CN114534624B - Tower type precondensation reactor - Google Patents
Tower type precondensation reactor Download PDFInfo
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- CN114534624B CN114534624B CN202011250773.7A CN202011250773A CN114534624B CN 114534624 B CN114534624 B CN 114534624B CN 202011250773 A CN202011250773 A CN 202011250773A CN 114534624 B CN114534624 B CN 114534624B
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- 239000000463 material Substances 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 24
- 230000008859 change Effects 0.000 claims abstract description 6
- 230000003247 decreasing effect Effects 0.000 claims abstract description 5
- 238000010438 heat treatment Methods 0.000 claims description 4
- 238000005452 bending Methods 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 3
- 238000006068 polycondensation reaction Methods 0.000 abstract description 16
- 238000006116 polymerization reaction Methods 0.000 abstract description 16
- 238000001704 evaporation Methods 0.000 abstract description 5
- 230000008020 evaporation Effects 0.000 abstract description 5
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 27
- 239000011797 cavity material Substances 0.000 description 13
- 239000000126 substance Substances 0.000 description 10
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 150000003384 small molecules Chemical class 0.000 description 6
- 238000003756 stirring Methods 0.000 description 6
- 229920000139 polyethylene terephthalate Polymers 0.000 description 5
- 239000005020 polyethylene terephthalate Substances 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000032050 esterification Effects 0.000 description 3
- 238000005886 esterification reaction Methods 0.000 description 3
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 3
- 238000010924 continuous production Methods 0.000 description 2
- 238000013016 damping Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 150000002148 esters Chemical class 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- -1 polyethylene terephthalate Polymers 0.000 description 2
- 239000002861 polymer material Substances 0.000 description 2
- 229920001634 Copolyester Polymers 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- KKEYFWRCBNTPAC-UHFFFAOYSA-L terephthalate(2-) Chemical compound [O-]C(=O)C1=CC=C(C([O-])=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-L 0.000 description 1
- 238000005809 transesterification reaction Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
- B01J3/04—Pressure vessels, e.g. autoclaves
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
- B01J3/002—Component parts of these vessels not mentioned in B01J3/004, B01J3/006, B01J3/02 - B01J3/08; Measures taken in conjunction with the process to be carried out, e.g. safety measures
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
- B01J3/03—Pressure vessels, or vacuum vessels, having closure members or seals specially adapted therefor
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Polyesters Or Polycarbonates (AREA)
Abstract
The invention discloses a tower type pre-polycondensation reactor, which comprises a tower body, wherein a material inlet and a material outlet are respectively arranged at the top and the bottom of the tower body, a vacuum pipe with a plurality of first vacuum ports is arranged at the central axis of the tower body, and the vacuum pipe outlet is arranged on the side wall of the tower body; a plurality of trays are arranged between the vacuum tube and the tower body, baffle plates are arranged on the trays, the height of each baffle plate is gradually increased or decreased from the position close to the tower body to the position far away from the tower body, and the height change directions of the adjacent upper layer of baffle plates and the adjacent lower layer of baffle plates are opposite; and each layer of tray is provided with a liquid drop port, and the liquid drop port is positioned at the baffle plate with the lowest height in each layer. According to the invention, materials are subjected to back-and-forth baffling/overflow on each layer of tray, liquid film flow can be realized at the overflow port, the gas-liquid contact area is increased, and mass transfer evaporation of EG is facilitated; the annular waterfall flows downwards at the inner side of the odd layer/the outer side of the even layer, so that the contact area between the material and the vacuum is quickly updated, the mass transfer efficiency is greatly improved, and the polymerization degree is increased higher.
Description
Technical Field
The invention relates to a reactor, in particular to a tower type pre-polycondensation reactor.
