CN218307844U - Continuous hydro-ammoniation preparation device for amine-terminated polyether - Google Patents
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- CN218307844U CN218307844U CN202222195358.7U CN202222195358U CN218307844U CN 218307844 U CN218307844 U CN 218307844U CN 202222195358 U CN202222195358 U CN 202222195358U CN 218307844 U CN218307844 U CN 218307844U
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Abstract
The application discloses a continuous-method hydroamination preparation device of amine-terminated polyether, which comprises a reaction tower, a membrane separator, a high-pressure separator, a water-ammonia separation tower, a liquid ammonia tank and a polyether tank; the reaction tower is internally provided with a reaction section with at least two reaction beds and a separation section with at least two layers of tower trays, and the polyether tank is communicated with the feeding branch pipe of each reaction bed; the liquid ammonia tank is communicated with a gas-phase material inlet of the reaction tower; a discharge hole at the top of the reaction tower is communicated with a feed inlet of the high-pressure separator; the liquid phase outlet of the high-pressure separator is communicated with the material inlet of the membrane separator, the concentrated solution outlet of the membrane separator is communicated with the reflux port of the reaction tower, and the permeate outlet of the membrane separator is communicated with the liquid inlet of the water-ammonia separation tower. By utilizing the method, the production of the amino-terminated polyether can be completed by adopting a single reaction tower, the effect of 4-6 fixed bed reactors or tubular reactors in the prior art can be achieved, and the equipment acquisition cost is saved because the number of the reactors is reduced and the corresponding separation system is cancelled.
Description
Technical Field
The utility model relates to a continuous process hydroamination preparation device of end amino polyether.
Background
The mature production method of the amine-terminated polyether is to perform catalytic ammoniation under the action of a metal catalyst, and at present, two production processes, namely a continuous method and a batch method, are available. Although the batch production process has simple production equipment and small process difficulty, a large amount of time and manpower are consumed for auxiliary operations such as loading and unloading, so that the cost of the product is too high, the product cannot be popularized on a large scale, and the activity of the catalyst is reduced after the catalyst is repeatedly utilized, thereby affecting the stability of the product.
The continuous method adopts a fixed bed type reactor, can continuously feed and discharge materials, can randomly adjust the proportion of liquid ammonia to polyether, has the advantages of keeping the high proportion of liquid ammonia to polyether and improving the reaction efficiency, but has complex production equipment and high requirements on process conditions. In addition, the catalyst of the polyether amine is very sensitive to the generation of water in the production process, and if the generated moisture is too much in the reaction process, the activity of the catalyst can be rapidly reduced.
SUMMERY OF THE UTILITY MODEL
In order to solve the problems, the utility model provides a continuous hydroammonation preparation device of amine-terminated polyether, which comprises a reaction tower, a membrane separator, a high-pressure separator, a water-ammonia separation tower, a liquid ammonia tank and a polyether tank; the reaction tower comprises a tower body extending along the vertical direction, wherein a reaction section and a separation section positioned above the reaction section are arranged in the tower body, at least two reaction beds are arranged in the reaction section, supported metal catalysts are filled in the reaction beds, and a feeding branch pipe is arranged above each reaction bed; at least two layers of tower trays are arranged in the separation section; the lower part of the reaction section is formed into an air inlet cavity, and a gas-phase material inlet communicated with the air inlet cavity is arranged on the tower body;
the discharge port of the polyether tank is communicated with the inlet of a raw material pump, the outlet of the raw material pump is connected with a feeding main pipe, and the feeding main pipe is communicated with each feeding branch pipe after sequentially passing through a refrigerant channel of a first heater, a refrigerant channel of a second heater and a first heating furnace;
