A kind of alcohol amine product production system and process

Abstract

The invention discloses an alcoholamine product production system, comprising a raw material metering and feeding device, a premixer, a retention and maturation device, a hot water circulation device, a condensate recovery device, an ammonia distillation device, a dehydration device, a vacuum device, a tail gas absorption device, a monoethyl distillation device, a diethyl distillation device and a triethyl distillation device. The invention realizes efficient, energy-saving and environmentally friendly production of alcoholamine products by optimizing the production process and adopting advanced production equipment.

Description

Technical Field

[0001] The invention belongs to the field of chemical equipment, and in particular relates to an alcohol amine product production system. Background Art

[0002] Alcoholamine products, including monoethanolamine, diethanolamine and triethanolamine, are widely used in chemical, pharmaceutical, textile, pesticide and other fields. The production process of traditional alkanolamine products has problems such as high energy consumption, unstable product quality and low production efficiency. Therefore, the development of an efficient, energy-saving and environmentally friendly alkanolamine production system and process is of great significance to improve the quality and market competitiveness of alkanolamine products. Summary of the invention

[0003] The technical problem to be solved by the present invention is to provide an olamine product production system in view of the above-mentioned deficiencies in the prior art, and to achieve efficient, energy-saving and environmentally friendly production of olamine products by optimizing the production process and adopting advanced production equipment.

[0004] The technical solution adopted by the present invention is: an alcohol amine product production system, a raw material metering and feeding device, used for metering and continuously feeding ethylene oxide, liquid ammonia and a catalyst;

[0005] A premixer, used for fully mixing the ethylene oxide, liquid ammonia and catalyst in the axial and radial directions;

[0006] The reactor is a tubular reactor, which is divided into several reaction sections, each of which is connected to a corresponding pre-mixer outlet for continuous reaction;

[0007] A retention aging device is connected to the outlet of one of the reaction sections of the reactor to ensure that the ethylene oxide in the reaction material reacts completely;

[0008] A hot water circulation device, used to provide the reactor with hot water required for heating or cooling;

[0009] Condensate recovery device, used to recover and reuse steam condensate;

[0010] an ammonia distillation device, receiving the pretreated alcoholamine raw material, and separating ammonia and water in the alcoholamine raw material in a gaseous form by heating, wherein the ammonia distillation device comprises an ammonia distillation tower, an ammonia distillation tower reboiler, an ammonia distillation tower condenser and an ammonia flash tank, wherein the ammonia distillation tower is divided into an ammonia distillation flash section and an ammonia distillation section, wherein the ammonia distillation flash section is used for preliminary separation of ammonia gas, and the ammonia distillation section is used for further separation of ammonia and water, wherein the ammonia distillation tower reboiler provides heat to maintain vaporization of materials in the ammonia distillation section, wherein the ammonia distillation tower condenser is used for condensing the separated ammonia gas, and the ammonia flash tank is used for further removing residual ammonia in the materials under reduced pressure conditions;

[0011] The dehydration device receives the alcoholamine mixture output from the ammonia distillation device and removes the water therein by vacuum distillation;

[0012] A vacuum device, connected to the dehydration device, used to maintain a vacuum state of the dehydration device;

[0013] The tail gas absorption device receives the exhaust gas generated by each process in the system, absorbs the ammonia, EO and water therein through the absorption liquid, and the absorption liquid is recycled and partly transported to the reactor for recycling;

[0014] An ethylene distillation device is used to separate the ethylene product from the mixed ethanolamine, including an ethylene feed flash tank, an ethylene tower, an ethylene tower top internal condenser, an ethylene reboiler, an ethylene tower bottom circulation pump, an ethylene product pump and an ethylene product cooler, and a matching ethylene vacuum unit;

[0015] The diethyl distillation device is used to receive the heavy component materials from the bottom of the first ethyl tower and separate the diethanolamine product, including the diethyl tower, the condenser in the top of the diethyl tower, the diethyl reboiler, the diethyl tower bottom circulation pump, the diethyl product extraction pump and the diethyl product cooler, and the supporting diethyl vacuum unit, wherein a light component distillation layer is added to the upper part of the diethyl tower distillation section to further improve the quality of the diethanolamine product;

[0016] The triethyl distillation device is used to receive the heavy component materials from the diethyl tower kettle and separate the triethanolamine product, including the triethyl tower, the condenser inside the triethyl tower top, the triethyl reboiler, the triethyl tower bottom circulation pump, the triethyl product pump and the triethyl product cooler, and the supporting triethyl vacuum unit;

[0017] The 1-ethyl distillation unit, the 2-ethyl distillation unit and the 3-ethyl distillation unit all adopt high-efficiency falling film evaporators for forced external circulation heating and reboiling. Each tower is equipped with a product side line discharge and head shaking device to achieve effective separation and reflux of components. At the same time, each vacuum unit contains a four-stage high vacuum pump to achieve distillation operation under high vacuum conditions.

[0018] In one embodiment, the ammonia evaporation tower flash section of the ammonia evaporation tower is provided with a first demister, a vaporization chamber and a heater, and the heater is a shell-and-tube heat exchanger, and low-pressure steam or hot water is passed between the tubes.

[0019] In one of the embodiments, the dehydration tower rectification section and the dehydration tower stripping section of the dehydration tower are provided with structured corrugated packing, a fluid distributor and a liquid redistributor.

[0020] In one embodiment, the vacuum ejector has an air suction port connected to a vacuum pipe port of a reflux tank, a liquid inlet connected to an outlet of a circulation pump, and an ejection port installed on the top of a catalyst collecting tank.

[0021] In one embodiment, the upper section of the tail gas absorption tower is a packed tower, and the lower section is an absorption liquid storage tank. The circulating absorption liquid is continuously transported by a circulating pump at the bottom of the tower to an absorption liquid cooler for cooling and then returned to the top of the absorption tower for spraying.

[0022] In one embodiment, the ethylene tower, the ethylene tower and the ethylene tower all include a distillation section and a stripping section, wherein the distillation section is provided with a product collecting tank, a reflux liquid distributor and fillers, and the stripping section is provided with a feed liquid redistributor, fillers and a tower bottom, and the material is in reverse contact with the reflux liquid and reboiling steam in the tower to achieve mass transfer, heat transfer and component separation.

[0023] In one embodiment, the condenser at the top of the 1 ethylene tower, the condenser at the top of the 2 ethylene tower and the condenser at the top of the 3 ethylene tower are all horizontal shell and tube heat exchangers, which are used to remove heat from the tower, condense the vapor at the top of the tower and form reflux liquid in the tower.

[0024] In one embodiment, the one ethylene reboiler, the two ethylene reboilers and the three ethylene reboilers are all falling film evaporators, which are used to provide the heat required for distillation to achieve continuous vaporization and separation of materials.

