) via a steam pipeline (6), the other output end of the first reboiler (5) is connected to a tert-butanol reflux tank (7), and the tert-butanol reflux tank (8) is connected to the bottom input end of the first tert-butanol recovery tower (1). A reflux unit (8) is provided between the output end of the butanol reflux tank (7) and the first tert-butanol recovery tower (1); a first-stage rearrangement reactor (9) is provided on one side of the first tert-butanol recovery tower (1); a second-stage rearrangement reactor (10) is provided on one side of the first-stage rearrangement reactor (9); a spare circulation cooling unit (11) is provided on one side of the first-stage rearrangement reactor (9); a first-stage rearrangement reaction unit (12) coordinated with the spare circulation cooling unit (11) is provided between the first-stage rearrangement reactor (9) and the second tert-butanol recovery tower (2); and a discharge unit (13) is provided on one side of the second tert-butanol recovery tower (2); The standby circulating cooling unit (11) comprises: a first-stage rearrangement circulation pump (111), wherein the input end of the first-stage rearrangement circulation pump (111) is connected to the liquid phase output end of the first-stage rearrangement reactor (9); a circulating water cooler (112), wherein an input end of the circulating water cooler (112) is connected to an output end of the first-stage rearrangement circulating pump (111); A cooling reflux pipeline (113), wherein both ends of the cooling reflux pipeline (113) are respectively connected to the output end of the circulating water cooler (112) and the input end of the first stage rearrangement reactor (9); The one-stage rearrangement reaction unit (12) comprises: A nicotinic acid feed pipeline (121), wherein the output end of the nicotinic acid feed pipeline (121) is connected to the input end of a first-stage rearrangement circulation pump (111); A cyclohexanone oxime pipeline (122), wherein the output end of the cyclohexanone oxime pipeline (122) is connected to the input end of the first-stage rearrangement reactor (9); a rearrangement cooler (123), wherein the output end of the rearrangement cooler (123) is connected to one side of the top of the second tert-butyl alcohol recovery tower (2); a first tert-butanol discharge pump (124), wherein the input end of the first tert-butanol discharge pump (124) is connected to the output end of the first tert-butanol recovery tower (1), and the output end of the first tert-butanol discharge pump (124) is connected to the input end of the rearrangement cooler (123); A rearrangement liquid feed line (125), wherein the input end of the rearrangement liquid feed line (125) is connected to the output end of a stage rearrangement circulation pump (111), and the output end of the rearrangement liquid feed line (125) is connected to the other input end of the rearrangement cooler (123); The rearrangement liquid reflux pipeline (126) has an input end connected to the other output end of the rearrangement cooler (123), and an output end of the rearrangement liquid reflux pipeline (126) is connected to a rearrangement reactor (9).

2. The device for recovering tert-butyl alcohol using heat from the rearrangement reaction of cyclohexanone oxime according to claim 1, characterized in that: The reflux unit (8) comprises: A gas phase reflux pipe (81), the gas phase reflux pipe (81) is connected between the gas phase output end of the tert-butanol reflux tank (7) and the input end of the tert-butanol condenser (4); a tert-butanol reflux pump (82), wherein the input end of the tert-butanol reflux pump (82) is connected to the liquid phase output end of the tert-butanol reflux tank (7); a tert-butanol cooler (83), wherein the input end of the tert-butanol cooler (83) is connected to the output end of the tert-butanol reflux pump (82); The liquid phase reflux pipeline (84) is provided at the output end of the tert-butanol cooler (83) and the input end on the top side of the first tert-butanol recovery tower (1).

3. The device for recovering tert-butyl alcohol using heat from the rearrangement reaction of cyclohexanone oxime according to claim 2, wherein: The gas phase output end of the tert-butanol cooler (83) is connected to a tert-butanol absorption tower (14) and a water ring vacuum pump (15).

4. The device for recovering tert-butyl alcohol using heat from the rearrangement reaction of cyclohexanone oxime according to claim 3, wherein: The discharging unit (13) comprises: a tert-butanol circulation pump (131), wherein the input end of the tert-butanol circulation pump (131) is connected to the output end of the bottom of the second tert-butanol recovery tower (2); a second reboiler (132), wherein an input end of the second reboiler (132) is connected to an output end of the tert-butyl alcohol circulation pump (131); A circulation pipeline (133), the circulation pipeline (133) is connected to one side of the bottom of the second tert-butyl alcohol recovery tower (2); A low-pressure pipeline (134), the low-pressure pipeline (134) is connected to the heat source input end of the second reboiler (132); a steam condensate collecting pipeline (135), the steam condensate collecting pipeline (135) being connected to a cold source output end of the second reboiler (132); a second tert-butanol discharge pump (136), wherein the input end of the second tert-butanol discharge pump (136) is connected to the output end of the second tert-butanol recovery tower (2); The oxime water extraction and distillation pipeline (137) has an input end connected to the output end of the second tert-butyl alcohol recovery tower (2).

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