the discharge port of the liquid ammonia tank is communicated with the inlet of an ammonia pump, the outlet of the ammonia pump is communicated with the inlet of an ammonia gasifier, and the outlet of the ammonia gasifier is communicated with the gas-phase material inlet of the reaction tower after sequentially passing through a refrigerant channel of a third heater, a refrigerant channel of a fourth heater and a second heating furnace;
a discharge hole at the top of the tower of the reaction tower is connected with a discharge pipe at the top of the tower, and the discharge pipe at the top of the tower is communicated with a feed inlet of the high-pressure separator after sequentially passing through a heating medium channel of the second heater, a heating medium channel of the first heater, a water cooler and a pressure regulating valve; a tower bottom discharge pipe is connected to a tower bottom discharge hole of the reaction tower, and the tower bottom discharge pipe is communicated with a finished product tank after sequentially passing through a heat medium channel of a fourth heater, a heat medium channel of a third heater and a finished product cooler;
a gas phase outlet at the top of the high-pressure separator is connected with a hydrogen return pipe, the hydrogen return pipe is communicated with an air inlet of a hydrogen compressor, an outlet of the hydrogen compressor is communicated with an inlet of a refrigerant channel of the third heat exchanger, and a hydrogen storage device is communicated with the hydrogen return pipe; the liquid phase outlet at the bottom of the high-pressure separator is communicated with the material inlet of the membrane separator, the concentrated solution outlet of the membrane separator is communicated with the reflux port at the top of the reaction tower, the reflux port is positioned above the separation section, the permeate outlet of the membrane separator is communicated with the liquid inlet of the aqueous ammonia separation tower, the exhaust port at the top of the aqueous ammonia separation tower is communicated with the air inlet of the ammonia compressor, and the outlet of the ammonia compressor is communicated with the inlet of the refrigerant channel of the third heat exchanger.
When the amino-terminated polyether is produced, the method comprises the following steps:
(1) Under the drive of a raw material pump, polyether in the polyether tank is heated to a set temperature after sequentially passing through a refrigerant channel of the first heat exchanger, a refrigerant channel of the second heat exchanger and the first heating furnace, then enters each reaction bed layer through each feeding branch pipe, and flows downwards along the reaction bed layers.
Liquid ammonia in the liquid ammonia tank is sent into ammonia vaporizer through the ammonia pump and is gasified in, forms the ammonia, then mixes with hydrogen and forms into the mixture, and after the mixture heated to the settlement temperature through third heat exchanger, fourth heat exchanger and second heating furnace in proper order, the formation is the mist of ammonia and hydrogen, and mist enters into the air inlet chamber to the upflow.
The mixed gas flowing upwards contacts with polyether flowing downwards, and is hydroammonation reacted under the action of supported metal catalyst. The gas-phase material discharged from the uppermost reaction bed layer passes through the trays of each layer step by step and is discharged from the top of the reaction tower.
And discharging the liquid phase material in the reaction tower from the bottom of the reaction tower, and cooling the liquid phase material to normal temperature through a heat medium channel of the fourth heat exchanger, a heat medium channel of the third heat exchanger and a finished product cooler in sequence to obtain the amino-terminated polyether product.
(2) And the gas-phase material is cooled by a heat medium channel of the second heat exchanger, a heat medium channel of the first heat exchanger and a water cooler in sequence, is decompressed by a pressure regulating valve, enters a high-pressure separator for separation, is discharged from the top of the high-pressure separator, is mixed with fresh hydrogen supplied by a hydrogen storage device, is compressed by a hydrogen compressor, and is returned to the reaction tower through a refrigerant channel of a third heater, so that the crude hydrogen is recycled.
(3) And the separation liquid discharged from the liquid phase outlet of the high-pressure separator enters a membrane separator for separation.
The concentrated solution discharged from the membrane separator returns to the reaction tower from the upper side of the tray at the uppermost layer, flows downwards along each layer of trays step by step, and absorbs the liquid drops contained in the upwards flowing gas in the downward flowing process, wherein the liquid drops are mainly polyether and amine-terminated polyether. The permeate discharged from the membrane separator enters a water-ammonia separation tower.