[0025] The present invention also discloses a process for producing an olamine product, which is realized by the olamine product production system according to any one of claims 1 to 8, and comprises the following steps:

[0026] Step 1, metering and continuously feeding ethylene oxide, liquid ammonia and catalyst into a premixer;

[0027] Step 2: fully mixing the materials in a premixer;

[0028] Step 3, continuously feeding the mixed materials into the reactor for reaction;

[0029] Step 4: sending the reacted material into a retention aging device for aging treatment, providing the required heating or cooling hot water for the reactor through a hot water circulation device, recovering and reusing steam condensate, and obtaining an alcoholamine raw material;

[0030] Step 5: feeding the alcohol amine raw material into an ammonia distillation device, separating ammonia and water by heating, recovering the ammonia gas after condensation, and further removing residual ammonia by flash distillation under reduced pressure;

[0031] Step 6: sending the alcoholamine mixture output from the ammonia distillation device to a dehydration device to remove water by distillation under vacuum conditions;

[0032] Step 7: Use a vacuum device to maintain the vacuum state of the dehydration device, remove the non-condensable gas in the system, and obtain a mixed ethanolamine material;

[0033] Step 8, after the mixed ethanolamine material is subjected to ammonia evaporation and dehydration treatment, it is continuously sent to a monoethanolamine distillation device for distillation to separate the monoethanolamine product;

[0034] Step 9, sending the heavy component materials in the bottom of the first ethyl tower to the diethyl distillation device for distillation to separate the diethanolamine product, and at the same time, returning the light component materials containing monoethanolamine to the first ethyl tower for reprocessing;

[0035] Step 10, sending the heavy component materials in the diethyl tower kettle to a triethyl distillation device for distillation to separate the triethanolamine product, and at the same time, returning the light component materials containing diethanolamine to the diethyl tower for further treatment;

[0036] Step 11. In each distillation unit, forced external circulation heating and reboiling are performed through a high-efficiency falling film evaporator, effective separation and reflux of components are achieved through a product side line discharge and a head-swing device, and a distillation operation under a high vacuum state is achieved through a four-stage high vacuum pump to obtain high-quality monoethanolamine, diethanolamine and triethanolamine products.

[0037] The beneficial effects of the present invention are:

[0038] 1. The present invention realizes the efficient, energy-saving and environmentally friendly production of alcoholamine products by optimizing the production process and adopting advanced production equipment;

[0039] 2. The ammonia evaporation device and the dehydration device of the present invention effectively remove ammonia and water from the alcoholamine raw material, thereby improving the purity of the product;

[0040] 3. The distillation device of the present invention adopts a high-efficiency falling film evaporator to perform a forced external circulation heating and reboiling method, thereby improving the distillation efficiency and product quality;

[0041] 4. The vacuum device and tail gas absorption device of the present invention ensure the stable operation of the system and environmental protection;

[0042] 5. The process steps of the present invention are reasonable, the operation is simple, and it is easy to realize industrial production. BRIEF DESCRIPTION OF THE DRAWINGS

[0043] Figure 1 It is a structural block diagram of the present invention;

[0044] Figure 2 This is a flow chart of the ammonia evaporation, dehydration and refining system of the present invention;

[0045] Figure 3 This is a schematic diagram of the structure of the ammonia distillation tower of the present invention;

[0046] Figure 4 This is a schematic diagram of the tower tray structure of the present invention;

[0047] Figure 5 It is a schematic diagram of the structure of the dehydration tower of the present invention;

[0048] Figure 6 It is a schematic diagram of the refining tower structure of the present invention.

[0049] In the figure: 1. Raw material metering and feeding device; 2. Premixer; 3. Reactor; 4. Retention and maturation device; 5. Hot water circulation device; 6. Condensate recovery device; 7. Ammonia distillation device; 8. Dehydration device; 9. Vacuum device; 10. Tail gas absorption device; 11. One ethyl distillation device; 12. Two ethyl distillation device; 13. Three ethyl distillation device; 71. Ammonia distillation tower; 72. Ammonia distillation tower reboiler; 73. Ammonia distillation tower condenser; 74. Ammonia flash tank; 711. Ammonia distillation tower body; 712. Ammonia distillation tower kettle; 713. Ammonia distillation tower skirt; 714. Head; 715. Ammonia distillation tower flash section; 716. Ammonia distillation tower distillation section; 717. Ammonia distillation tower gas phase outlet; 718. First demister; 719. Heater; 7110. Vaporization chamber; 71 11. Ammonia still tower feed port; 7112. Upper steam inlet; 7113. Upper condensate outlet; 7114. Ammonia still tower upper bottom outlet; 7115. Second demister; 7116. Tower tray; 7117. Ammonia still tower lower gas phase outlet; 7118. Ammonia still tower lower material inlet; 7119. Ammonia still tower reboiler return port; 7120. Ammonia still tower discharge port; 7121. Ammonia still tower steam coil; 7122. Ammonia still tower external heating steam inlet; 7123. Ammonia still tower external heating condensate outlet; 7124. Ammonia still tower conical transition section; 7125. Exhaust port; 7126. Drain port; 7127. Ammonia still tower feed baffle; 7128. Ammonia still tower anti-vortex baffle; 71161. Liquid receiving pan; 71162. Tower tray; 7 1163, water retaining plate; 71164, downcomer; 81, dehydration tower; 82, dehydration condenser; 83, reflux tank; 811, dehydration tower body; 812, dehydration tower kettle; 813, dehydration tower skirt; 814, fluid distributor; 815, dehydration tower rectification section; 816, dehydration tower stripping section; 817, dehydration tower gas phase outlet; 818, dehydration tower upper section packing support grid; 819, dehydration tower reflux port; 8110, dehydration tower feed port; 8111, dehydration tower lower section packing support grid; 8112, dehydration tower reboiler return port; 8113, dehydration tower discharge port; 8114, dehydration tower steam coil; 8115, dehydration tower external heating steam inlet; 8116, dehydration tower external heating condensate outlet; 8117, dehydration Tower elliptical head; 8118, dehydration tower feed baffle; 8119, dehydration tower anti-vortex baffle; 111, 1-ethylene tower; 112, 1-ethylene tower top internal condenser; 113, 1-ethylene reboiler; 114, 1-ethylene tower bottom circulation pump; 115, 1-ethylene product pump; 116, 1-ethylene product cooler; 121, 2-ethylene tower; 122, 2-ethylene tower top internal condenser; 123, 2-ethylene reboiler; 124, 2-ethylene tower bottom circulation pump; 125, 2-ethylene product extraction pump; 126, 2-ethylene product cooler; 131, 3-ethylene tower; 132, 3-ethylene tower top internal condenser; 133, 3-ethylene reboiler; 134, 3-ethylene tower bottom circulation pump; 135, 3-ethylene product pump; 136, 3-ethylene product cooler; 1311, refining tower body; 1312, refining tower kettle;1313, refining tower skirt; 1314, condenser in the tower top; 1315, refining tower feed port; 1316, refining tower rectifying section; 1317, refining tower stripping section; 1318, tower product collecting tank; 1319, refining tower reflux liquid distributor; 13110, refining tower upper section packing support grid; 13111, first refining tower product discharge port; 13112, second refining tower product discharge port; 13113, refining tower reflux port; 13114, liquid distributor; 1311 5. Filler support grid for the lower section of the refining tower; 13116. Refining tower reboiler return port; 13117. Refining tower discharge port; 13118. Refining tower steam coil; 13119. Refining tower external heating steam inlet; 13120. Refining tower external heating condensate outlet; 13121. First refining tower feed baffle; 13122. Cone shell; 13123. Distributor connecting pipe; 13124. Crossbeam; 13125. Second refining tower feed baffle; 13126. Refining tower anti-vortex baffle. ; DETAILED DESCRIPTION

[0050] The present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments.

