CN216778816U - Device for polycondensing polyol by using cyclic compound - Google Patents
Device for polycondensing polyol by using cyclic compound Download PDFInfo
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- CN216778816U CN216778816U CN202220205906.7U CN202220205906U CN216778816U CN 216778816 U CN216778816 U CN 216778816U CN 202220205906 U CN202220205906 U CN 202220205906U CN 216778816 U CN216778816 U CN 216778816U
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- 150000001923 cyclic compounds Chemical class 0.000 title claims abstract description 44
- 229920005862 polyol Polymers 0.000 title claims abstract description 18
- 150000003077 polyols Chemical class 0.000 title claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 88
- 238000006068 polycondensation reaction Methods 0.000 claims abstract description 23
- 239000000463 material Substances 0.000 claims abstract description 18
- 239000007789 gas Substances 0.000 claims description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims description 7
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 6
- 150000005846 sugar alcohols Polymers 0.000 claims 4
- 238000010992 reflux Methods 0.000 claims 1
- 238000009834 vaporization Methods 0.000 claims 1
- 230000008016 vaporization Effects 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 4
- 239000000047 product Substances 0.000 description 35
- 239000007788 liquid Substances 0.000 description 17
- 238000012546 transfer Methods 0.000 description 15
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 9
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 description 9
- 238000003756 stirring Methods 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 7
- 239000002202 Polyethylene glycol Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 6
- 239000012071 phase Substances 0.000 description 6
- 229920001223 polyethylene glycol Polymers 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 4
- 239000006185 dispersion Substances 0.000 description 4
- 238000009826 distribution Methods 0.000 description 4
- 238000004880 explosion Methods 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 229920000642 polymer Polymers 0.000 description 4
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 3
- 239000004721 Polyphenylene oxide Substances 0.000 description 3
- 230000007547 defect Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000007046 ethoxylation reaction Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000000178 monomer Substances 0.000 description 3
- 229920000570 polyether Polymers 0.000 description 3
- 238000011112 process operation Methods 0.000 description 3
- 238000010926 purge Methods 0.000 description 3
- 238000007789 sealing Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000007792 gaseous phase Substances 0.000 description 2
- 239000012456 homogeneous solution Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 238000013021 overheating Methods 0.000 description 2
- 238000012643 polycondensation polymerization Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical group C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
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- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
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Abstract
The utility model provides a device for polycondensing polyol by using cyclic compounds, which comprises a reaction kettle, wherein a first micro-interface generator is arranged at the bottom layer in the reaction kettle, a second micro-interface generator is arranged at the middle layer in the reaction kettle, a first one-way channel for preventing materials from flowing reversely is arranged between the first micro-interface generator and the second micro-interface generator, a second one-way channel is arranged above the second micro-interface generator, a polyol pipeline and a cyclic compound pipeline are arranged on the side edge of the bottom of the reaction kettle, the first micro-interface generator is connected with the cyclic compound pipeline for introducing vaporized cyclic compounds for dispersing and crushing, and a polycondensation product pipeline is arranged at the top of the reaction kettle. By applying the micro-interface enhanced reaction technology, the consumption rate of the cyclic compound gas can be greatly increased, the partial pressure of the cyclic compound in the gas phase is effectively reduced, and the intrinsic safety of equipment is greatly improved.
Description
Technical Field
The utility model belongs to the technical field of high molecular polymers, and particularly relates to a device for polycondensing polyol by using a cyclic compound.
Background
Condensation polymerization, abbreviated as polycondensation, is a reaction in which one or more monomers are condensed with each other to form a polymer, the main product of which is called a polycondensate. The monomer for condensation polymerization is a polymer formed by removing small molecules when a compound with 2 (or more) reactive functional groups is polymerized, so that the molecular weight of a repeating structural unit of the polymer is smaller than that of the monomer.