And gas discharged from the top of the water-ammonia separation tower is compressed by an ammonia compressor through crude ammonia and then returns to the reaction tower through a refrigerant channel of the third heater for cyclic utilization.
In the application, besides the reaction section, a separation section which mainly comprises a tower tray is also arranged in the reaction tower and is combined with a high-pressure separator and a membrane separator, the end amino polyether can be effectively separated from ammonia and hydrogen, particularly water, the reaction efficiency is improved while the reaction depth is ensured, the separation energy consumption is reduced, and the operation cost is saved.
Because the reaction section and the separation section are arranged, and the reaction section is provided with at least two reaction beds, the height of a single reaction bed is reduced, the pressure drop in the single reaction bed is reduced, a plurality of reaction beds can redistribute materials, the uniformity of the materials entering the next reaction bed is improved, the materials are in full contact with a catalyst, and the reaction efficiency is improved. Polyether is fed in a segmented mode, and the ratio of ammonia to polyether and the ratio of hydrogen to polyether in each reaction bed layer are improved.
In the application, in the reaction tower, from top to bottom, the concentration of polyether is lower and lower, and the concentration of ammonia and hydrogen is higher and higher, so that the proportion of ammonia and polyether is higher and higher, the forward proceeding of the hydroamination reaction is promoted, and the reaction efficiency is improved. In the application, the production of the amino-terminated polyether can be completed by adopting a single reaction tower, the effect of 4-6 fixed bed reactors or tubular reactors in the prior art can be achieved, and the number of reactors is reduced, so that a corresponding separation system is also cancelled, and the equipment acquisition cost is saved. In the application, a high-pressure separator and a membrane separator are used for condensing and separating gas-phase materials discharged from the top of a reaction tower, the obtained concentrated solution is returned to the reaction tower, and the concentrated solution mainly comprises a mixture of unreacted polyether and amine-terminated polyether.
By utilizing the method, the amino-terminated polyether can be produced by adopting a single reaction tower, and the produced amino-terminated polyether can be directly used as a commodity without refining.
Specifically, in order to ensure the smooth proceeding of the reaction, make the material discharged from the uppermost layer of reaction bed layer reflux as much as possible and improve the reaction efficiency, 4-6 reaction bed layers are arranged in the reaction section, each reaction bed layer is filled with a supported metal catalyst with the same height, and 10-20 layers of tower trays are arranged in the separation section.
Furthermore, in order to improve the distribution uniformity of polyether in the reaction bed layers, a liquid distributor is arranged above each reaction bed layer corresponding to each feeding branch pipe, and the feeding branch pipes are communicated with the corresponding liquid distributors.
Furthermore, in order to improve the distribution uniformity of the hydrogen and the ammonia in the reactor, a gas distributor is arranged in the gas inlet cavity, and the gas-phase material inlet is communicated with the gas distributor.
Further, for improving the separation purity of ammonia, the water-ammonia separation tower is a tray tower, and is provided with an upper tray set and a lower tray set in the water-ammonia separation tower, wherein the upper tray set is located above the lower tray set, and in the height direction, the liquid inlet of the water-ammonia separation tower is located between the upper tray set and the lower tray set. Specifically, the upper tray group comprises 10-20 layers of upper trays, and the lower tray group comprises 10-20 layers of lower trays.
Furthermore, a reflux tank is arranged at the top of the water-ammonia separation tower, an exhaust port at the top of the water-ammonia separation tower is communicated with the reflux tank after passing through a condenser, the bottom of the reflux tank is communicated with the top of the water-ammonia separation tower through a reflux pipe, and an air outlet at the top of the reflux tank is communicated with an air inlet of an ammonia compressor;
the bottom of the water-ammonia separation tower is provided with a reboiler, two liquid outlet pipes are led out from the tower bottom of the water-ammonia separation tower, one liquid outlet pipe is communicated with a liquid inlet of the reboiler, the other liquid outlet pipe is used as a sewage discharge pipe, and a liquid outlet of the reboiler is communicated with the tower bottom of the water-ammonia separation tower.