[0051] like Figure 1-Figure 6 As shown, a system for producing an alcohol amine product comprises:

[0052] A raw material metering and feeding device 1, used for metering and continuously feeding ethylene oxide, liquid ammonia and catalyst;

[0053] A premixer 2 is used to fully mix the ethylene oxide, liquid ammonia and catalyst in the axial and radial directions;

[0054] Reactor 3 is a tubular reactor 3, which is divided into several reaction sections, each reaction section is connected to the corresponding outlet of premixer 2, for continuous reaction;

[0055] The retention aging device 4 is connected to the outlet of one of the reaction sections of the reactor 3 to ensure that the ethylene oxide in the reaction material reacts completely;

[0056] A hot water circulation device 5, used to provide the reactor 3 with hot water required for heating or cooling;

[0057] A condensate recovery device 6, for recovering and reusing steam condensate;

[0058] an ammonia evaporation device 7, which receives the pretreated alcoholamine raw material and separates ammonia and water in the alcoholamine raw material in a gaseous form by heating. The ammonia evaporation device 7 comprises an ammonia evaporation tower 71, an ammonia evaporation tower reboiler 72, an ammonia evaporation tower condenser 73 and an ammonia flash tank 74. The ammonia evaporation tower 71 is divided into an ammonia evaporation flash section and an ammonia evaporation distillation section. The ammonia evaporation flash section is used for preliminary separation of ammonia gas, and the ammonia evaporation distillation section is used for further separation of ammonia and water. The ammonia evaporation tower reboiler 72 provides heat to maintain vaporization of the material in the ammonia evaporation distillation section. The ammonia evaporation tower condenser 73 is used for condensing the separated ammonia gas, and the ammonia flash tank 74 is used for further removing residual ammonia in the material under reduced pressure conditions;

[0059] The dehydration device 8 receives the alcoholamine mixture outputted from the ammonia evaporation device 7 and removes the water therein by vacuum distillation. The dehydration device 8 comprises a dehydration tower 81, a dehydration condenser 82 and a reflux tank 83. The dehydration tower 81 is divided into a dehydration tower distillation section 815 and a dehydration tower stripping section 816. The dehydration condenser 82 is used to condense the tower top gas, and the reflux tank 83 is used to receive the condensate and partially reflux it to the dehydration tower 81.

[0060] A vacuum device 9, connected to the dehydration device 8, used to maintain the vacuum state of the dehydration device 8, including a vacuum ejector, a catalyst collection tank, a circulation pump and a circulation liquid cooler, wherein the circulation pump drives the circulation liquid to circulate among the catalyst collection tank, the circulation liquid cooler and the vacuum ejector to remove the non-condensable gas in the system;

[0061] The tail gas absorption device 10 receives the exhaust gas generated by each process in the system, absorbs ammonia, EO and water therein through an absorption liquid, and the absorption liquid is recycled and partially transported to the reactor 3 for recycling. The tail gas absorption device 10 includes a tail gas absorption tower, a tower bottom circulation pump and a circulating liquid cooler;

[0062] An ethylene distillation device 11 is used to separate the ethylene product from the mixed ethanolamine, and comprises an ethylene feed flash tank, an ethylene tower 111, an ethylene tower top internal condenser 112, an ethylene reboiler 113, an ethylene tower bottom circulating pump 114, an ethylene product pump 115 and an ethylene product cooler 116, and a matching ethylene vacuum unit;

[0063] The diethyl distillation device 12 is used to receive the heavy component materials from the kettle of the first ethyl tower 111 and separate the diethanolamine product, including the diethyl tower 121, the diethyl tower top internal condenser 122, the diethyl reboiler 123, the diethyl tower bottom circulation pump 124, the diethyl product extraction pump 125 and the diethyl product cooler 126, and the matching diethyl vacuum unit, wherein a light component distillation layer is added to the upper part of the diethyl tower distillation section to further improve the quality of the diethanolamine product;

[0064] The triethyl distillation device 13 is used to receive the heavy component materials from the kettle of the diethyl tower 121 and separate the triethanolamine product, including a triethyl tower 131, a triethyl tower top internal condenser 132, a triethyl reboiler 133, a triethyl tower bottom circulating pump 134, a triethyl product pump 135 and a triethyl product cooler 136, and a matching triethyl vacuum unit;

[0065] The ethylene distillation unit 11, the diethylene distillation unit 12 and the triethylene distillation unit 13 all adopt a high-efficiency falling film evaporator for forced external circulation heating and reboiling. Each tower is provided with a product side line discharge and a head shaking device to achieve effective separation and reflux of the components. At the same time, each vacuum unit includes a four-stage high vacuum pump to achieve distillation operation under high vacuum conditions.

[0066] In this embodiment, the ammonia evaporation tower flash section 715 of the ammonia evaporation tower 71 is provided with a first demister 718, a vaporization chamber 7110 and a heater 719. The heater 719 is a shell-and-tube heat exchanger, and low-pressure steam or hot water is passed between the tubes.

[0067] In this embodiment, the dehydration tower rectification section 815 and the dehydration tower stripping section 816 of the dehydration tower 81 are provided with regular corrugated packing, a fluid distributor 814 and a liquid redistributor.

[0068] In this embodiment, the air extraction port of the vacuum ejector is connected to the vacuum pipe port of the reflux tank 83, the liquid inlet is connected to the outlet of the circulation pump, and the ejection port is installed on the top of the catalyst collection tank.

[0069] In this embodiment, the upper section of the tail gas absorption tower is a packed tower, and the lower section is an absorption liquid storage tank. The circulating absorption liquid is continuously transported by a circulating pump at the bottom of the tower to the absorption liquid cooler for cooling and then returned to the top of the absorption tower for spraying.

[0070] In this embodiment, the ethyl tower 111, the diethyl tower 121 and the triethyl tower 131 all include a distillation section and a stripping section, wherein the distillation section is provided with a product collecting tank, a reflux liquid distributor and fillers, and the stripping section is provided with a feed liquid redistributor, fillers and a tower bottom, and the material is in reverse contact with the reflux liquid and reboiling steam in the tower to achieve mass transfer, heat transfer and component separation.

