Device for continuously producing polyether

Abstract

The utility model discloses a device for continuously producing polyether. The device comprises a mixing kettle, a mixing kettle discharging pump, a receiving tank A, a receiving tank discharging pump A, a PO feeding pump, a static mixer, a pipeline reactor, a reactor discharging pump, an adsorption tower, an adsorption tower discharging pump, a receiving tank B, a receiving tank discharging pump B and a distillation tower, the method comprises the following steps: mixing an alcohol raw material and a catalyst in a mixing kettle, pumping into a receiving tank A for temporary storage, pumping the mixed material in the receiving tank A into a static mixer, mixing with epoxypropane, feeding into a pipeline reactor for reaction, pumping the reaction product in the pipeline reactor into an adsorption tower to remove metal elements introduced by the catalyst, a reaction product in the adsorption tower is pumped into a receiving tank B for temporary storage through an adsorption tower discharging pump, a reaction product in the receiving tank B is pumped into a distillation tower for distillation and purification, and purified polyether is obtained. By adopting the continuous production device, the energy consumption can be reduced, the generation of waste gas, waste residues and waste water is reduced, and the production cost is further reduced.

Description

TECHNICAL FIELD

[0001] The utility model relates to the technical field of polymer preparation, specifically relates to a device for continuous production of polyether. BACKGROUND

[0002] D230 polyether amine is a kind of bifunctional primary amine, with propylene oxide (PO) as chain extender, low molecular polyether with hydroxyl value of 470-490 mgKOH / g, average molecular weight is about 230;Its main chain is composed of repeated propylene oxide units, functional groups are located at the second carbon atom at the end of aliphatic polyether chain, it is a kind of active hydrogen equivalent higher polyether amine, which makes polyether amine D230 have higher reactivity and selectivity in many applications. Main applications include epoxy resin curing agent, manufacturing epoxy resin handicraft and paint, spraying polyurea elastomer and other fields.

[0003] 2023 polyether is the initiator of D230 polyether amine, and its synthesis technology is that propylene glycol (PG), dipropylene glycol (DPG) or tripropylene glycol (TPG) is used as initiator, and PO is polymerized under the action of catalyst under certain temperature, time and pressure in reaction kettle, to form 2023 crude polyether, the crude polyether is treated to obtain semi-finished product, and the semi-finished product is purified by rectification to obtain product.

[0004] The existing polyether is usually produced by high-pressure reaction kettle type batch method, and the batch method production has the defects of unstable quality, many side reactions and difficult to realize automatic control. UTILITY MODEL CONTENT

[0005] To solve the above problems, the utility model provides a device for continuous production of polyether.

[0006] The technical scheme adopted by the utility model is:

[0007] A device for continuous production of polyether, comprising a mixing kettle, a mixing kettle discharge pump, a receiving tank A, a receiving tank discharge pump A, a PO feed pump, a static mixer, a pipeline reactor, a reactor discharge pump, an adsorption tower, an adsorption tower discharge pump, a receiving tank B, a receiving tank discharge pump B and a distillation column;After alcohol raw materials and catalyst are mixed in the mixing kettle, the mixture is pumped into the receiving tank A for temporary storage by the mixing kettle discharge pump, the mixture in the receiving tank A is pumped into the static mixer by the receiving tank discharge pump A, and then mixed with propylene oxide pumped in by the PO feed pump to enter the pipeline reactor for reaction, the reaction product in the pipeline reactor is pumped into the adsorption tower to remove metal elements introduced by the catalyst by the reactor discharge pump, the reaction product in the adsorption tower is pumped into the receiving tank B for temporary storage by the adsorption tower discharge pump, and the reaction product in the receiving tank B is pumped into the distillation column for distillation and purification by the receiving tank discharge pump B.

