CN113769665A - Reactor and method for removing small molecules at low temperature - Google Patents
Reactor and method for removing small molecules at low temperature Download PDFInfo
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- CN113769665A CN113769665A CN202010521925.6A CN202010521925A CN113769665A CN 113769665 A CN113769665 A CN 113769665A CN 202010521925 A CN202010521925 A CN 202010521925A CN 113769665 A CN113769665 A CN 113769665A
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- 150000003384 small molecules Chemical class 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 21
- 239000002245 particle Substances 0.000 claims abstract description 47
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 41
- 238000006243 chemical reaction Methods 0.000 claims abstract description 38
- 229920000728 polyester Polymers 0.000 claims abstract description 34
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 21
- 238000009826 distribution Methods 0.000 claims abstract description 14
- 239000007789 gas Substances 0.000 claims description 11
- 230000014759 maintenance of location Effects 0.000 claims description 6
- 239000003638 chemical reducing agent Substances 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 239000008187 granular material Substances 0.000 claims description 4
- 238000004321 preservation Methods 0.000 claims description 3
- 239000000498 cooling water Substances 0.000 claims description 2
- 238000013461 design Methods 0.000 abstract description 5
- 238000002156 mixing Methods 0.000 abstract description 5
- 238000012546 transfer Methods 0.000 abstract description 3
- IKHGUXGNUITLKF-UHFFFAOYSA-N Acetaldehyde Chemical compound CC=O IKHGUXGNUITLKF-UHFFFAOYSA-N 0.000 description 20
- 239000000463 material Substances 0.000 description 11
- 239000000428 dust Substances 0.000 description 7
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 6
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 6
- 239000007790 solid phase Substances 0.000 description 5
- HGINCPLSRVDWNT-UHFFFAOYSA-N Acrolein Chemical compound C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 229920000139 polyethylene terephthalate Polymers 0.000 description 4
- 239000005020 polyethylene terephthalate Substances 0.000 description 4
- 238000006116 polymerization reaction Methods 0.000 description 4
- 239000012798 spherical particle Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical compound [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- -1 Polyethylene terephthalate Polymers 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 235000013361 beverage Nutrition 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000007791 dehumidification Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000001746 injection moulding Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000006068 polycondensation reaction Methods 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 229920001169 thermoplastic Polymers 0.000 description 1
- 239000004416 thermosoftening plastic Substances 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
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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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
-
- 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
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/785—Preparation processes characterised by the apparatus used
Abstract
The invention discloses a reactor and a method for removing small molecules at low temperature, comprising a vertical two-section reactor, wherein the upper section of the reactor is a cylinder, the lower section of the reactor is an inverted cone, the tail end of the inverted cone is a reactor outlet, and the outlet is connected with an external cooler; the top of the reactor is provided with a feed inlet and an air outlet, and the reactor is also provided with a first air inlet and a second air inlet; the cylinder section is divided into a first reaction area and a second reaction area. According to the invention, the design of the flow distribution plate can realize plug flow in the particle conveying process, back mixing is not easy to cause, the hot nitrogen/air outlet pipe provides stable airflow to fully perform heat and mass transfer with the spherical polyester particles, and the efficiency of removing small molecules of the polyester particles is greatly improved.
Description
Technical Field
The invention relates to a reactor and a method for removing small molecules at low temperature.
Background
Polyethylene terephthalate (PET) is a semi-crystalline thermoplastic polyester that is widely used in the manufacture of fibers, films, sheets, and food trays and beverage containers. In the prior art, terephthalic acid (PTA) and Ethylene Glycol (EG) are used as main raw materials to prepare high-viscosity polyester, low-viscosity polyester with the intrinsic viscosity of about 0.65dl/g and the polymerization degree of about 100 is obtained through conventional liquid phase polymerization, and then high-viscosity polyester with the intrinsic viscosity of 0.80dl/g and the average polymerization degree of more than 135 is improved through a solid-phase tackifying process, so that the high-viscosity polyester meets the requirements of subsequent processing.