[0071] In this embodiment, the condenser 112 at the top of the 1-ethylene tower, the condenser 122 at the top of the 2-ethylene tower and the condenser 132 at the top of the 3-ethylene tower are all horizontal shell-and-tube heat exchangers, which are used to remove heat from the tower, condense the vapor at the top of the tower and form reflux liquid in the tower.

[0072] In this embodiment, the 1-ethylene reboiler 113, the 2-ethylene reboiler 123 and the 3-ethylene reboiler 133 are all falling film evaporators, which are used to provide the heat required for distillation to achieve continuous vaporization and separation of materials.

[0073] The present invention also discloses a production process of an alcoholamine product, which is realized by the alcoholamine product production system and comprises the following steps:

[0074] Step 1, metering and continuously feeding ethylene oxide, liquid ammonia and catalyst into premixer 2;

[0075] Step 2: fully mixing the materials in the premixer 2;

[0076] Step 3: continuously feeding the mixed materials into the reactor 3 for reaction. During this process, the hot water circulation device 5 provides the reactor 3 with the required heating or cooling hot water. Meanwhile, the condensate recovery device 6 recovers and reuses the steam condensate.

[0077] Step 4: sending the reacted material into a retention aging device 4 for aging treatment to obtain an alcoholamine raw material;

[0078] Step 5: feeding the alcoholamine raw material into the ammonia distillation device 7, separating ammonia and water by heating, recovering the ammonia gas after condensation, and further removing residual ammonia by flash distillation under reduced pressure;

[0079] Step 6: sending the alcoholamine mixture output from the ammonia evaporation device 7 to the dehydration device 8 to remove water by distillation under vacuum conditions;

[0080] Step 7: Use a vacuum device 9 to maintain the vacuum state of the dehydration device 8, remove the non-condensable gas in the system, and obtain a mixed ethanolamine material;

[0081] Step 8, after the mixed ethanolamine material is subjected to ammonia evaporation and dehydration treatment, it is continuously sent to a monoethanolamine distillation device 11 for distillation to separate the monoethanolamine product;

[0082] Step 9: sending the heavy component material at the bottom of the first ethyl tower to the diethyl distillation device 12 for distillation to separate the diethanolamine product, and at the same time, returning the light component material containing monoethanolamine to the first ethyl tower for further treatment;

[0083] Step 10: sending the heavy component material at the bottom of the diethyl tower to the triethyl distillation device 13 for distillation to separate the triethanolamine product, and at the same time, returning the light component material containing diethanolamine to the diethyl tower for further treatment;

[0084] Step 11. In each distillation unit, forced external circulation heating and reboiling are performed through a high-efficiency falling film evaporator, effective separation and reflux of components are achieved through a product side line discharge and a head-swing device, and a distillation operation under a high vacuum state is achieved through a four-stage high vacuum pump to obtain high-quality monoethanolamine, diethanolamine and triethanolamine products.

[0085] The ammonia evaporation tower 71 of the present invention comprises an ammonia evaporation tower body 711, an ammonia evaporation tower kettle 712 disposed at the bottom of the ammonia evaporation tower body 711 and connected thereto, and an ammonia evaporation tower skirt 713 disposed at the bottom of the ammonia evaporation tower body 711, wherein a sealing head 714 is provided inside the ammonia evaporation tower body 711 and is sealed with the inner wall of the ammonia evaporation tower body 711, wherein the sealing head 714 divides the interior of the tower body from top to bottom into two independent spaces, an ammonia evaporation tower flash section 715 and an ammonia evaporation tower distillation section 716, wherein an ammonia evaporation tower gas phase outlet 717 is provided at the top of the ammonia evaporation tower flash section 715 and is connected thereto, wherein the ammonia evaporation tower The flash section 715 is provided with a first demister 718 and a heater 719 from top to bottom, a vaporization chamber 7110 is formed between the first demister 718 and the heater 719, an ammonia evaporation tower feed port 7111 communicating with the interior of the vaporization chamber 7110 is provided on the outside of the ammonia evaporation tower flash section 715, an upper steam inlet 7112 and an upper condensate outlet 7113 communicating with the heater 719 are provided on the outside of the ammonia evaporation tower flash section 715, and an ammonia evaporation tower upper section bottom outlet 7113 communicating with the interior of the ammonia evaporation tower flash section 715 is provided near the bottom of the ammonia evaporation tower flash section 715. 14, the interior of the distillation section is provided with a second demister 7115 and a plurality of tower plates 7116 in sequence from top to bottom, the plurality of tower plates 7116 are staggered from top to bottom, the end cap 714 is provided with a gas phase outlet 7117 of the lower section of the ammonia evaporation tower which is connected to the interior of the distillation section 716 of the ammonia evaporation tower and extends to the outside of the ammonia evaporation tower body 711, the outside of the distillation section is provided with a material inlet 7118 of the lower section of the ammonia evaporation tower which is connected to the position between the second demister 7115 and the tower plate 7116 located at the top, the bottom outlet 7114 of the upper section of the ammonia evaporation tower is connected to the material outlet 7118 of the lower section of the ammonia evaporation tower The ammonia evaporation tower is connected to the ammonia evaporation tower. The ammonia evaporation tower reboiler return port 7119 is provided near the bottom of the ammonia evaporation tower distillation section 716 and is connected to the interior thereof. The ammonia evaporation tower kettle 712 is provided with an ammonia evaporation tower discharge port 7120 and is connected to the interior thereof at the bottom thereof. The ammonia evaporation tower discharge port 7120 is connected to the ammonia evaporation tower reboiler return port 7119 through a pipeline. The ammonia evaporation tower kettle 712 is provided with an ammonia evaporation tower steam coil 7121 on the outside thereof. The ammonia evaporation tower steam coil 7121 is provided with an ammonia evaporation tower external heating steam inlet 7122 and an ammonia evaporation tower external heating condensed water outlet 7123 connected thereto. An ammonia evaporation tower conical transition section 7124 is provided between the ammonia evaporation tower body 711 and the ammonia evaporation tower kettle 712. The heater 719 is provided with an exhaust port 7125 and a drain port 7126 connected thereto. Each of the tower plates 7116 includes a liquid receiving plate 71161 arranged on the inner wall of the distillation section and a tower plate 71162 connected to the liquid receiving plate 71161, the end of the tower plate 71162 away from the liquid receiving plate 71161 is connected to a water retaining plate 71163, the lower end of the water retaining plate 71163 is connected to an inclined liquid drop plate 71164, and the liquid drop plate 71164 located on the upper layer is inclined toward the liquid receiving plate 71161 located below.The upper surface of the liquid receiving pan 71161 is lower than the upper surface of the tower plate 71162, and the upper surface of the water baffle 71163 is higher than the upper surface of the tower plate 71162. An ammonia evaporation tower feed baffle 7127 is provided at a position corresponding to the material inlet 7118 of the lower section of the ammonia evaporation tower inside the distillation section 716 of the ammonia evaporation tower. An ammonia evaporation tower anti-vortex baffle 7128 is provided at a position on the inner bottom surface of the ammonia evaporation tower kettle 712 outside the ammonia evaporation tower discharge port 7120.