[0008] Further, the mixing kettle is internally provided with a stirrer, the top of the mixing kettle is provided with an alcohol raw material inlet, a catalyst inlet, a vacuum extraction port and a circulating material inlet, the bottom of the mixing kettle is provided with a discharge port, the discharge port of the mixing kettle is connected with the inlet of a mixing kettle discharge pump through a pipeline and a mixing kettle discharge valve A, the outlet of the mixing kettle discharge pump is connected with the circulating material inlet of the mixing kettle through a pipeline and a mixing kettle circulating valve on one hand, and is connected with the inlet of a receiving tank A through a pipeline and a mixing kettle discharge valve B on the other hand.

[0009] Further, the top of the receiving tank A is provided with an inlet and a circulating material inlet, the bottom of the receiving tank A is provided with a discharge port, the discharge port of the receiving tank A is connected with the inlet of a receiving tank discharge pump A through a pipeline and a receiving tank discharge valve A, the outlet of the receiving tank discharge pump A is connected with the circulating material inlet of the receiving tank A through a pipeline and a receiving tank circulating valve on one hand, and is connected with the first inlet of a static mixer through a pipeline and a receiving tank discharge valve B on the other hand.

[0010] Further, the pipeline connecting the receiving tank discharge valve B and the static mixer is provided with a flow meter A and a preheater A.

[0011] Further, the outlet of the PO feeding pump is connected with the static mixer through a pipeline and a feeding valve, and the pipeline connecting the feeding valve and the static mixer is provided with a flow meter B and a preheater B.

[0012] Further, the reaction tube of the pipeline reactor is internally provided with an internal component of SX, SK, SL, SV or SD type, the inner diameter of the reaction tube is DN15-80, and the total length is 50-500 m.

[0013] Further, the pipeline reactor is provided with a heating and heat preservation device and a pressurizing device.

[0014] Further, the side of the distillation tower is sequentially provided with a propylene glycol outlet, a dipropylene glycol outlet, a tripropylene glycol outlet and a polyether discharge port from top to bottom.

[0015] Further, the propylene glycol outlet, the dipropylene glycol outlet and the tripropylene glycol outlet are respectively connected with the alcohol raw material sampling inlet of the mixing kettle through pipelines.

[0016] The utility model discloses the beneficial effects of:

[0017] 1. By adopting the pipeline reactor to carry out polymerization reaction, can stabilize the control reaction temperature, shorten the reaction time, reduce the occurrence of side reaction, greatly improve production efficiency, and the quality of the obtained product is stable and has narrower molecular weight distribution.

[0018] 2. By adopting the continuous production device, energy consumption can be reduced, waste gas, waste residue and waste water can be reduced, and production cost can be reduced.

[0019] 3, The device can be used for the production of 2023 polyether, and can also be used for the production of other types of polyether, including but not limited to polyether polyols generated by reacting propylene glycol, glycerol and the like as starting agents, wherein the molecular weight of the propylene glycol polyether polyol is 200-4000, and the propylene glycol, dipropylene glycol, and tripropylene glycol series products can also be produced; the molecular weight of the glycerol polyether polyol is 200-6000. BRIEF DESCRIPTION OF DRAWINGS

[0020] Figure 1 A schematic diagram of a device structure for continuous production of polyether.

[0021] The drawings are explained as follows: 101 is a mixing kettle, 102 is a mixing kettle discharge pump, 103 is a receiving tank A, 104 is a receiving tank discharge pump A, 105 is a flow meter A, 106 is a preheater A, 107 is a static mixer, 108 is a PO feed pump, 109 is a flow meter B, 110 is a preheater B, 111 is a pipe reactor, 112 is a reactor discharge pump, 113 is an adsorption tower, 114 is an adsorption tower discharge pump, 115 is a receiving tank B, 116 is a receiving tank discharge pump A, and 117 is a distillation column. DETAILED DESCRIPTION

[0022] In order to make the purpose, technical scheme and advantages of the utility model clearer, the technical scheme of the utility model will be described clearly and completely in combination with the drawings and a preferred embodiment.