Most of the existing polycondensation reactions use a stirred tank reactor, and the reactor has the advantages of compact structure, simple equipment, high process operation flexibility, high stirring power, suitability for production of high molecular weight polyether and the like. But the reactor also has obvious defects that the effect of stirring and breaking bubbles in the reaction process is poor, and the gas-liquid mixture in the reaction kettle is uneven and easily generates concentration and temperature gradient, so that the mass transfer and reaction rate are low; the existence of the coil type heat exchanger reduces the effective volume of the kettle, reduces the production capacity of the reactor, and is difficult to overhaul and replace; the presence of the stirrer is liable to cause local hot spots of the gaseous cyclic compound, creating the risk of explosion (formation of electric dipoles between the stirrer and the reactor wall and overheating of the mechanical sealing means). In addition, if the mechanical sealing means is damaged or fails, oxides may overflow from the inside of the reactor, and foreign substances may enter the reactor, causing a problem in the safety of the reactor.
In view of the above, the present invention is particularly proposed.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a device for polycondensing polyol by using cyclic compounds, which solves the problems of small gas-liquid contact surface, poor gas dispersion performance, low mass transfer efficiency and wide molecular weight distribution of products of a stirred tank reactor.
In order to achieve the technical purpose, the utility model provides the following technical scheme:
the utility model provides a device for polycondensing polyol by using cyclic compounds, which comprises a reaction kettle, wherein a first micro-interface generator is arranged at the bottom layer in the reaction kettle, a second micro-interface generator is arranged at the middle layer in the reaction kettle, a first one-way channel for preventing materials from flowing reversely is arranged between the first micro-interface generator and the second micro-interface generator, a second one-way channel is arranged above the second micro-interface generator, a polyol pipeline and a cyclic compound pipeline are arranged on the side edge of the bottom of the reaction kettle, the first micro-interface generator is connected with the cyclic compound pipeline for introducing vaporized cyclic compounds for dispersing and crushing, and a polycondensation product pipeline is arranged at the top of the reaction kettle.
Most of the stirred tank reactors in the prior art have the advantages of compact structure, simple equipment, high process operation flexibility, high stirring power, suitability for production of high molecular weight polyether and the like, but the stirred tank reactors also have obvious defects, the effect of stirring and breaking bubbles in the reaction process is poor, the gas-liquid mixture in the reaction kettle is not uniform, and concentration and temperature gradient are easily generated, so that the mass transfer and reaction rate is low; the existence of the heat exchange coil reduces the effective volume of the kettle, so that the production capacity of the stirred tank reactor is reduced, and the maintenance and the replacement are difficult; the presence of the stirred tank reactor is liable to cause local hot spots of the gaseous cyclic compound, creating the risk of explosion (formation of electrical dipoles between the stirrer and the reactor wall and overheating of the mechanical seal), and moreover, if the mechanical seal is damaged or fails, the oxides may overflow from the inside of the stirred tank reactor and external substances may enter the stirred tank reactor, causing reactor safety problems.
According to the utility model, the first micro-interface generator is arranged at the bottom of the reaction kettle, so that the cyclic compound is crushed and dispersed into the micro-bubbles of the cyclic compound, the phase boundary mass transfer area of the cyclic compound and the polyol is increased, the gas-liquid mass transfer efficiency is greatly enhanced, and the polycondensation reaction efficiency is improved. The first micro-interfacial generator is disposed at the bottom of the reaction vessel, and preferably is disposed at the centerline of the reaction vessel. First, the microbubbles are upwardly directed, and placing the first micro-interfacial surface generator lowermost allows the microbubbles to react with the polyol for a longer period of time, which also increases the efficiency of the polycondensation reaction. Secondly, the reason for this is that the gas bubbles are more uniformly distributed in the center line of the reactor. If the first micro-interface generator is arranged at one side of the reaction kettle, the micro-bubbles at the position far away from the first micro-interface generator are less and the reaction efficiency is not high.
A first one-way channel is further arranged above the first micro-interface generator, so that materials can only move from bottom to top, and the materials on the upper side cannot flow back. After the lower polycondensation reaction is finished, the reaction product enters the middle part of the reaction kettle through the first one-way channel and continues to react in the second micro-interface generator, so that the product from the middle part of the reaction kettle is higher in purity than the product from the bottom part, and in order to prevent the high-purity product and the low-purity product from being mixed together, the first one-way channel is arranged to block the bottom part and the middle part of the reaction kettle.