[0086] The ammonia still 71 includes the following components:

[0087] Ammonia evaporation tower body 711: It is the main part of the ammonia evaporation tower, and is provided with a head 714 sealed with the inner wall of the ammonia evaporation tower body 711. The head 714 divides the interior of the ammonia evaporation tower body 711 from top to bottom into two independent spaces: an ammonia evaporation tower flash section 715 and an ammonia evaporation tower distillation section 716.

[0088] Ammonia evaporation tower kettle 712: It is arranged at the bottom of the ammonia evaporation tower body 711 and is connected thereto, and is used to collect the materials after ammonia evaporation.

[0089] Ammonia still tower skirt 713: arranged at the bottom of the ammonia still tower body 711, used to support the entire ammonia still tower structure.

[0090] In the flash section 715 of the ammonia evaporation tower, a gas phase outlet 717 of the ammonia evaporation tower is provided at the top for discharging the gas phase material after ammonia evaporation. The first demister 718 and the heater 719 are provided in sequence from top to bottom in the flash section, and a vaporization chamber 7110 is formed between the first demister 718 and the heater 719 for vaporization treatment of the material. An ammonia evaporation tower feed port 7111 connected to the inside of the vaporization chamber 7110 is provided on the outside of the flash section for adding the material to be evaporated into the ammonia evaporation tower. At the same time, an upper steam inlet 7112 and an upper condensate outlet 7113 connected to the heater 719 are also provided on the outside of the flash section for steam supply and condensate discharge of the heater 719. An upper bottom outlet 7114 of the ammonia evaporation tower connected to the inside of the flash section is provided near the bottom of the flash section for discharging the material after the flash section treatment.

[0091] In the distillation section 716 of the ammonia evaporation tower, a second demister 7115 and several trays 7116 are sequentially arranged from top to bottom inside, and the several trays 7116 are staggered from top to bottom for further ammonia evaporation treatment of the material. The end cap 714 is provided with a gas phase outlet 7117 of the lower section of the ammonia evaporation tower, which is connected to the inside of the distillation section 716 of the ammonia evaporation tower and extends to the outside of the ammonia evaporation tower body 711, for discharging the gas phase material after the distillation section treatment. The outer side of the distillation section is provided with a material inlet 7118 of the lower section of the ammonia evaporation tower, which is connected to the position between the second demister 7115 and the tray 7116 located at the top, for adding materials into the distillation section. The bottom outlet 7114 of the upper section of the ammonia evaporation tower is connected to the material inlet 7118 of the lower section of the ammonia evaporation tower, so as to form continuous treatment of the material. The outer side of the distillation section is provided with an ammonia evaporation tower reboiler return port 7119, which is connected to the inside, near the bottom, for returning part of the material to the distillation section for re-evaporation of ammonia.

[0092] In addition, an ammonia evaporation tower conical transition section 7124 is provided between the ammonia evaporation tower body 711 and the ammonia evaporation tower kettle 712, which is used to connect and transition the two parts of the structure. The heater 719 is provided with an exhaust port 7125 and a drain port 7126 connected thereto, which are used for gas discharge and material drain of the heater 719. Each tower plate 7116 includes a liquid receiving tray 71161 arranged on the inner side wall of the distillation section and a tower plate 71162 connected to the liquid receiving tray 71161. The end of the tower plate 71162 away from the liquid receiving tray 71161 is connected to a water retaining plate 71163, and the lower end of the water retaining plate is connected to an inclined liquid downcomer 71164. The liquid downcomer 71164 located on the upper layer is inclined toward the liquid receiving tray 71161 located below, so as to optimize the flow of materials and the ammonia evaporation effect. The upper surface of the liquid receiving pan 71161 is lower than the upper surface of the tower plate 71162, and the upper surface of the water retaining plate 71163 is higher than the upper surface of the tower plate 71162, so as to further improve the ammonia evaporation efficiency.

[0093] An ammonia evaporation tower feed baffle 7127 is provided at the position corresponding to the material inlet 7118 of the lower section of the ammonia evaporation tower inside the distillation section 716, which is used to reduce the impact force of the material when entering the distillation section to avoid damage to the tower plate 7116. An ammonia evaporation tower anti-vortex baffle 7128 is provided at the position outside the ammonia evaporation tower discharge port 7120 on the inner bottom surface of the ammonia evaporation tower kettle 712, which is used to prevent the material from forming a vortex in the kettle and affecting the ammonia evaporation effect.

[0094] An ammonia evaporation tower steam coil 7121 is provided outside the ammonia evaporation tower kettle 712, which is used to heat the materials in the ammonia evaporation tower to improve the efficiency of ammonia evaporation. An ammonia evaporation tower external heating steam inlet 7122 and an ammonia evaporation tower external heating condensate outlet 7123 are provided on the steam coil, which are used to connect to an external steam source and a condensate discharge system.

[0095] When the ammonia evaporation tower 71 is working, the material from the reactor 3 with a pressure of 5.0 MPa and a temperature of 80°C-100°C flows into the vaporization chamber 7110 of the flash section 715 of the ammonia evaporation tower with a pressure of 0.9-1.6 MPa by gravity, and is rapidly decompressed and flash-vaporized by its own thermal enthalpy and vaporized by the heat supplemented by the upper heater 719. The ammonia output of the flash section 715 of the ammonia evaporation tower accounts for about 85% of the total ammonia content of the material. The first demister 718 is a built-in wire mesh demisting filler, which is used to capture the ethanolamine droplets entrained in the rising ammonia gas. The ammonia gas after demisting enters the gas phase outlet 717 of the ammonia evaporation tower. The heater 719 is a shell-and-tube heat exchanger, and low-pressure steam or hot water is passed between its tubes to timely provide the heat required for the ammonia vaporization of the material in the tube to maintain the material liquid temperature stable between 80°C-95°C. After the material stays in the vaporization chamber 7110 and the heater 719 tube for a period of time, it enters the distillation section 716 of the ammonia evaporation tower.

[0096] The ammonia distillation tower distillation section 716 is provided with a tray 7116. The material flows downstream from the top of the ammonia distillation tower distillation section 716 through the trays 71162 of each tray 7116 in turn, and countercurrently contacts with the rising vapor of the heated material at the bottom; after mass transfer and heat transfer, the light components (ammonia and a small amount of water) contained in it are continuously vaporized and purified, and merge with the ammonia vapor evaporated from the flash distillation section 715 of the ammonia distillation tower and enter the gas phase outlet 717 of the ammonia distillation tower together; the heavy components are enriched in the ammonia distillation tower kettle 712 after stripping, and discharged from the ammonia distillation tower outlet 7120.