Background
At present, in the production process of high polymer materials of polyethylene terephthalate (PET) and copolyester thereof, the high polymer materials mainly comprise two stages of esterification and polycondensation. The polycondensation process of the existing continuous production device generally consists of three continuous processes of first preshrinking, second preshrinking and final polycondensation, wherein the main functions of the first preshrinking and the second preshrinking are to remove a large amount of small molecules or non-condensable gases in the esterified substances, and form an oligomer with the polymerization degree of 25-35, so that the guarantee is provided for the final polycondensation reaction. The traditional five-kettle process precondensation needs to involve two-stage independent reactors, and the system has the defects of long process, more control points, high operation cost and the like. In recent years, a plurality of enterprises sequentially push out a multi-layer prepolymerization kettle with stirring at the bottom, and an up-flow type prepolymerization tower and a down-flow type prepolymerization tower without stirring all have the defects of high equipment manufacturing cost, high equipment height, high operation cost and the like.
Disclosure of Invention
The invention aims to: the invention aims to provide a tower type precondensation reactor which can continuously react, is efficient and has low manufacturing and running costs.
The technical scheme is as follows: the tower-type precondensation reactor comprises a tower body and is characterized in that a material inlet and a material outlet are respectively arranged at the top and the bottom of the tower body, a vacuum pipe with a plurality of first vacuum ports is arranged at the central axis in the tower body, and the vacuum pipe outlet is arranged on the side wall of the lower part of the tower body; a plurality of trays are arranged between the vacuum tube and the tower body, and baffle plates are arranged on the trays;
The baffle plate at least comprises one of the following: the heights of the baffle plates are gradually increased or decreased from the position close to the tower body to the position far away from the tower body, and the height change directions of the adjacent upper layer of baffle plates and the lower layer of baffle plates are opposite; the height of each baffle plate is gradually increased or decreased from the middle part of the tray to the edge of the tray, and the height change directions of the adjacent upper and lower layers of baffle plates are opposite;
and each layer of tray is provided with a liquid drop port, and the liquid drop port is positioned at the baffle plate with the lowest height in each layer.
If the highest baffle plate of the tray is positioned in the middle of the tray, two liquid dropping ports are arranged and are respectively positioned at the inner edge and the outer edge of the tray.
The liquid-lowering port of the tray at the lowest layer is arranged close to the side wall of the tower body, an inner cavity and an outer cavity which are mutually nested are arranged below the tray at the lowest layer, the bottom of the outer cavity is communicated with the space in the tower, and the upper part of the inner cavity is communicated with the outer cavity.
And a second vacuum port is arranged at the top of the outer chamber.
The top of the baffle plate is provided with an overflow port, the overflow port comprises a notch and a bent guide vane, and the bending direction is towards one side of the adjacent shorter baffle plate.
When the highest baffle plate is positioned in the middle of the tray, the overflow port on the highest baffle plate comprises two flow guide sheets and notches facing opposite directions.
The first vacuum port is arranged below each layer of tray, and the height of the first vacuum port exceeds the highest baffle plate of the layer; if the layer of liquid dropping port is positioned at the vacuum tube, a baffle is arranged above the layer of vacuum port.
The height of the highest baffle plate of each layer is less than 1/2-3/4 of the distance between the two trays.
An umbrella cap is arranged at the top of the vacuum tube.
And a heating coil is arranged at the bottom of each layer of tray.
The beneficial effects are that:
compared with the prior art, the invention has the following remarkable advantages:
(1) The upper part of the invention adopts trays, materials are baffled/overflowed back and forth on each tray layer, and flow to the trays at the lower layer in the form of annular waterfall at the inner side of the odd layer/the outer side of the even layer, and liquid film flow can be realized at the overflow port, so that the gas-liquid contact area is increased, and mass transfer evaporation of EG (ethylene glycol) is facilitated; the annular waterfall flows downwards at the inner side of the odd layer/the outer side of the even layer, so that the contact area between the material and the vacuum is quickly updated, the mass transfer efficiency is greatly improved, and the polymerization degree is increased higher. The plug flow is used for replacing the full mixed flow, the uniformity of the prepolymer material is better, and the molecular weight distribution is narrower. In addition, repeated baffling/overflow replaces stirring film forming devolatilization, so that the gas-liquid updating times and devolatilization area are increased, and the polymerization degree is improved.