And a second one-way channel is also arranged above the second micro-interface generator, the function of the second one-way channel is the same as that of the first one-way channel, and a product coming out of the first one-way channel can be discharged and collected through a polycondensation product pipeline, so that the purity of the polycondensation product can be further ensured.
Preferably, the second micro-interface generator is communicated with a second external circulation channel, an outlet of the second external circulation channel is arranged between the first one-way channel and the second micro-interface generator, the outlet of the second external circulation channel is sequentially connected with a second one-way valve, a second circulation pump and a second heat exchanger, and a return port of the second external circulation is communicated with the top of the second micro-interface generator. And a second external circulation channel is arranged at the side edge of the second micro-interface generator and outside the reaction kettle, and an outlet of the second external circulation channel is arranged above the first one-way channel and close to the first one-way channel, so that liquid-phase and gas-phase materials which come out from the first one-way channel and are not completely reacted are directly sucked into the second external circulation channel and are sent to the second micro-interface generator for re-crushing and dispersion after being heated, the mass transfer efficiency between gas and liquid is improved again in the process, and the efficiency of polycondensation reaction is improved.
Preferably, the first micro-interface generator is communicated with a first external circulation channel, an outlet of the first external circulation channel is arranged at the bottom of the reaction kettle, the outlet of the first external circulation channel is sequentially connected with a first one-way valve, a first circulation pump and a first heat exchanger, and a return port of the first external circulation is communicated with the top of the first micro-interface generator. The side of the first micro-interface generator, the outer side of the reaction kettle is communicated with a first outer circulation channel, and the outlet of the first outer circulation channel is arranged at the bottom of the reaction kettle, so that the material at the bottom of the reaction kettle can be rolled back to the first micro-interface generator, and the reaction material can be effectively utilized. First outer circulation channel is provided with first check valve can prevent that the material from the first outer circulation channel countercurrent of following, and the rethread circulating pump provides power, and the rethread heat exchanger heats, returns first micro-interface generator after heating the material to reaction temperature.
Preferably, the top of the reaction kettle is provided with a sieve plate for slowing down the flow rate of the materials.
Preferably, the top of the reaction kettle is connected with a nitrogen inlet pipeline. The nitrogen inlet pipeline is arranged at the top of the reaction kettle, so that firstly, nitrogen is used as purge gas to purge the top of the reaction kettle, and secondly, the pressure in the reaction kettle can be controlled.
Preferably, a tail gas pipeline is arranged at the top of the reaction kettle and is divided into two pipelines, one pipeline is connected with a second external circulation channel, and the other pipeline is used for transporting and discharging the cyclic compound after passing through a cold well for collecting the cyclic compound. The purpose of the cold well is to liquefy, collect and store the cyclic compound and prevent the cyclic compound from polluting the air.
Preferably, the product pipeline is divided into two pipelines, one pipeline sends the product back to the second external circulation channel, and the other pipeline discharges and collects the product.
Preferably, the second outer circulation channel is provided with a second product outlet for discharging the product. The polycondensation product from the second product outlet is of a somewhat higher purity than the polycondensation product from the first product outlet, and may be collected for discharge.
Preferably, the first external circulation channel is provided with a first product outlet for discharging the product. The polycondensation products with low purity can also be obtained after the treatment by the first micro-interface generator, and the polycondensation products are discharged and collected through the first product outlet.
Compared with the prior art, the utility model has the advantages that:
(1) greatly improves the mass transfer efficiency of gas-liquid two phases and improves the molecular weight distribution of products.
The ethoxylation reactor is a typical vapor-liquid phase reactor, in which a vapor phase cyclic compound enters a liquid phase in a diffusion mode for reaction and is controlled by chemical reaction and interfacial mass transfer, wherein the mixing and mass transfer of gas-liquid materials are important factors influencing the reaction performance, the production capacity and the technical advancement of the reactor. The mass transfer efficiency is an important index for measuring the technical level of an ethoxylation device, and the mass transfer enhancement is an important direction for the improvement of all ethoxylation processes. The stirred tank reactor has small gas-liquid contact surface, poor gas dispersion performance, low mass transfer efficiency and wide molecular weight distribution of products. The utility model forms a micro-interface system in the reactor by applying a micro-interface reinforced reaction technology, increases the gas-liquid contact area by tens of times, greatly strengthens the gas-liquid mass transfer efficiency, and hopes to obtain products with narrow molecular weight distribution.