[0097] The dehydration tower 81 of the present invention comprises a dehydration tower body 811, a dehydration tower kettle 812 disposed at the bottom of the dehydration tower body 811 and connected thereto, and a dehydration tower skirt 813 disposed at the bottom of the dehydration tower body 811. The dehydration tower body 811 is provided with a fluid distributor 814 sealedly connected to the inner wall of the dehydration tower body 811. The fluid distributor 814 divides the interior of the dehydration tower body 811 from top to bottom into two independent sections: a dehydration tower rectification section 815 and a dehydration tower stripping section 816. The dehydration tower rectifying section 815 is provided with a dehydration tower gas phase outlet 817 connected to the interior thereof at the top thereof, a dehydration tower upper section packing support grid 818 is provided in the dehydration tower rectifying section 815, and a dehydration tower upper section sealing packing is provided on the dehydration tower upper section packing support grid 818, a dehydration tower rectifying section 815 rectifying section 815 outer side wall is provided with a dehydration tower reflux port 819 connected to the interior thereof and opening located above the dehydration tower upper section sealing packing, a dehydration tower rectifying section 815 rectifying section 815 outer side wall is provided with a dehydration tower feed port 8110 connected to the interior thereof and opening located above the fluid distributor 814, a dehydration tower lower section packing support grid 8111 is provided in the dehydration tower stripping section 816 at a position below the fluid distributor 814, a dehydration tower lower section packing support grid 8111 is provided with a dehydration tower lower section sealing packing, a dehydration tower stripping section 816 outer side wall is provided with a dehydration tower lower section sealing packing connected to the interior thereof and outlet located at the dehydration tower lower section sealing packing and the dehydration tower kettle 81 2, a dehydration tower reboiler return port 8112 is provided at the bottom of the dehydration tower kettle 812, and a dehydration tower discharge port 8113 is connected to the inside thereof, and the dehydration tower discharge port 8113 is connected to the dehydration tower reboiler return port 8112 through a pipeline, and a dehydration tower steam coil 8114 is provided on the outside of the dehydration tower kettle 812, and a dehydration tower external heating steam inlet 8115 and a dehydration tower external heating condensed water outlet 8116 are provided on the dehydration tower steam coil 8114. A dehydration tower elliptical head 8117 is provided between the dehydration tower body 811 and the dehydration tower kettle 812. A dehydration tower feed baffle 8118 is provided at a position corresponding to the dehydration tower feed port 8110 on the inner side of the dehydration tower rectification section 815. A dehydration tower anti-vortex baffle 8119 is provided on the inner bottom surface of the dehydration tower kettle 812, which is located outside the dehydration tower discharge port 8113.

[0098] The dehydration tower 81 of the present invention comprises the following components:

[0099] Dehydration tower body 811: It is the main part of the dehydration tower, and a fluid distributor 814 is arranged inside it. The fluid distributor 814 is sealed and connected to the inner wall of the dehydration tower body 811, dividing the interior of the dehydration tower body 811 from top to bottom into two independent cavities: a dehydration tower distillation section 815 and a dehydration tower stripping section 816.

[0100] Dehydration tower kettle 812: It is arranged at the bottom of the dehydration tower body 811 and is connected thereto, and is used to collect the dehydrated materials.

[0101] Dehydration tower skirt 813: arranged at the bottom of the dehydration tower body 811, used to support the entire dehydration tower structure.

[0102] In the rectifying section 815 of the dehydration tower, there is a dehydration tower gas phase outlet 817 for discharging the dehydrated gas phase material. At the same time, the rectifying section is provided with a dehydration tower upper section packing support grid 818 and a dehydration tower upper section sealing packing to improve the dehydration efficiency. The dehydration tower reflux port 819 is arranged on the outer wall of the rectifying section, and the opening is located above the dehydration tower upper section sealing packing, which is used to reflux part of the material to adjust the dehydration process. The dehydration tower feed port 8110 is also arranged on the outer wall of the rectifying section, and the opening is located above the fluid distributor 814, which is used to add the material to be dehydrated into the dehydration tower.

[0103] In the dehydration tower stripping section 816, a dehydration tower lower section packing support grid 8111 and a dehydration tower lower section sealing packing are provided to further improve the dehydration efficiency. The dehydration tower reboiler return port 8112 is provided on the outer side wall of the stripping section, and the outlet is located between the dehydration tower lower section sealing packing and the dehydration tower kettle 812, which is used to return part of the material to the stripping section for re-dehydration.

[0104] In addition, a dehydration tower elliptical head 8117714 is provided between the dehydration tower body 811 and the dehydration tower kettle 812 to connect and seal the two parts. A dehydration tower feed baffle 8118 is provided at the position corresponding to the dehydration tower feed port 8110 on the inner side of the dehydration tower rectification section 815 to reduce the impact force of the material when entering the dehydration tower to avoid damage to the packing. A dehydration tower anti-vortex baffle 8119 is provided on the inner bottom surface of the dehydration tower kettle 812 at the position outside the dehydration tower discharge port 8113 to prevent the material from forming a vortex in the kettle and affecting the dehydration effect.

[0105] A dehydration tower steam coil 8114 is provided outside the dehydration tower kettle 812 to heat the materials in the dehydration tower and improve the dehydration efficiency. The steam coil is provided with a dehydration tower external heating steam inlet 8115 and a dehydration tower external heating condensate outlet 8116 to connect to an external steam source and a condensate discharge system.

[0106] The vacuum device 9 of the present invention is connected to the dehydration device 8 and is used to maintain the vacuum state of the dehydration device 8, and includes a vacuum ejector, a catalyst collection tank, a circulation pump and a circulation liquid cooler. The circulation pump drives the circulation liquid to circulate between the catalyst collection tank, the circulation liquid cooler and the vacuum ejector to remove the non-condensable gas in the system;

[0107] The tail gas absorption device 10 of the present invention is used to receive the exhaust gas generated by each process in the system, absorb the ammonia, EO and water therein through the absorption liquid, and the absorption liquid is recycled and partially transported to the reactor 3 for recycling. The tail gas absorption device 10 includes a tail gas absorption tower, a tower bottom circulation pump and a circulating liquid cooler;