The design can reduce the purity of the recovered ammonia gas and reduce the ammonia content in the discharged sewage.
Drawings
Fig. 1 is a schematic flow chart of an embodiment of the present invention.
Fig. 2 is a schematic structural view of the liquid distributor.
Fig. 3 is a schematic diagram of the structure of the gas distributor.
Detailed Description
A continuous hydroammonation preparation device of amine-terminated polyether comprises a reaction tower 10, a membrane separator 31, a high-pressure separator 32, a water-ammonia separation tower 40, a polyether tank 51 and a liquid ammonia tank 61.
The reaction tower 10 comprises a tower body 19 extending along the vertical direction, a reaction section 12 and a separation section 14 positioned above the reaction section 12 are arranged in the tower body, five reaction beds 121 are arranged in the reaction section, and each reaction bed 121 is filled with a supported metal catalyst with the same height.
A liquid distributor 13 is disposed above each reaction bed 121, referring to fig. 2, the liquid distributor 13 is a tubular distributor, the liquid distributor 13 includes a horizontally disposed main feed pipe 131 and an auxiliary feed pipe 132 horizontally disposed at two sides of the main feed pipe, wherein one end of the main feed pipe extends out of the tower body 19 to form a feed port 133, the main feed pipe and the auxiliary feed pipe are supported on the inner wall of the tower body, and each feed port 133 is connected with a feed branch pipe 181. In order to improve the dispersion uniformity of polyether, atomizing nozzles are installed on the lower sides of the main feed pipe 131 and the auxiliary feed pipe 132. Each liquid distributor is connected with a feeding branch pipe.
18 layers of trays 141 are arranged in the separation section 14, and the trays adopt float valve trays; the lower part of the reaction section is formed into an air inlet chamber 11, and an air distributor 111 is installed in the air inlet chamber, referring to fig. 3, the air distributor 111 specifically includes a main air inlet pipe 112 horizontally arranged and an auxiliary air inlet pipe 113 horizontally arranged at two sides of the main air inlet pipe, one end of the main air inlet pipe extends out of the tower body to form a gas phase material inlet 114, and the main air inlet pipe 112 and the auxiliary air inlet pipe 113 are both supported on the inner wall of the tower body. Air intake holes are opened at the lower sides of the main intake pipe 112 and the sub intake pipe 113. Namely, a gas-phase material inlet communicated with the air inlet cavity is arranged on the tower body.
The discharge port of the polyether tank 51 is communicated with the inlet of the raw material pump 52, the outlet of the raw material pump 52 is connected with the feeding main pipe 18, and the feeding main pipe is communicated with the feeding branch pipes 181 after sequentially passing through the refrigerant channel of the first heater 15, the refrigerant channel of the second heater 16 and the first heating furnace 17.
The discharge port of the liquid ammonia tank 61 is communicated with the inlet of the ammonia pump 62, the outlet of the ammonia pump 62 is communicated with the inlet of the ammonia vaporizer 63, and the outlet of the ammonia vaporizer 63 is communicated with the gas-phase material inlet 114 of the reaction tower 10 after sequentially passing through the refrigerant channel of the third heater 21, the refrigerant channel of the fourth heater 22 and the second heating furnace 23.
The top discharge port 191 of the reaction column 10 is connected to a top discharge pipe 193, and the top discharge pipe 193 is connected to the feed port of the high-pressure separator 32 through a heat medium passage of the second heater 16, a heat medium passage of the first heater 15, the water cooler 151, and the pressure regulating valve 35 in this order. The bottom outlet 192 of the reaction column 10 is connected to a bottom outlet pipe 194, which is connected to the product tank via the heat medium channel of the fourth heater 22, the heat medium channel of the third heater 21 and the product cooler 25 in this order, i.e. the bottom outlet pipe 194 serves as a product outlet pipe. In the drawings, the finished can is not shown.