(2) The invention adopts the design of combining the inner cavity and the outer cavity at the lower part, the reciprocating baffling/overflow of the tray eliminates the stirring of the traditional kettle type pre-polycondensation kettle, the design of the inner cavity and the outer cavity at the lower part adopts gravity and pressure difference to realize the overflow of the outer cavity material to the inner cavity, the mass transfer and the heat transfer of the tower kettle material of the tower type pre-polycondensation reactor are realized under the condition of no stirring, the further improvement of the polymerization degree is promoted, and the effect of adjusting the residence time of the tower kettle material of the reactor is also realized.
(2) The vacuum system adopts the lower section for air extraction, the pressure in the reactor realizes the upper high and lower low, and the bumping of the upper tray is reduced. The lower tray is close to the vacuum port, the vacuum degree is higher, and under the condition of higher material viscosity, the high vacuum is beneficial to removing small molecules such as EG and the like, and the polymerization degree is further improved; the invention does not need power driving, the efficiency of plug flow and gas-liquid mass transfer is higher than that of the conventional pre-polycondensation reactor, the arrangement of vacuum pipelines is reasonable, the dynamic viscosity of the prepolymer reaches 5-20 Pa.s, and the intrinsic viscosity of the PET prepolymer can exceed 0.30dL/g.
(3) According to the invention, the heating coils are arranged in the annular diversion trenches of each layer, and the reaction temperature is maintained by means of the heat release of the polycondensate of the esterified substance, so that the method has the advantages of saving energy consumption and reducing equipment manufacturing difficulty.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
FIG. 2 is a schematic view of section A-A of FIG. 1;
FIG. 3 is a schematic view of the overflow port structure.
Detailed Description
The technical scheme of the invention is further described below with reference to the accompanying drawings.
From the standpoint of PET polyester polycondensation reaction mechanism, PET pre-polycondensation is to remove glycol micromolecules from the esterified substance under the condition of negative pressure forward reaction, and the transesterification reaction is continuously carried out between the glycol terephthalate monomers. Based on the reaction mechanism, the design of the precondensation reactor needs to be started from the following points: 1. and heat and mass transfer. The polycondensation reaction is exothermic, but the latent heat and sensible heat required for the evaporation of a large amount of EG in the ester are greater than the heat of reaction, so a large amount of heat is required just before the ester changes from positive pressure to negative pressure. In addition, the mass transfer area of the material is increased, so that the pre-polymerization reaction rate can be effectively improved. 2. Area and space are devolatilized. The small molecules are removed by converting liquid into gas under the vacuum negative pressure condition, the interface removal efficiency problem exists in the process, and in general, the larger the devolatilization area and the space, the more favorable the small molecules are removed. 3. Back mixing is avoided. The problem of uneven residence time distribution exists in the pre-polycondensation in the conventional vertical full-mixing reactor, so that the index of the prepolymer is easy to fluctuate, and the performance of a final polycondensation product is influenced. The ideal precondensate flowing state is always in a plug flow state, so that the uniform and stable material properties are ensured.
In view of the above-described drawbacks of the prior art, the column precondensation reactor of the present invention comprises: the tower body 1, the vacuum tube 2, the tray 3, the baffle plate 4, the liquid dropping port 5, the connecting pipe 6, the vacuum outlet 7, the outer chamber 8, the inner chamber 9, the material outlet 10, the material inlet 11, the first vacuum port 12, the second vacuum port 14, the lowest liquid dropping port 13 and the umbrella cap 15.
The top and the bottom of the tower body 1 are respectively provided with a material inlet 11 and a material outlet 10, the material inlet 11 can be arranged on the side wall of the top of the tower body 1 and is provided with one or more material outlets 10, and the material outlet 10 is arranged at the center of the bottom of the tower body 1.