[0108] The one ethyl tower 111, the two ethyl tower 121 and the three ethyl tower 131 described in the present invention are all refining towers, which include a refining tower body 1311, a refining tower kettle 1312 arranged at the bottom of the refining tower body 1311 and connected thereto, and a refining tower skirt 1313 arranged at the bottom of the refining tower body 1311, a tower top internal condenser 1314 is arranged at the top of the refining tower distillation section 1316, a refining tower feed port 1315 connected thereto is arranged at the middle of the outer side of the refining tower body 1311, and a refining tower distillation section 1316 is formed above the refining tower feed port 1315. A refining tower stripping section 1317 is formed below 1315, the air inlet of the condenser 1314 in the tower top is connected to the refining tower distillation section 1316, and the interior of the refining tower distillation section 1316 is provided with a tower product collecting tank 1318, a refining tower reflux liquid distributor 1319 and a refining tower upper section packing support grid 13110 from top to bottom, and the outer side of the refining tower distillation section 1316 is provided with a first refining tower product discharge port 13111 connected to the tower product collecting tank 1318, the upper part of the tower product collecting tank 1318 is connected to the refining tower reflux liquid distributor 1319, and the refining tower The upper section packing support grid 13110 is provided with a refining tower upper section sealing packing, and the outer side of the refining tower distillation section 1316 is provided with a second refining tower product discharge port 13112 and a refining tower reflux port 13113 connected to the refining tower distillation section 1316 at a position corresponding to the upper section sealing packing of the refining tower, and the interior of the refining tower stripping section 1317 is provided with a liquid distributor 13114 and a refining tower lower section packing support grid 13115 from top to bottom, and the refining tower lower section sealing packing is provided on the refining tower lower section packing support grid 13115, and the outer side of the refining tower stripping section 1317 The wall is provided with a refining tower reboiler return port 13116 which is connected to the interior thereof and the outlet is located between the sealing packing of the lower section of the refining tower and the refining tower kettle 1312. The bottom of the refining tower kettle 1312 is provided with a refining tower discharge port 13117 which is connected to the interior thereof. The refining tower discharge port 13117 is connected to the refining tower reboiler return port 13116 through a pipeline. The outside of the refining tower kettle 1312 is provided with a refining tower steam coil 13118, and the refining tower steam coil 13118 is provided with a refining tower external heating steam inlet 13119 and a refining tower external heating condensed water outlet 13120 which are connected to the refining tower. A first refining tower feed baffle 13121 is provided at a position corresponding to the refining tower feed port 1315 on the inner side of the refining tower body 1311. The product collecting tank 1318 in the tower is connected to the inner wall of the refining tower rectifying section 1316 through a cone shell 13122. The refining tower reflux liquid distributor 1319 is connected to the product collecting tank 1318 in the tower through the distributor connecting pipe 13123. A crossbeam 13124 is provided on the inner wall of the refining tower rectifying section 1316, and the distributor connecting pipe 13123 passes through the crossbeam 13124 and is connected to the crossbeam 13124.A second refining tower feed baffle 13125 is provided at a position corresponding to the refining tower reflux port 13113 on the inner side of the refining tower rectifying section 1316. A refining tower anti-vortex baffle 13126 is provided at a position outside the refining tower discharge port 13117 on the inner bottom surface of the refining tower kettle 1312.

[0109] The refining tower of the present invention comprises the following components:

[0110] Refining tower body 1311: It is the main part of the refining tower, and a tower top condenser 1314 is provided on the top of the tower to condense the refined gas phase material.

[0111] Refining tower kettle 1312: arranged at the bottom of the refining tower body 1311 and connected thereto, and used for collecting the refined materials.

[0112] Refining tower skirt 1313: arranged at the bottom of the refining tower body 1311, used to support the entire refining tower structure.

[0113] A refining tower feed port 1315 connected to the interior of the refining tower body 1311 is provided at the middle of the outer side thereof for feeding the material to be refined into the refining tower. A refining tower rectifying section 1316 is formed above the refining tower feed port 1315, and a refining tower stripping section 1317 is formed below the refining tower feed port 1315. The air inlet of the condenser 1314 in the tower top is connected to the refining tower rectifying section 1316 for receiving and condensing the refined gaseous material.

[0114] Inside the refining tower rectifying section 1316, there are arranged from top to bottom a tower product collecting tank 1318, a refining tower reflux liquid distributor 1319 and a refining tower upper section packing support grid 13110. The tower product collecting tank 1318 is used to collect the refined products and discharge them through the first refining tower product discharge port 13111. The upper part of the tower product collecting tank 1318 is connected to the refining tower reflux liquid distributor 1319, which is used to reflux part of the products into the refining tower to regulate the refining process. The refining tower upper section packing support grid 13110 is provided with a refining tower upper section sealing packing to improve the refining efficiency. The second refining tower product discharge port 13112 and the refining tower reflux port 13113 are provided on the outer side of the refining tower rectifying section 1316 at a position corresponding to the refining tower upper section sealing packing, which are used to discharge the refined products and the reflux materials respectively.

[0115] Inside the refining tower stripping section 1317, a liquid distributor 13114 and a refining tower lower section packing support grid 13115 are arranged from top to bottom. A refining tower lower section sealing packing is arranged on the refining tower lower section packing support grid 13115 to further improve the refining efficiency. A refining tower reboiler return port 13116 is arranged on the outer side wall of the refining tower stripping section 1317, which is connected to the inside thereof and the outlet is located between the refining tower lower section sealing packing and the refining tower kettle 1312, for returning part of the material to the stripping section for further refining.

[0116] In addition, a first refining tower feed baffle 13121 is provided at a position corresponding to the refining tower feed port 1315 on the inner side of the refining tower body 1311, which is used to reduce the impact force of the material when entering the refining tower to avoid damage to the packing. The product collection tank 1318 in the tower is connected to the inner wall of the refining tower distillation section 1316 through the cone shell 13122 to improve the stability and sealing of the connection. The refining tower reflux liquid distributor 1319 is connected to the product collection tank 1318 in the tower through the distributor connecting pipe 13123, and the distributor connecting pipe 13123 passes through the crossbeam 13124 on the inner wall of the refining tower distillation section 1316 and is connected to the crossbeam 13124 to fix the distributor and optimize the material reflux path. A second refining tower feed baffle 13125 is provided at a position corresponding to the refining tower reflux port 13113 on the inner side of the refining tower distillation section 1316 to further reduce the impact force of the reflux material.

[0117] A refining tower steam coil 13118 is provided on the outside of the refining tower kettle 1312, which is used to heat the materials in the refining tower to improve the refining efficiency. The steam coil is provided with a refining tower external heating steam inlet 13119 and a refining tower external heating condensate outlet 13120, which are used to connect the external steam source and the condensate discharge system. A refining tower anti-vortex baffle 13126 is provided on the inner bottom surface of the refining tower kettle 1312, located outside the refining tower discharge port 13117, to prevent the materials from forming vortices in the kettle and affecting the refining effect.

[0118] The above-mentioned embodiments only express the specific implementation of the present invention, and the description thereof is relatively specific and detailed, but it cannot be understood as limiting the scope of the present invention. It should be pointed out that, for ordinary technicians in this field, several variations and improvements can be made without departing from the concept of the present invention, which all belong to the protection scope of the present invention.