The high pressure separator 32 is a vertical gas-liquid separator, and the feed inlet is arranged in the middle of the high pressure separator. The gas phase outlet 321 at the top of the high-pressure separator 32 is connected with a hydrogen return pipe 36, the hydrogen return pipe 36 is communicated with the gas inlet of the hydrogen compressor 33, the outlet of the hydrogen compressor 33 is communicated with the inlet of the refrigerant channel of the third heat exchanger 21, the hydrogen storage device 130 is communicated with the hydrogen return pipe, the hydrogen storage device 130 is used for supplementing hydrogen, and the hydrogen storage device can be a hydrogen pipe network or a hydrogen storage tank which is specifically adopted in the application.
A liquid phase outlet 322 at the bottom of the high-pressure separator 32 is communicated with a material inlet of the membrane separator 31, a concentrated solution outlet 311 of the membrane separator 31 is communicated with a reflux port 196 at the top of the reaction tower, the reflux port 196 is positioned above the separation section 14, a permeate outlet 312 of the membrane separator 31 is communicated with a liquid inlet 41 of the water-ammonia separation tower 40, a tower top exhaust port 46 of the water-ammonia separation tower is communicated with a reflux tank 43 through a condenser 432, the bottom of the reflux tank 43 is communicated with the top of the water-ammonia separation tower through a reflux pipe 433, and a gas outlet at the top of the reflux tank is communicated with a gas inlet of an ammonia compressor 34; i.e. the top gas outlet 46 of the water-ammonia separation tower is communicated with the gas inlet of the ammonia compressor. The reflux drum 43 is provided at the top of the water-ammonia separation column. The outlet of the ammonia compressor 34 is communicated with the inlet of the refrigerant channel of the third heat exchanger.
In this embodiment, the water-ammonia separating tower 40 is a tray tower, and the water-ammonia separating tower is provided with an upper tray set 44 and a lower tray set 45, wherein the upper tray set is located above the lower tray set, and the liquid inlet 41 of the water-ammonia separating tower is located between the upper tray set and the lower tray set in the height direction. The upper tray set includes 15 layers of upper trays and the lower tray set includes 18 layers of lower trays. The upper tray and the lower tray are both float valve trays.
The bottom of the water-ammonia separation tower 40 is provided with a reboiler 42, two liquid outlet pipes are led out from the tower bottom of the water-ammonia separation tower, the two liquid outlet pipes are respectively a first liquid outlet pipe 421 and a second liquid outlet pipe 422, wherein the first liquid outlet pipe 421 is communicated with a liquid inlet of the reboiler, the second liquid outlet pipe 422 is used as a sewage discharge pipe, and a liquid outlet of the reboiler is communicated with the tower bottom of the water-ammonia separation tower through a reboiling pipe 423.
The procedure used in this example to produce the amino-terminated polyether is described below:
(1) Under the drive of the raw material pump 52, the polyether in the polyether tank 51 is heated to 200 ℃ through the refrigerant channel of the first heat exchanger 15, the refrigerant channel of the second heat exchanger 16 and the first heating furnace 17 in sequence, enters each liquid distributor 13 through the feeding main pipe 18 and each feeding branch pipe 181, is sprayed downwards onto the corresponding reaction bed layer 121 through each liquid distributor 13, and flows downwards along the reaction bed layer.
Liquid ammonia in the liquid ammonia tank 61 is sent into an ammonia vaporizer 63 through an ammonia pump 62 to be vaporized to form ammonia gas, then the ammonia gas is mixed with hydrogen gas to form a mixture, the mixture is heated to 200 ℃ through a third heat exchanger 21, a fourth heat exchanger 22 and a second heating furnace 23 in sequence to form mixed gas of the ammonia gas and the hydrogen gas, and the mixed gas enters a gas distributor 111 through a gas-phase material inlet 114 and then enters a gas inlet cavity and flows upwards.