The central axis department is equipped with the vacuum tube 2 that has a plurality of first vacuum ports 12 in the tower body 1, and vacuum tube 2 one end is located tower body 1 top, and the other end is for connecting vacuum outlet 7 through connecting pipe 6, and vacuum outlet 7 locates tower body 1 lower part lateral wall, namely on the tower body 1 lateral wall of lower floor's tower tray below. The top of the vacuum tube 2 is provided with an umbrella cap 15. In the partial existing reactor, top vacuum air suction is adopted, the chambers are subjected to vacuum adjustment through damping adjusting valves, and in the actual operation process, because the top vacuum air suction is adopted, the pressure of the uppermost chamber is lower than that of the lower chamber, so that the first chamber contains a large amount of EG, the esterified substances enter the reactor and are affected by high vacuum, fast vaporization is realized, bumping is generated, a large amount of glycol evaporation also entrains the esterified substances to enter a vacuum tube, and the damping regulator and the vacuum cyclone separator are easily blocked when the esterified substances are more. And the polymerization degree of the prepolymer cannot be effectively improved as the vacuum tube is higher in the lower pressure under the influence of vacuum air suction. The structure of the invention can ensure that the vacuum degree in the tower is increased layer by layer from top to bottom, and is beneficial to the downward flow of materials layer by layer.
A plurality of trays 3 are arranged between the vacuum tube 2 and the tower body 1, and baffle plates 4 are arranged on the trays 3. The height of the baffle plates 4 is gradually increased or decreased from the position close to the tower body 1 to the position far away from the tower body 1, and the height change directions of the baffle plates 4 of the adjacent upper layer and the lower layer are opposite. The height of the highest baffle plate of each layer is less than 1/2-3/4 of the distance between the two trays. The tower tray 3 divides the reactor into a plurality of chambers, materials are reciprocally baffled and overflowed in each layer of tower tray 3, the devolatilization efficiency is higher than that of the traditional full mixing stirring precondensation reaction kettle, and the reaction efficiency is high; the materials present plug flow in the high-efficiency tower type pre-polycondensation reactor, no back mixing is caused, and all physical indexes are uniform and stable.
The arrangement of the baffle plates 4 is according to the cross-sectional shape of the tower body 1, when the cross-section of the tower body 1 is square, the cross-section of the baffle plates 4 is in a corresponding shape like a Chinese character 'hui', and when the cross-section of the tower body 1 is circular, the cross-section of the baffle plates 4 is in a ring shape.
Each layer of trays 3 is provided with a liquid drop port 5, and the liquid drop port 5 is positioned at the baffle plate 4 with the lowest height in each layer, so that materials are sequentially reserved at the lowest baffle plate from the highest baffle plate, and the liquid drop port 5 at the baffle plate with the lowest height is reserved at the next layer of trays 3. The bottom of each tray 3 is provided with a heating coil, so that enough heat is ensured to maintain the evaporation of small molecules after the materials enter.
The first vacuum port 12 is arranged below each layer of partition board, the height of the vacuum port exceeds the highest baffle plate 7 of the layer, the material is ensured not to cover the first vacuum port 12, and if the layer of liquid dropping port is positioned near a vacuum pipe, a baffle plate is arranged above the layer of first vacuum port 12.
The top of each baffle plate 4 is provided with an overflow port 16, and the overflow port 16 of each baffle plate 4 comprises a notch 17 and a bent guide vane 18, wherein the bending direction is towards one side of the adjacent shorter baffle plate, so that the material is further ensured to flow towards the baffle plate with lower height.
The liquid-lowering mouth of the lowest tray is close to the side wall of the tower body 1, the liquid-lowering mouth 13 of the lowest tray extends for a certain length, an inner chamber 9 and an outer chamber 8 which are nested with each other are arranged below the tray, the bottom of the outer chamber 8 is communicated with the space in the tower and fixed with the tower body through a bracket, a second vacuum mouth 14 is arranged at the top of the outer chamber 8, the second vacuum mouth 14 is connected with an external air extraction system, and the outlet does not pass through the side wall of the tower body, so that the material is prevented from being sucked. The upper part of the inner chamber 9 is communicated with the outer chamber, the bottom of the inner chamber 9 is closed, and the center of the bottom is a material outlet 10. The vacuum level of the inner and outer chambers is higher than the vacuum level of the tray area, so that the material continuously flows into the inner chamber and is output from the outlet.