Claims

1. An olamine product production system, characterized in that: include: Raw material metering and feeding device, used for metering and continuous feeding of ethylene oxide, liquid ammonia and catalyst; A premixer, used for fully mixing the ethylene oxide, liquid ammonia and catalyst in the axial and radial directions; The reactor is a tubular reactor, which is divided into several reaction sections, each of which is connected to a corresponding pre-mixer outlet for continuous reaction; A retention aging device is connected to the outlet of one of the reaction sections of the reactor to ensure that the ethylene oxide in the reaction material reacts completely; A hot water circulation device, used to provide the reactor with hot water required for heating or cooling; Condensate recovery device, used to recover and reuse steam condensate; an ammonia distillation device, receiving the pretreated alcoholamine raw material, and separating ammonia and water in the alcoholamine raw material in a gaseous form by heating, wherein the ammonia distillation device comprises an ammonia distillation tower, an ammonia distillation tower reboiler, an ammonia distillation tower condenser and an ammonia flash tank, wherein the ammonia distillation tower is divided into an ammonia distillation flash section and an ammonia distillation section, wherein the ammonia distillation flash section is used for preliminary separation of ammonia gas, and the ammonia distillation section is used for further separation of ammonia and water, wherein the ammonia distillation tower reboiler provides heat to maintain vaporization of materials in the ammonia distillation section, wherein the ammonia distillation tower condenser is used for condensing the separated ammonia gas, and the ammonia flash tank is used for further removing residual ammonia in the materials under reduced pressure conditions; The dehydration device receives the alcoholamine mixture output from the ammonia distillation device and removes the water therein by vacuum distillation; A vacuum device, connected to the dehydration device, used to maintain a vacuum state of the dehydration device; The tail gas absorption device receives the exhaust gas generated by each process in the system, absorbs the ammonia, EO and water therein through the absorption liquid, and the absorption liquid is recycled and partly transported to the reactor for recycling; An ethylene distillation device is used to separate the ethylene product from the mixed ethanolamine, including an ethylene feed flash tank, an ethylene tower, an ethylene tower top internal condenser, an ethylene reboiler, an ethylene tower bottom circulation pump, an ethylene product pump and an ethylene product cooler, and a matching ethylene vacuum unit; The diethyl distillation device is used to receive the heavy component materials from the bottom of the first ethyl tower and separate the diethanolamine product, including the diethyl tower, the condenser in the top of the diethyl tower, the diethyl reboiler, the diethyl tower bottom circulation pump, the diethyl product extraction pump and the diethyl product cooler, and the supporting diethyl vacuum unit, wherein a light component distillation layer is added to the upper part of the diethyl tower distillation section to further improve the quality of the diethanolamine product; The triethyl distillation device is used to receive the heavy component materials from the diethyl tower kettle and separate the triethanolamine product, including the triethyl tower, the condenser inside the triethyl tower top, the triethyl reboiler, the triethyl tower bottom circulation pump, the triethyl product pump and the triethyl product cooler, and the supporting triethyl vacuum unit; The 1-ethyl distillation unit, the 2-ethyl distillation unit and the 3-ethyl distillation unit all adopt high-efficiency falling film evaporators for forced external circulation heating and reboiling. Each tower is equipped with a product side line discharge and head shaking device to achieve effective separation and reflux of components. At the same time, each vacuum unit contains a four-stage high vacuum pump to achieve distillation operation under high vacuum conditions.

2. The alcoholamine product production system according to claim 1, characterized in that: The ammonia evaporation tower flash section of the ammonia evaporation tower is provided with a first demister, a vaporization chamber and a heater. The heater is a shell-and-tube heat exchanger, and low-pressure steam or hot water is passed between the tubes.

3. The alcoholamine product production system according to claim 1, characterized in that: The dehydration tower rectification section and the dehydration tower stripping section of the dehydration tower are provided with regular corrugated fillers, a fluid distributor and a liquid redistributor.

4. The alcoholamine product production system according to claim 1, characterized in that: The vacuum ejector has an air extraction port connected to the vacuum pipe port of the reflux tank, a liquid inlet connected to the outlet of the circulation pump, and an ejection port installed on the top of the catalyst collecting tank.

5. The alcoholamine product production system according to claim 1, characterized in that: The upper section of the tail gas absorption tower is a packed tower, and the lower section is an absorption liquid storage tank. The circulating absorption liquid is continuously transported to the absorption liquid cooler by a circulating pump at the bottom of the tower for cooling and then returned to the top of the absorption tower for spraying.

6. The alcoholamine product production system according to claim 1, characterized in that: The one ethyl tower, the two ethyl tower and the three ethyl tower all include a distillation section and a stripping section, wherein the distillation section is provided with a product collecting tank, a reflux liquid distributor and fillers, and the stripping section is provided with a feed liquid redistributor, fillers and a tower bottom. The material is in reverse contact with the reflux liquid and the reboiling steam in the tower to achieve mass transfer, heat transfer and component separation.

7. The alcoholamine product production system according to claim 1, characterized in that: The condenser at the top of the 1 ethylene tower, the condenser at the top of the 2 ethylene tower and the condenser at the top of the 3 ethylene tower are all horizontal shell and tube heat exchangers, which are used to remove heat from the tower, condense the vapor at the top of the tower and form reflux liquid in the tower.

8. The alcoholamine product production system according to claim 1, characterized in that: The one ethylene reboiler, the two ethylene reboilers and the three ethylene reboilers are all falling film evaporators, which are used to provide the heat required for distillation to achieve continuous vaporization and separation of materials.

9. A process for producing an alcoholamine product, characterized in that: The method is realized by the ethanolamine product production system according to any one of claims 1 to 8, comprising the following steps: Step 1, metering and continuously feeding ethylene oxide, liquid ammonia and catalyst into a premixer; Step 2: fully mixing the materials in a premixer; Step 3, continuously feeding the mixed materials into a reactor for reaction; Step 4: sending the reacted material into a retention aging device for aging treatment, providing the required heating or cooling hot water for the reactor through a hot water circulation device, recovering and reusing steam condensate, and obtaining an alcoholamine raw material; Step 5: feeding the alcohol amine raw material into an ammonia distillation device, separating ammonia and water by heating, recovering the ammonia gas after condensation, and further removing residual ammonia by flash distillation under reduced pressure; Step 6: sending the alcoholamine mixture output from the ammonia distillation device to a dehydration device to remove water by distillation under vacuum conditions; Step 7: Use a vacuum device to maintain the vacuum state of the dehydration device, remove the non-condensable gas in the system, and obtain a mixed ethanolamine material; Step 8, after the mixed ethanolamine material is subjected to ammonia evaporation and dehydration treatment, it is continuously sent to a monoethanolamine distillation device for distillation to separate the monoethanolamine product; Step 9, sending the heavy component materials in the bottom of the first ethyl tower to the diethyl distillation device for distillation to separate the diethanolamine product, and at the same time, returning the light component materials containing monoethanolamine to the first ethyl tower for reprocessing; Step 10, sending the heavy component materials in the diethyl tower kettle to a triethyl distillation device for distillation to separate the triethanolamine product, and at the same time, returning the light component materials containing diethanolamine to the diethyl tower for further treatment; Step 11. In each distillation unit, forced external circulation heating and reboiling are performed through a high-efficiency falling film evaporator, effective separation and reflux of components are achieved through a product side line discharge and a head-swing device, and a distillation operation under a high vacuum state is achieved through a four-stage high vacuum pump to obtain high-quality monoethanolamine, diethanolamine and triethanolamine products.

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