The mixed gas flowing upwards contacts with polyether flowing downwards, and is hydroammonation reacted under the action of supported metal catalyst. The gas-phase material discharged from the uppermost reaction bed layer passes through each layer of tower tray step by step and is discharged from a tower top discharge port 191 at the top of the reaction tower.
And discharging the liquid phase material in the reaction tower from a discharge hole 192 at the bottom of the reaction tower, and cooling the liquid phase material to the normal temperature through a heat medium channel of the fourth heat exchanger 22, a heat medium channel of the third heat exchanger 21 and the finished product cooler 25 in sequence to obtain the amino-terminated polyether product 150.
(2) The gas phase material sequentially passes through a heat medium channel of the second heat exchanger 16, a heat medium channel of the first heat exchanger 15 and a water cooler 151, is cooled to 40 ℃, is decompressed to 4MPa through a pressure regulating valve 35, enters the high-pressure separator 32 for separation, discharges crude hydrogen from a gas phase outlet 321 at the top of the high-pressure separator 32, is mixed with fresh hydrogen supplied by a hydrogen storage tank, is compressed through a hydrogen compressor 33, and returns to the reaction tower through a refrigerant channel of the third heater 21, so that the crude hydrogen is recycled.
(3) The separation liquid discharged from the liquid phase outlet 322 of the high-pressure separator 32 enters a membrane separator 31 for separation, the separation membrane adopts a BR20-35 nanofiltration membrane of Delnameer, USA, the throttling molecular weight of the nanofiltration membrane is 200 daltons, and the operating pressure difference is 1.0MPa.
The concentrated solution discharged from the membrane separator 31 returns to the reaction tower from the upper side of the tray at the uppermost layer, and flows downwards along each tray step by step, and absorbs the liquid drops contained in the upwards flowing gas in the downward flowing process, wherein the liquid drops are mainly polyether and amine terminated polyether. The permeate discharged from the membrane separator 31 enters the aqueous ammonia separation column 40.
Gas discharged from the top of the aqueous ammonia separation tower 40 enters the reflux tank 43 after being cooled by the condenser 432, liquid in the reflux tank returns to the aqueous ammonia separation tower 40, and crude ammonia discharged from the top of the reflux tank is compressed by the ammonia compressor 34 and then returns to the reaction tower through a refrigerant channel of the third heater 21 for recycling.
The bottoms portion of the water-ammonia separation column 40 is discharged as wastewater 140 through a second effluent pipe 422 into a wastewater treatment system.
Part of the bottom liquid enters the reboiler 42 through the first liquid outlet pipe 421 for heating, and then returns to the bottom of the water-ammonia separation tower through the reboiling pipe 423.