(2) Improve the intrinsic safety performance of the equipment.
The gas phase space above the kettle type reactor is provided with gaseous phase aggregation of cyclic compounds, and the dynamic seal of the stirring paddle is easy to leak and generate static electricity, thereby causing safety accidents such as poisoning, explosion and the like. By applying the micro-interface enhanced reaction technology, the consumption rate of the cyclic compound can be greatly accelerated, the partial pressure of the cyclic compound in the gas phase is effectively reduced, and the intrinsic safety of equipment is greatly improved.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the utility model. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
FIG. 1 is a schematic structural diagram of an apparatus for polycondensing a polyol with a cyclic compound according to this example.
Wherein:
10-a reaction kettle; 11-a first micro-interface generator;
12-a second micro-interface generator; 111-a first unidirectional channel;
121-a second unidirectional channel; 13-a polyol conduit;
14-a cyclic compound conduit; a 17-polycondensation product conduit;
102-a second external circulation channel; 128-an outlet of the second external circulation channel;
122-a second one-way valve; 123-a second circulation pump;
124-a second product outlet; 125-a second valve;
126-a second heat exchanger; 127-a return port for the second external circulation;
101-a first external circulation channel; 118-the outlet of the first external circulation channel;
112-a first one-way valve; 113-a first circulation pump;
114-a first product outlet; 115-a first valve;
116-a first heat exchanger; 117 — return port for first external circulation;
15-nitrogen inlet line; 16-a tail gas pipeline;
161-return valve; 162-cold well;
171-a third valve; 18-sieve plate.
Detailed Description
The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and the detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are conventional products which are not indicated by manufacturers and are commercially available.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In order to more clearly illustrate the technical solution of the present invention, the following description is made in the form of specific embodiments.
Examples
Referring to fig. 1, a schematic structural diagram of an apparatus for polycondensing polyol with cyclic compounds according to the present invention is shown. This device includes reation kettle 10, and reation kettle 10 divide into bottom, middle part and top three, and bottom and middle part are separated through first one-way passageway 111, and middle part and top are separated through second one-way passageway 121. In this embodiment, the cyclic compound is selected from propylene oxide and the polyol is ethylene glycol.
First, the bottom of the reaction vessel 10 is provided with a first micro-interface generator 11. The first micro-interface generator 11 is disposed on the centerline of the reaction vessel 10. Polyol line 13 enters reactor 10 through the bottom sidewall of reactor 10, ethylene glycol is introduced into reactor 10, and cyclic compound line 14 also enters reactor 10 through the bottom sidewall of reactor 10 and communicates with the top of first micro-interfacial generator 11. Propylene oxide is vaporized instantaneously upon entering reaction vessel 10 because the operating temperature of reaction vessel 10 will vaporize propylene oxide. A first external circulation channel 101 is further arranged around the first micro-interface generator 11, and the bottom of the reaction kettle 10 is provided with an outlet 118 of the first external circulation channel. The outlet 118 of the first external circulation channel pumps the material at the bottom of the reaction kettle 10 through the first check valve 112 by the first circulation pump 113, and then the material is returned to the first micro-interface generator 11 after passing through the first heat exchanger 116, that is, the first external circulation channel 101 returns the material to the first micro-interface generator 11 through the return port 117 of the first external circulation. The first external circulation channel 101 is further divided into a channel, which is arranged between the first circulation pump 113 and the first heat exchanger 116, and a first valve 115 is arranged on the channel, the first valve 115 is followed by a first product outlet 114, and the first product outlet 114 can collect polyethylene glycol with purity not too high.