In polyester packaging products, besides intrinsic viscosity, the content of small molecules is another most important index, particularly acetaldehyde (AA), can permeate into packaged objects to produce adverse effects, and if food is packaged, the taste of food is directly influenced and health risks are caused to human bodies. The sources of acetaldehyde are mainly: in the liquid phase polymerization stage, part of AA with the content of about 100 mu g/g is formed due to high-temperature degradation reaction; partial side reactions occur in the solid phase tackifying stage, and a small amount of AA is produced. AA generated by the two sources can be basically removed in the solid-phase tackifying process, and the final AA content is not more than 1.0 mu g/g. Although the solid-phase tackifying technology is mature, hot nitrogen/air is usually adopted to remove small molecules in polyester solid particles and improve viscosity, the technology has the problems of high energy consumption and material consumption, uneven molecular weight distribution of PET products, much dust and the like. In the existing production technology, the liquid phase tackifying technology is to make PET reach higher intrinsic viscosity (generally above 0.78 dL/g) in a final polycondensation reactor, perform underwater crystallization, cutting and granulation, and then realize the preparation of a final polyester product through a micromolecule removing device. The preparation of polyester chips with low small molecular weight content aiming at the crystallized spherical particles obtained by liquid phase tackifying is of great importance in the structural design and process conditions of the reactor in the production flow.
At present, all existing reactors are designed by tower body structures of conventional cylindrical polyester particles, so that polyester chips fall unevenly by means of dead weight, the stacking density of the polyester particles is low, plug flow cannot be effectively formed, heat exchange is uneven, back mixing is easily caused, the existing tubular heat exchanger at a cooling section has a short cleaning period due to impurity precipitation, the removal efficiency of small molecules in the chips is low, and the replacement period of dust removal bags of a cooler is greatly influenced by the outside.
Disclosure of Invention
The purpose of the invention is as follows: the invention aims to provide a reactor and a method for removing small molecules at low temperature so as to solve the technical problems.
The technical scheme is as follows: the reactor for removing small molecules at low temperature comprises a vertical two-section reactor, wherein the upper section of the reactor is a cylinder, the lower section of the reactor is an inverted cone, the tail end of the inverted cone is a reactor outlet, and the outlet is connected with an external cooler; the top of the reactor is provided with a feed inlet and an air outlet, and the reactor is also provided with a first air inlet and a second air inlet; the cylinder section is divided into a first reaction area and a second reaction area; the first reaction zone is internally provided with a flow distribution plate and an air outlet pipe positioned on the central axis of the first reaction zone, the air outlet pipe is provided with a plurality of air outlets, and an inlet of the air outlet pipe is connected with a first air inlet through a pipeline; the second reaction zone is provided with a plurality of vertical channels, particles fall in the channels, and a certain gap is reserved in front of the channels.
The method for removing small molecules at low temperature of the invention is based on the reactor and comprises the following steps,
(1) spherical polyester particles enter a first reaction zone of the reactor from a feed inlet at the top of the reactor, and hot air or nitrogen is introduced from a first air inlet of the reactor to remove micromolecules in the particles;
(2) the polyester particles with most of small molecules removed enter a channel of a second reaction zone, and the small molecules in the particles are further removed through air or nitrogen of a second air inlet;
(3) the particles are discharged from the outlet and enter the next process.
The first reaction zone of the reactor in the step (1) passes through a jacket heat preservation device, the internal temperature is maintained at 190 ℃, the retention time is 15-40h, and the temperature of hot air or nitrogen is 160-190 ℃.
The temperature of the cooling water in the step (2) is less than or equal to 40 ℃, the circulating flow rate in the pipe is 1.0-2.0 m/s, and the residence time of the particles in the cooling section is not more than 3 hours.
The ratio of the amount of the particles in the steps (1) and (2) to the amount of the introduced air or nitrogen is 5-25.