Claims (7)
1. The continuous hydroammonation preparation device for the amine-terminated polyether is characterized by comprising a reaction tower, a membrane separator, a high-pressure separator, a water-ammonia separation tower, a liquid ammonia tank and a polyether tank; the reaction tower comprises a tower body extending along the vertical direction, wherein a reaction section and a separation section positioned above the reaction section are arranged in the tower body, at least two reaction beds are arranged in the reaction section, supported metal catalysts are filled in the reaction beds, and a feeding branch pipe is arranged above each reaction bed; at least two layers of tower trays are arranged in the separation section; the lower part of the reaction section is formed into an air inlet cavity, and a gas-phase material inlet communicated with the air inlet cavity is arranged on the tower body;
the discharge port of the polyether tank is communicated with the inlet of the raw material pump, the outlet of the raw material pump is connected with a feeding main pipe, and the feeding main pipe is communicated with each feeding branch pipe after sequentially passing through a refrigerant channel of the first heater, a refrigerant channel of the second heater and the first heating furnace;
the discharge port of the liquid ammonia tank is communicated with the inlet of an ammonia pump, the outlet of the ammonia pump is communicated with the inlet of an ammonia gasifier, and the outlet of the ammonia gasifier is communicated with the gas-phase material inlet of the reaction tower after sequentially passing through a refrigerant channel of a third heater, a refrigerant channel of a fourth heater and a second heating furnace;
a discharge hole at the top of the tower of the reaction tower is connected with a discharge pipe at the top of the tower, and the discharge pipe at the top of the tower is communicated with a feed inlet of the high-pressure separator after sequentially passing through a heating medium channel of the second heater, a heating medium channel of the first heater, a water cooler and a pressure regulating valve; a tower bottom discharge pipe is connected to a tower bottom discharge hole of the reaction tower, and the tower bottom discharge pipe is communicated with a finished product tank after sequentially passing through a heat medium channel of a fourth heater, a heat medium channel of a third heater and a finished product cooler;
a gas phase outlet at the top of the high-pressure separator is connected with a hydrogen return pipe, the hydrogen return pipe is communicated with an air inlet of a hydrogen compressor, an outlet of the hydrogen compressor is communicated with an inlet of a refrigerant channel of the third heat exchanger, and a hydrogen storage device is communicated with the hydrogen return pipe; the liquid phase outlet at the bottom of the high-pressure separator is communicated with the material inlet of the membrane separator, the concentrated solution outlet of the membrane separator is communicated with the reflux port at the top of the reaction tower, the reflux port is positioned above the separation section, the permeate outlet of the membrane separator is communicated with the liquid inlet of the aqueous ammonia separation tower, the exhaust port at the top of the aqueous ammonia separation tower is communicated with the air inlet of the ammonia compressor, and the outlet of the ammonia compressor is communicated with the inlet of the refrigerant channel of the third heat exchanger.
2. The continuous hydroammonation production apparatus for amino-terminated polyethers according to claim 1, wherein,
4-6 reaction beds are arranged in the reaction section, each reaction bed is filled with supported metal catalysts with the same height, and 10-20 layers of trays are arranged in the separation section.
3. The continuous hydroammonation production apparatus for amino-terminated polyethers according to claim 1, wherein,
corresponding to each feeding branch pipe, a liquid distributor is arranged above each reaction bed layer, and the feeding branch pipes are communicated with the corresponding liquid distributors.
4. The continuous hydroammonation production apparatus for amino-terminated polyethers according to claim 1, wherein,
a gas distributor is arranged in the gas inlet cavity, and the gas-phase material inlet is communicated with the gas distributor.
5. The continuous hydroammonation production apparatus for amino-terminated polyethers according to claim 1, wherein,
the water-ammonia separation tower is a tray tower, an upper tray set and a lower tray set are arranged on the water-ammonia separation tower, wherein the upper tray set is positioned above the lower tray set, and a liquid inlet of the water-ammonia separation tower is positioned between the upper tray set and the lower tray set in the height direction.
6. The continuous hydroamination preparation apparatus of an amino-terminated polyether according to claim 5, wherein,
the upper tray group comprises 10-20 layers of upper trays, and the lower tray group comprises 10-20 layers of lower trays.
7. The continuous hydroamination preparation apparatus of an amino-terminated polyether according to claim 1, wherein,
a reflux tank is arranged at the top of the water-ammonia separation tower, an exhaust port at the top of the water-ammonia separation tower is communicated with the reflux tank after passing through a condenser, the bottom of the reflux tank is communicated with the top of the water-ammonia separation tower through a reflux pipe, and an air outlet at the top of the reflux tank is communicated with an air inlet of an ammonia compressor;
the bottom of the water-ammonia separation tower is provided with a reboiler, two liquid outlet pipes are led out from the tower bottom of the water-ammonia separation tower, one liquid outlet pipe is communicated with a liquid inlet of the reboiler, the other liquid outlet pipe is used as a sewage discharge pipe, and a liquid outlet of the reboiler is communicated with the tower bottom of the water-ammonia separation tower.
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