And a second micro-interface generator 12 is arranged at the middle section of the reaction kettle 10. The second micro-interface generator 12 is also arranged on the midline of the reaction kettle 10, and is positioned right above the first micro-interface generator 11. An outlet 128 of the second external circulation channel is formed at the middle section of the reaction kettle 10, which is close to the first one-way channel 111, and the material coming out from the outlet 128 of the second external circulation channel sequentially passes through the second one-way valve 122, the second circulation pump 123 and the second heat exchanger 126 and then returns to the second micro-interface generator 12 from a return port 127 of the second external circulation. Thus, the unreacted cyclic compound microbubbles from the bottom of the reaction vessel 10 are sucked into the second micro-interface generator 12 for secondary crushing and dispersion. A second valve 125 and a second product outlet 124 are disposed on the second external circulation channel 102 for collecting the polyethylene glycol with higher purity.
Finally, the top end of the reaction vessel 10 is provided with sieve plates 18, and the sieve plates 18 slow down the rising speed of the bubbles. A nitrogen gas inlet pipeline 15 is also arranged on the liquid level at the top of the reaction kettle 10 for purging the unreacted propylene oxide gas at the top of the reaction kettle 10. A part of the cyclic propylene oxide gas is cooled by the cold well 162 and then recovered, and then the remaining tail gas is discharged through the tail gas pipeline 16; the other part returns to the second external circulation channel 102 through the return valve 161 to continue the reaction, thus improving the utilization rate of the materials. A polycondensation product pipeline 17 is arranged above the sieve plate 18 at the top of the reaction kettle 10, one part of the polyethylene glycol is collected and stored, and the other part of the polyethylene glycol is returned to the second external circulation channel 102 for recycling.
When the device is used for producing polyethylene glycol, 150L of ethylene glycol is added into a reaction kettle 10 at the beginning of the reaction, nitrogen gas replacement is carried out on the reaction kettle 10, and nitrogen gas is introduced until the pressure is 140 KPa. Starting the first micro-interface generator and the second micro-interface generator and heating the reaction kettle 10 to 100 ℃ to form a liquid homogeneous solution. Liquid propylene oxide is continuously added into the first micro-interface generator 11 at a feeding speed of 100-160kg/h, the liquid propylene oxide is vaporized into gaseous propylene oxide at the moment of entering the reaction kettle 10 and is introduced into the first micro-interface generator 11, and the reaction temperature is controlled to be about 130-140 ℃ by using the first heat exchanger and the second heat exchanger in the reaction process.
Comparative example
The comparative example adopts a stirred tank reactor, firstly, 150L of initiator is added into the reactor at the beginning of the reaction, nitrogen gas replacement is carried out on the reactor, and nitrogen gas is introduced until the pressure is 150 kPa; starting stirring to heat the materials in the reaction kettle to 100 ℃ to form a liquid homogeneous solution; continuously adding liquid ethylene oxide into a feed inlet at the bottom of the reactor at the feeding speed of 100-; in the reaction process, an external jacket of the reactor is used for heating and an internal cooling coil is used for cooling so as to accurately control the reaction temperature to be 130-150 ℃, and the highest reaction pressure is 550 kPa; after the feeding is finished, continuously preserving heat and curing, wherein the feeding time is 3 hours, and the curing time is 0.5-1 hour; when the pressure difference between the feeding pipeline and the kettle is less than 150kPa, the pressure in the kettle exceeds 550kPa, and the temperature in the kettle exceeds 190 ℃, the interlocking starts to automatically cut off the feeding of EO.