In another structure of the present invention, the height of the baffle plates 4 increases or decreases from the middle of the tray 3 to the edge of the tray 3 one by one, and may be symmetrically arranged about the middle of the tray or asymmetrically arranged. The height change directions of the upper and lower baffle plates are opposite. If the highest baffle plate of the tray 3 is positioned in the middle of the tray, two liquid dropping ports 5 are respectively positioned at the inner edge and the outer edge of the tray, so that the material flows from the middle to two sides. In this structure, when the highest baffle plate is located in the middle of the tray 3, the overflow port 16 on the highest baffle plate includes two flow guiding sheets and notches with opposite directions, and the flow guiding sheets may be disposed in the same notch or may be disposed in different notches in a staggered manner.
The invention can be used for pre-polycondensation reaction of terephthalic acid (PTA) and Ethylene Glycol (EG), wherein the esterified substance enters from a material inlet, and the density of the imported esterified substance is as follows: 1050-1100 kg/m 3, and the esterification rate is 96-98%. After entering the reactor, the odd-layer trays gradually flow into one side close to the vacuum tube from the outermost chamber in a baffling and overflow mode, the even-layer trays gradually flow into one side close to the vacuum tube from one side close to the tower body in a baffling and overflow mode, the even-layer trays are alternately performed, finally pass through the inner cavity structure and the outer cavity structure at the bottom of the tower body and are output from the material outlet at the bottom, the dynamic viscosity of the outlet is 5-20 Pa.s, and the residence time is 60-90 min.
The test results of the invention are:
The density of the esterified substance is 1060kg/m 3, the dynamic viscosity is 0.1 Pa.s, the esterification rate is 96%, the esterified substance enters the outer chamber of the first tray layer from the upper part of the tower body, the temperature of the prepolymerization tower is 280 ℃, the pressure is 15.0KPa, the number of the trays is 2, and the number of baffle plates of each layer is 6. The material is pre-polycondensed in the pre-polymerization tower for 60min to obtain the polymer with dynamic viscosity of 5 Pa.s.
In the tower-type precondensation reactor, the intrinsic viscosity of the material at the outlet of the first layer of tray can reach 0.15dL/g, the polymerization degree reaches 5-6, and the vacuum is 25KPa; the intrinsic viscosity of the material at the outlet of the second tray layer can reach 0.20dL/g, the polymerization degree reaches 5-10, and the vacuum is 20KPa; the intrinsic viscosity of the material at the outlet of the third layer tray can reach 0.24dL/g, the polymerization degree reaches 10-15, and the vacuum is 15KPa; the intrinsic viscosity of the material at the outlet of the fourth tray layer can reach 0.28dL/g, the polymerization degree reaches 15-20, and the vacuum is 10KPa; the intrinsic viscosity of the material at the outlet of the fifth layer tray can reach 0.32dL/g, the polymerization degree reaches 20-25, and the vacuum is 8KPa; the intrinsic viscosity of the material at the outlet of the sixth layer of tray can reach 0.34dL/g, the polymerization degree reaches 25-30, and the vacuum is 5KPa. By adopting the method, small molecules can be smoothly removed, and the polymerization degree of the prepolymerization reaction can reach or even exceed the expected target.