Has the advantages that: compared with the prior art, the invention has the following remarkable advantages:
(1) the first reaction zone is provided with a hollow cylindrical hot nitrogen/air outlet pipe, and the air outlet pipe is connected with a hot nitrogen/air inlet pipe outside the tower through the bottom of the first reaction zone, so that stable airflow in the whole tower is provided to fully perform heat and mass transfer by forward and reverse collision with spherical polyester particles, and each particle can obtain the same contact opportunity.
(2) According to the invention, the circular coil splitter plate is nested at the top and the middle of the nitrogen outlet pipe, so that the uniformity of material distribution in the reactor is fully improved. The gas outlet is arranged on the splitter plate and matched with the gas inlet pipe, so that the contact area of the material and the gas is further increased, the splitter plate is particularly suitable for removing small molecules from granular materials, the problem of back mixing can be solved, the flat plug flow in the conveying process of the slice particles is realized, and the efficiency of removing the small molecules from the polyester slices can be greatly improved.
(3) The second reaction zone is vertically provided with a plurality of channels, the polyester particles descend from the circular tube pass by the dead weight, and the upper end of the tube pass is in an inverted cone shape and is in gapless connection with the tower wall. Ensuring that the particles enter the discharge port at a uniform speed, increasing the retention time, avoiding back mixing and playing a role in further removing small molecules. .
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a schematic view of the structure of the splitter plate of the present invention;
fig. 3 is a partial structural view of a in fig. 1.
Detailed Description
The technical scheme of the invention is further explained by combining the attached drawings.
As shown in fig. 1, the tower body of the reactor 2 of the present invention is designed in two vertical sections, including a cylindrical section 1 and an inverted cone section 3. The center of the top of the tower body is provided with a feed inlet 22 and a gas phase outlet 21, the tail end of the inverted cone at the lower end is provided with a reactor material outlet 23, and an external cooler is arranged below the material outlet 23. The cylindrical section is divided into a first reaction zone 10 and a second reaction zone 11. The diameter of the second reaction zone 11 is smaller than the diameter of the first reaction zone 10 in order to ensure that the material has different residence times in the two zones.
A hollow cylindrical hot nitrogen/air outlet pipe 103 is arranged at the central axis of the first reaction zone 10, the air outlet pipe 103 is connected with a first air inlet 105 through a pipeline at the bottom of the first reaction zone, the inlet air is nitrogen or air, a plurality of air outlets are arranged on the air outlet pipe 103, and the diameter of each air outlet is smaller than that of spherical polyester particles. The cylindrical outer wall of the tower body of the first reaction zone 10 is provided with a jacket heat preservation device which can maintain the temperature in the tower.
Be equipped with flow distribution plate 102 in reactor 1, the flow distribution plate nestification is outside air-out pipe 103, and the flow distribution plate is equipped with 1 layer at least. The splitter plate 102 has honeycomb-shaped holes, which are polygonal, such as hexagonal as shown in fig. 2, and are selected according to the required retention time and the particle diameter, and the inner diameter of the holes is not less than 500 times of the inner diameter of the spherical polyester particles.
The outer diameter of the air outlet pipe 103 is the minimum diameter of the inner ring of the circular coil splitter plate, and the joint of the air outlet pipe and the circular coil splitter plate has no dead angle. The upper and lower splitter plates 102 are welded and supported by cylindrical brackets, and the disks are also connected by the brackets. The ratio of the distance between the adjacent circular rings of the flow distribution plate to the diameter of the reactor is more than 1:11, and the thickness of the flow distribution plate is less than 100mm, preferably 30-100 mm.
The first air inlet 105 is also connected with a heat medium system 6, and the heat medium system 6 comprises a heat exchanger and a dryer, so that the drying of the inlet air can be further ensured, and the inlet air temperature is kept constant.
The second reaction zone 11 has a plurality of vertically disposed channels 111 through which the material particles fall by gravity or vibration. The material particles fall down in the channels with a certain gap in front of the adjacent channels. The junction of the passage of the second reaction zone 11 and the first reaction zone 10 is provided with a reducer 112 having an inverted cone shape, as shown in fig. 3.