[0023] Reference Figure 1 A device for continuous production of polyether, comprising a mixing kettle 101, a mixing kettle discharge pump 102, a receiving tank A 103, a receiving tank discharge pump A 104, a PO feed pump 108, a static mixer 107, a pipe reactor 111, a reactor discharge pump 112, an adsorption tower 113, an adsorption tower discharge pump 114, a receiving tank B 115, a receiving tank discharge pump B 116, and a distillation column 117.

[0024] The mixing kettle 101 is provided with a stirrer, an external heating and insulation device, an alcohol raw material inlet, a catalyst inlet, a vacuum extraction port and a circulating material inlet at the top, and a discharge port at the bottom. The alcohol raw material inlet is connected with an alcohol raw material feeding pipe, and the alcohol raw material feeding pipe is provided with an alcohol raw material feeding valve 1; the catalyst inlet is connected with a catalyst feeding pipe, and the catalyst feeding pipe is provided with a catalyst feeding valve 2; the vacuum extraction port is connected with a vacuum extraction pipeline, and the vacuum extraction pipeline is connected with a vacuum extraction device. The mixing kettle discharge port is connected with the inlet of the mixing kettle discharge pump 102 through a pipeline and a mixing kettle discharge valve A3, and the outlet of the mixing kettle discharge pump 102 is connected with the mixing kettle circulating material inlet through a pipeline and a mixing kettle circulating valve 4, and is connected with the feeding port of the receiving tank A 103 through a pipeline and a mixing kettle discharge valve B5.

[0025] The receiving tank A103 is externally provided with a heating and heat preservation device, a feed inlet and a circulating material inlet at the top, and a discharge outlet at the bottom. The discharge outlet of the receiving tank is connected with the inlet of a receiving tank discharge pump A104 through a pipeline and a receiving tank discharge valve A6. The outlet of the receiving tank discharge pump A104 is connected with the circulating material inlet of the receiving tank through a pipeline and a receiving tank circulating valve 7, and is connected with the first inlet of a static mixer 107 through a pipeline and a receiving tank discharge valve B8.

[0026] The second inlet of the static mixer 107 is connected with the outlet of a PO feed pump 108 through a pipeline and a feed valve 9. The pipeline between the feed valve 9 and the static mixer 107 is provided with a flow meter B109 and a preheater B110. The inlet of the PO feed pump 108 is connected with a PO raw material tank through a pipeline.

[0027] The outlet of the static mixer 107 is connected with the inlet of a reaction tube of a pipeline reactor 111.

[0028] The reaction tube of the pipeline reactor 111 is internally provided with an SX, SK, SL, SV or SD type of internal component to effectively improve the liquid-liquid and liquid-gas material mixing effect. The reaction tube has a preferred inner diameter of DN15-80 and a total length of 50-500 m to further improve the reaction efficiency. The reaction tube is externally provided with a heating and heat preservation device and a pressurizing device. The heating and heat preservation device is used to control the temperature range in the reaction tube, which is preferably 80-180 ℃, and the pressurizing device is used to control the pressure range in the reaction tube, which is preferably 0.1-3 MPa. The pipeline reactor is a prior art, and the specific model is not specially limited.

[0029] The outlet of the reaction tube of the pipeline reactor 111 is connected with the inlet of a reactor discharge pump 112 through a reactor discharge valve 10. The outlet of the reactor discharge pump 112 is connected with the feed inlet of an adsorption tower 113 through a pipeline.

[0030] The adsorption tower 113 is a prior art, and the specific model is not specially limited. The adsorption tower can adopt an upper inlet and lower outlet or a lower inlet and upper outlet mode. The adsorption tower 113 is filled with an adsorbent for adsorbing metal elements such as potassium and sodium ions introduced by a catalyst.