Claims (7)
1. The tower type precondensation reactor comprises a tower body (1) and is characterized in that a material inlet and a material outlet (10) are respectively arranged at the top and the bottom of the tower body (1), a vacuum tube (2) with a plurality of first vacuum ports (12) is arranged at the central axis in the tower body (1), one end of the vacuum tube (2) is positioned at the top of the tower body (1), the other end of the vacuum tube is connected with a vacuum outlet (7) through a connecting pipe (6), and the vacuum outlet (7) is arranged on the side wall of the tower body (1) below the lowest tray; a plurality of trays (3) are arranged between the vacuum tube (2) and the tower body (1), and baffle plates (4) are arranged on the trays (3); the first vacuum ports (12) are arranged below each layer of tray (3), and the heights of the first vacuum ports (12) exceed the highest baffle plate (4) of the layer;
The height of each baffle plate (4) is gradually increased or decreased from the position close to the tower body to the position far away from the tower body, and the height change directions of the adjacent upper and lower layers of baffle plates (4) are opposite;
Each layer of tray (3) is provided with a liquid dropping port (5), and the liquid dropping port (5) is positioned at the baffle plate (4) with the lowest height in each layer; the liquid dropping port of the tray (3) at the lowest layer is close to the side wall of the tower body (1), an inner chamber (9) and an outer chamber (8) which are mutually nested are arranged below the tray at the lowest layer, the bottom of the outer chamber (8) is communicated with the space in the tower, and the upper part of the inner chamber (9) is communicated with the outer chamber (8); the top of the outer chamber (8) is provided with a second vacuum port (14), and the second vacuum port (14) is connected with an external air extraction system; the bottom of the inner chamber (9) is closed, and the center of the bottom is provided with a material outlet (10).
2. A tower precondensation reactor according to claim 1, wherein the liquid drop port (5) is provided with two if the highest baffle (4) of the tray (3) is positioned in the middle of the tray (3).
3. The tower precondensation reactor according to claim 1, wherein the top of the baffle plate (4) is provided with an overflow port (16), and the overflow port (16) comprises a notch (18) and a bent guide vane (17), and the bending direction is towards one side of the adjacent shorter baffle plate.
4. A tower-type prepolycondensation reactor according to claim 3 characterized in that the overflow (16) on the highest baffle (4) comprises two guide vanes (17) and a notch (18) facing opposite directions when the baffle is located in the middle of the tray (3).
5. A tower precondensation reactor according to claim 1, characterized in that a baffle is arranged above the layer of vacuum ports if the layer of liquid-lowering ports (5) is located at the vacuum tube (2).
6. Tower precondensation reactor according to claim 1, wherein the top of the vacuum tube (2) is provided with a cap (15).
7. A tower precondensation reactor according to claim 1, wherein a heating coil is arranged at the bottom of each tray (3).
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| CN202011250773.7A CN114534624B (en) | 2020-11-11 | 2020-11-11 | Tower type precondensation reactor |
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| CN202011250773.7A CN114534624B (en) | 2020-11-11 | 2020-11-11 | Tower type precondensation reactor |
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| CN114534624B true CN114534624B (en) | 2024-04-19 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| DE10246251A1 (en) * | 2002-10-02 | 2004-04-15 | Zimmer Ag | Continuous production of polyesters by the (trans)esterification of dicarboxylic acids, comprises use of a vertical reactor having three reaction zones with a pressure of 10-40% of the diol equilibrium pressure |
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| CN2537445Y (en) * | 2002-03-28 | 2003-02-26 | 屈一新 | Atmospheric polymerization reactor |
| CN1743356A (en) * | 2004-08-07 | 2006-03-08 | 齐默股份公司 | Method and device for the continuous prepolycondensation of esterification/reesterification products |
| CN101837276A (en) * | 2010-03-24 | 2010-09-22 | 华东理工大学 | Novel flow-field structurized falling film polycondensation reactor and application thereof |
| CN102451660A (en) * | 2011-05-06 | 2012-05-16 | 上海聚友化工有限公司 | Downflow type pre-polymerization tower |
| CN103041763A (en) * | 2013-01-17 | 2013-04-17 | 扬州惠通化工技术有限公司 | Vertical non-stirring polycondensation reactor |
| CN204932917U (en) * | 2015-09-01 | 2016-01-06 | 云南大为恒远化工有限公司 | Extractive distillation device in a kind of hydrofining process of crude benzene |
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