A reducing pipe 4 is arranged in the inverted cone 3 at the lower section, and the reducing pipe 4 and the shell of the inverted cone 3 form an annular space which is in a double-top cone design. The shell of the inverted cone 3 is provided with a second gas inlet 31, the second gas inlet 31 is connected with the heat medium system 6, the position of the gas inlet corresponds to the annular space, dry air or nitrogen enters into the gap of the channel 111 in the second reaction zone through the annular gap generated by the cone, and particles fall from the reducer 4.
The method for removing the small molecules at low temperature by adopting the reactor comprises the following steps:
spherical polyester particles enter a first reaction zone at the first section of the tower body from a feed inlet at the top of the reactor, wherein the viscosity of the spherical polyester particles at the feed inlet is 0.70-0.80dL/g, the acetaldehyde content is 10-100 mu g/g, the formaldehyde content is 10-50 mu g/g, and the crystallinity is 30-40%. The particles fall to the circular coil pipe splitter plate by means of dead weight and then are split and descend, because the contact area among the spherical polyester particles is small, relative displacement is easy to occur, so that the speed in the falling process is uneven, the stacking density is smaller than that of the cylindrical particles, the design of the splitter plate can keep the descending speed of the middle and the edge of the spherical polyester particles balanced, the plug flow is effectively formed, stable airflow in the whole tower is provided in the hot nitrogen/air outlet pipe, the heat and mass transfer is fully carried out by forward and reverse collision of the spherical polyester particles, each particle can obtain the same contact opportunity, and therefore the micromolecule removal efficiency is improved. The micromolecules are formaldehyde, acetaldehyde, acrolein, benzene, toluene, ethylbenzene, xylene, styrene and the like. The temperature of the jacket of the cylinder is kept at 190 ℃ and 160 ℃ for 15-40 h.
Most of the small molecular polyester particles are removed and uniformly enter the second reaction zone, the upper end of the tube pass is in inverted cone shape and is in gapless connection with the tower wall, the spherical particles are ensured to keep uniform speed and enter the discharge port, the retention time is increased, and the small molecules are further removed from the material particles in the second reaction zone.
The cone at the lower section of the reactor adopts a double-top cone design, and simultaneously plays a role of a flow guide cone, so that the descending speed of spherical particles in the middle part and the edge of the reactor is balanced, and the back mixing of a discharge port is avoided. Dry air or nitrogen is continuously blown into the heat exchanger tube bundle through the annular gap generated by the cone, fully contacts with the spherical particles from top to bottom, and continuously discharges formaldehyde, acetaldehyde, acrolein gas and micromolecules in the tower body. The discharged materials are sent to an external cooler 5 for cooling.
The exhausted air/nitrogen can be recycled after dehumidification and catalyst absorption of moisture, formaldehyde, acetaldehyde and micromolecules. The ratio of the amount of the granules in the whole micromolecule removing process to the air/nitrogen is 5-25, wherein the temperature of the hot air/nitrogen is 160-190 ℃, and preferably 170-185 ℃. Because the reactor is internally provided with the splitter plate, the central air outlet pipe and the second reaction zone, and the splitter plate is honeycomb-shaped, the efficiency of removing small molecules can be increased, the process can be carried out at a temperature lower than the conventional temperature by 20 ℃, and the reactor is energy-saving and low-carbon.
The polyester particles prepared by the reactor have low micromolecule content, the dust content is lower than 10 mu g/g, the dust proportion is reduced by 80 percent compared with polyester slices produced by a conventional solid-phase tackifying device, the retention time is greatly shortened to 15-30 h, the internal and external viscosity difference of the particles is lower than 0.01dL/g, the molecular weight distribution is less than or equal to 2.2, and the post-processing injection molding temperature of a user is reduced by 10-15 ℃. Compared with the prior art, the reactor has the advantages of low energy consumption and material consumption, low equipment investment, uniform internal and external particle viscosity, less dust and high devolatilization efficiency.