[0031] The discharge outlet of the adsorption tower 113 is connected with the inlet of a receiving tank discharge pump B114 through a pipeline and an adsorption tower discharge valve 11. The outlet of the receiving tank discharge pump B114 is connected with the top feed inlet of a receiving tank B115 through a pipeline. The bottom discharge outlet of the receiving tank B115 is connected with the inlet of a receiving tank discharge pump B116 through a pipeline and a receiving tank discharge valve B12. The outlet of the receiving tank discharge pump B116 is connected with the feed inlet of a distillation tower 117 through a pipeline.

[0032] The distillation column 117 is a prior art, preferably a plate column or a packed column, which is provided with propylene glycol outlet, dipropylene glycol outlet, tripropylene glycol outlet and polyether outlet from top to bottom. The propylene glycol (PG) outlet, dipropylene glycol (DPG) outlet and tripropylene glycol (TPG) outlet can be connected to the alcohol raw material inlet of the mixing kettle through pipelines, respectively. The PG, DPG and TPG are refluxed to the mixing kettle through pipelines, and are recycled as reaction raw materials to further improve the reaction efficiency.

[0033] The working mode of the device is as follows:

[0034] Before the reaction, all valves are in the closed state.

[0035] (1) Open the alcohol raw material feeding valve 1, and add one or more alcohol raw materials, preferably propylene glycol, dipropylene glycol, tripropylene glycol, glycerol, etc.

[0036] (2) Open the catalyst feeding valve 2, and add the catalyst, preferably KOH or NaOH.

[0037] (3) Start the stirring motor in the mixing kettle 101, mix the alcohol raw material and catalyst thoroughly, control the internal temperature of the mixing kettle in the range of 40-100℃, use the vacuum pump to draw negative pressure, and control the pressure in the mixing kettle in the range of -0.095 to 0 MPa.

[0038] (3) After the alcohol raw material and catalyst in the mixing kettle are thoroughly mixed, open the mixing kettle discharge valve A3 and the mixing kettle discharge valve B5, and use the mixing kettle discharge pump 102 to draw the mixed material into the receiving tank A 103, and control the internal temperature of the tank in the range of 40-100℃.

[0039] (4) Open the receiving tank discharge valve A6, the receiving tank discharge valve B8 and the feeding valve 9, start the receiving tank discharge pump A104 and the PO feeding pump 108, the mixed material in the receiving tank A is metered by the flowmeter A105 and preheated by the preheater A106, then enters the static mixer 107; at the same time, the PO is metered by the flowmeter B109 and preheated by the preheater B110, then enters the static mixer and is thoroughly mixed with the mixed material, and then enters the pipeline reactor 111.

[0040] (5) Control the temperature in the reaction tube of the pipeline reactor 111 in the range of 80-180℃, and the pressure in the range of 0.1-3 MPa; the alcohol raw material and PO are polymerized under the action of the catalyst in the pipeline reactor 111 to generate polyether.

[0041] (6) After the polymerization reaction is completed, open the reactor discharge valve 10, start the reactor discharge pump 112, and draw the polyether product into the adsorption tower 113 to remove the metal elements of the catalyst primer.

[0042] (7) open the adsorption column discharge valve 11, start the receiving tank discharge pump B114, remove the metal element polyether product into the receiving tank B115.

[0043] (8) open the receiving tank discharge valve B12, start the receiving tank discharge pump B116, the polyether product in the receiving tank B enters the distillation column 117, and is separated and purified by the distillation column to obtain 2023 polyether, and the PG, DPG and TPG taken from the side line of the distillation column 117 can be refluxed to the mixing kettle through a pipeline and recycled as a reaction raw material.

[0044] The above only describes the preferred embodiments of the present application, and it should be pointed out that for ordinary skilled persons in the art, some improvements and refinements can be made without departing from the principles of the present application, and these improvements and refinements are also within the protection scope of the present application.