Polyethylene glycol was produced according to the above examples, with the following data:
| parameters in the reaction tank | Examples | Comparative example |
| Initial reaction pressure (KPa) | 140 | 150 |
| End stage reaction pressure (KPa) | 530 | 550 |
| Reaction temperature (. degree.C.) | 130 | 150 |
| End stage reaction viscosity (cp) | 85 | 95 |
| Propylene oxide addition Rate (kg/h) | 150 | 120 |
From the experimental data, the stirred tank reactor adopted in the comparative example has the advantages of compact structure, simple equipment, high process operation flexibility, high stirring power, suitability for production of high molecular weight polyether and the like. However, the reactor has obvious defects that the effect of stirring and breaking bubbles in the reaction process is poor, and the gas-liquid mixture in the reaction kettle is not uniform and is easy to generate concentration and temperature gradient, so that the mass transfer and reaction rate is low; the effective volume of the kettle is reduced due to the existence of the coil pipe, so that the production capacity of the reactor is reduced, and the maintenance and the replacement are difficult; the presence of the stirrer is liable to cause localised hot spots of ethylene oxide in the gaseous phase, creating a risk of explosion. In addition, if the mechanical sealing means is damaged or fails, oxides may overflow from the inside of the reactor, and foreign substances may enter the reactor, causing a problem in the safety of the reactor. The embodiment of the utility model forms a micro-interface system in the reaction kettle, increases the gas-liquid contact area by tens of times, greatly enhances the gas-liquid mass transfer efficiency, and effectively reduces the reaction pressure and the reaction temperature. And by applying a micro-interface reinforced reaction technology, the consumption rate of the ethylene oxide is greatly increased, the partial pressure of the ethylene oxide in a gas phase is effectively reduced, and the intrinsic safety of equipment is greatly improved.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the utility model has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (9)
1. The utility model provides an utilize cyclic compound to device of polyol polycondensation, its characterized in that, includes reation kettle, reation kettle's inside bottom is provided with first micro interface generator, reation kettle's inside middle level is provided with second micro interface generator, first micro interface generator with the centre of second micro interface generator is provided with the first one-way channel that is used for preventing the material countercurrent, the top of second micro interface generator is provided with the one-way channel of second, polyol pipeline and cyclic compound pipeline have been seted up to reation kettle's bottom side, first micro interface generator is connected with the cyclic compound pipeline is in order to be used for introducing the cyclic compound of vaporization and to disperse the breakage, reation kettle's top is provided with the polycondensation product pipeline.
2. The apparatus according to claim 1, wherein the second micro-interface generator is connected to a second external circulation channel, an outlet of the second external circulation channel is disposed between the first one-way channel and the second micro-interface generator, the outlet of the second external circulation channel is connected to a second one-way valve, a second circulation pump and a second heat exchanger in sequence, and a return port of the second external circulation channel is connected to a top of the second micro-interface generator.
3. The apparatus according to claim 1, wherein the first micro-interface generator is connected to a first external circulation channel, an outlet of the first external circulation channel is disposed at the bottom of the reaction kettle, the outlet of the first external circulation channel is connected to a first check valve, a first circulation pump and a first heat exchanger in sequence, and a reflux port of the first external circulation channel is connected to the top of the first micro-interface generator.
4. The apparatus for polycondensation of polyhydric alcohol with cyclic compound according to claim 1, wherein the top of the reaction vessel is provided with a sieve plate for slowing down the flow rate of the material.
5. The apparatus for polycondensation of polyol with cyclic compound according to claim 1, wherein a nitrogen gas inlet line is connected to the top of the reaction vessel.
6. The apparatus according to claim 2, wherein a tail gas pipe is opened at the top of the reaction vessel, the tail gas pipe is divided into two pipes, one of the two pipes is connected to the second external circulation channel, and the other pipe is used for transporting and discharging the cyclic compound after passing through a cold well for collecting the cyclic compound.
7. The apparatus for polycondensation of polyhydric alcohol with cyclic compound according to claim 2, wherein the product line is divided into two lines, one line feeding back the product to the second external circulation path and the other line discharging and collecting the product.
8. The apparatus for polycondensation of polyhydric alcohol with cyclic compound according to claim 2, wherein the second external circulation passage is provided with a second product outlet for discharging the product.
9. The apparatus for polycondensation of polyhydric alcohol with cyclic compound according to claim 3, wherein the first external circulation passage is provided with a first product outlet for discharging the product.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114471403A (en) * | 2022-01-19 | 2022-05-13 | 南京延长反应技术研究院有限公司 | Device and method for polycondensing polyol by using cyclic compound |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114471403A (en) * | 2022-01-19 | 2022-05-13 | 南京延长反应技术研究院有限公司 | Device and method for polycondensing polyol by using cyclic compound |
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