The polyester granules produced by the above reactor, the dust was collected by a cyclone to obtain the dust content, and the molecular weight distribution and the formaldehyde and acetaldehyde contents were also measured with reference to the polyester test standard (GB17931-2003) and the results are shown in the following table:
Claims (13)
1. a reactor for removing micromolecules at low temperature is characterized by comprising a two-section reactor (2), wherein the upper section of the reactor is a cylindrical section (1), the lower section of the reactor is an inverted cone section (3), the tail end of the inverted cone section is provided with a discharge hole (23), and the discharge hole is connected with an external cooler (5); the top of the reactor (2) is provided with a feed inlet (22) and an air outlet (21), and the reactor is also provided with a first air inlet (105) and a second air inlet (31); the cylinder section (1) is divided into a first reaction zone (10) and a second reaction zone (11); a splitter plate (102) and an air outlet pipe (103) positioned on the central axis of the first reaction zone are arranged in the first reaction zone (10), a plurality of air outlets are arranged on the air outlet pipe, and an inlet of the air outlet pipe (103) is connected with a first air inlet (105) through a pipeline; the second reaction zone (11) is provided with a plurality of vertical channels (111) in which the particles fall with a certain gap in front of the channels.
2. The reactor for removing small molecules at low temperature according to claim 1, wherein the flow distribution plate (102) is provided with honeycomb-shaped holes.
3. The reactor for removing small molecules at low temperature as claimed in claim 2, wherein the inner diameter of the holes is more than or equal to 500 times of the inner diameter of the spherical polyester particles.
4. The reactor for low-temperature removal of small molecules as claimed in claim 1, wherein a reducer (112) with an inverted cone shape is arranged at the joint of the channel of the second reaction zone (11) and the first reaction zone (10).
5. The reactor for removing small molecules at low temperature as claimed in claim 1, wherein the first gas inlet (105) and the second gas inlet (31) are connected with a heat medium system (6), and the heat medium system comprises a heat exchanger and a dryer.
6. The reactor for removing small molecules at low temperature according to claim 1, wherein the flow distribution plate (102) is provided with at least two layers.
7. The reactor for removing small molecules at low temperature as claimed in claim 1, wherein the diameters of the air outlets of the air outlet pipes (103) are smaller than the diameter of the particles.
8. The reactor for low-temperature removal of small molecules as claimed in claim 1, wherein the thickness of the flow distribution plate (102) is less than 100 mm.
9. The reactor for low-temperature removal of small molecules as claimed in claim 1, wherein a reducer (4) is disposed in the inverted cone section (3), the reducer and the inverted cone section housing form an annular space, and the second gas inlet (31) is disposed on the inverted cone housing.
10. A method for removing small molecules at low temperature is based on the reactor of any one of claims 1 to 9, and is characterized by comprising the following steps,
(1) spherical polyester particles enter a first reaction zone of the reactor from a feed inlet at the top of the reactor, and hot air or nitrogen is introduced from a first air inlet of the reactor to remove micromolecules in the particles;
(2) the polyester particles with most of small molecules removed enter a channel of a second reaction zone, and the small molecules in the particles are further removed through air or nitrogen of a second air inlet;
(3) the granules are discharged from the outlet, cooled by an external cooler and then enter the next process.
11. The method for removing small molecules at low temperature as claimed in claim 10, wherein the first reaction zone of the reactor in step (1) is maintained at an internal temperature of 160-190 ℃ by a jacket heat preservation device, the retention time is 15-40h, and the temperature of hot air or nitrogen is 160-190 ℃.
12. The method for removing small molecules at low temperature according to claim 10, wherein the temperature of the cooling water in the step (2) is less than or equal to 40 ℃, the circulating flow rate in the pipe is 1.0-2.0 m/s, and the residence time of the particles in the cooling section is not more than 3 hours.
13. The method for removing small molecules at low temperature according to claim 10, wherein the ratio of the amount of the particles in the steps (1) and (2) to the amount of the introduced air or nitrogen is 5-25.
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Application publication date: 20211210 |