Claims

1. An apparatus for the continuous production of polyether, characterized in that The system comprises a mixing kettle (101), a mixing kettle discharge pump (102), a receiving tank A (103), a receiving tank discharge pump A (104), a PO feed pump (108), a static mixer (107), a pipe reactor (111), a reactor discharge pump (112), an adsorption tower (113), an adsorption tower discharge pump (114), a receiving tank B (115), a receiving tank discharge pump B (116) and a distillation column (117). After the alcohol raw material and the catalyst are mixed in the mixing kettle (101), the mixture is pumped into the receiving tank A (103) for temporary storage through the mixing kettle discharge pump (102), the mixture in the receiving tank A (103) is pumped into the static mixer (107) through the receiving tank discharge pump A (104), mixed with the propylene oxide pumped in through the PO feed pump (108), and then enters the pipe reactor (111) for reaction, the reaction product in the pipe reactor (111) is pumped into the adsorption tower (113) to remove metal elements introduced by the catalyst through the reactor discharge pump (112), the reaction product in the adsorption tower (113) is pumped into the receiving tank B (115) for temporary storage through the adsorption tower discharge pump (114), and the reaction product in the receiving tank B (115) is pumped into the distillation column (117) for distillation and purification through the receiving tank discharge pump B (116).

2. A device for the continuous production of polyethers according to claim 1, characterized in that The mixing kettle (101) is provided with a stirrer, an alcohol raw material inlet, a catalyst inlet, a vacuum extraction port and a circulating material inlet at the top of the mixing kettle (101), and a discharge port at the bottom of the mixing kettle (101), the mixing kettle discharge port is connected with the inlet of the mixing kettle discharge pump (102) through a pipeline and a mixing kettle discharge valve A (3), the outlet of the mixing kettle discharge pump (102) is connected with the circulating material inlet of the mixing kettle (101) through a pipeline and a mixing kettle circulating valve (4), and connected with the inlet of the receiving tank A (103) through a pipeline and a mixing kettle discharge valve B (5).

3. A device for continuous production of polyether according to claim 1, characterized in that, The receiving tank A (103) is provided with an inlet and a circulating material inlet at the top, and a discharge port at the bottom, the receiving tank discharge port is connected with the inlet of the receiving tank discharge pump A (104) through a pipeline and a receiving tank discharge valve A (6), the outlet of the receiving tank discharge pump A (104) is connected with the circulating material inlet of the receiving tank A (103) through a pipeline and a receiving tank circulating valve (7), and connected with the first inlet of the static mixer (107) through a pipeline and a receiving tank discharge valve B (8).

4. A device for the continuous production of polyether according to claim 3, characterized in that A flow meter A (105) and a preheater A (106) are arranged on the pipeline connecting the receiving tank discharge valve B (8) and the static mixer (107).

5. The apparatus for continuous production of polyether according to claim 1, wherein, The outlet of the PO feed pump (108) is connected with the static mixer (107) through a pipeline and a feed valve (9), a flow meter B (109) and a preheater B (110) are arranged on the pipeline connecting the feed valve (9) and the static mixer (107).

6. The apparatus for continuously producing polyether according to claim 1, wherein The reaction tube of the pipe reactor (111) is provided with an internal component of SX, SK, SL, SV or SD type, the inner diameter of the reaction tube is DN15-80, and the total length is 50-500 m.

7. The apparatus for continuously producing polyether according to claim 1, wherein The pipe reactor (111) is provided with a heating and heat preservation device and a pressurizing device.

8. The apparatus for continuously producing polyether according to claim 1, wherein The distillation column (117) is provided with propylene glycol outlet, dipropylene glycol outlet, tripropylene glycol outlet and polyether outlet from top to bottom in sequence.

9. A device for the continuous production of polyether according to claim 8, characterized in that The propylene glycol outlet, dipropylene glycol outlet and tripropylene glycol outlet are connected with the alcohol raw material sampling port of the mixing kettle (101) through pipelines respectively.

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