CN211189219U - Settling tank for continuously removing falling powder of palladium-carbon catalyst - Google Patents
Settling tank for continuously removing falling powder of palladium-carbon catalyst Download PDFInfo
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- CN211189219U CN211189219U CN201921456626.8U CN201921456626U CN211189219U CN 211189219 U CN211189219 U CN 211189219U CN 201921456626 U CN201921456626 U CN 201921456626U CN 211189219 U CN211189219 U CN 211189219U
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Abstract
The settling tank for continuously removing the palladium-carbon catalyst falling powder comprises a shell, wherein the upper part of the shell is a transverse columnar cylinder, the lower part of the shell is a longitudinal circular cylinder, and a cylinder opening at the upper part of the longitudinal circular cylinder is communicated with the inside of the transverse columnar cylinder; the cylindrical barrel is provided with a settling tank feeding hole, an overflow hole is formed in the cylindrical barrel and away from the settling tank feeding hole, and a feeding hole guide plate, a longitudinal circular barrel upper barrel opening front guide plate, a longitudinal circular barrel upper barrel opening middle guide plate, a longitudinal circular barrel upper barrel opening rear guide plate and an overflow plate are sequentially arranged in the cylindrical barrel; the feed inlet guide plate, the front guide plate and the rear guide plate are sealed with the upper part of the interior of the columnar cylinder, and a channel for fluid to pass through is reserved between the feed inlet guide plate, the front guide plate and the rear guide plate and the lower part of the interior of the columnar cylinder; the height of the upper end edge of the middle guide plate is not lower than that of the upper end edge of the overflow plate; the overflow plate is positioned between the rear guide plate and the overflow outlet; the bottom of the longitudinal round cylinder is provided with a liquid outlet.
Description
Technical Field
The utility model relates to a subsider of continuous desorption palladium carbon catalyst powder falling
Background
Terephthalic Acid (PTA) is one of aromatic dicarboxylic acids, and is white needle-like crystal or powder at normal temperature, sublimes at about 300 deg.C, and has a spontaneous combustion point of 680 deg.C. It is soluble in hot ethanol, slightly soluble in water, insoluble in diethyl ether, glacial acetic acid and chloroform, low toxic, and inflammable. Terephthalic acid has wide application, is mainly used for producing polyester resin, polyester fiber, films, insulating paint, engineering plastics, plasticizers, dye intermediates, polyester chips, long and short polyester fibers, poultry feed additives and the like, and is an important industrial chemical. Terephthalic acid and Ethylene Glycol (EG) are polycondensed to obtain polyethylene terephthalate (PET) which is used as a polyester fiber raw material. The growth rate of Purified Terephthalic Acid (PTA) in the main raw materials of the three synthetic fibers is the largest and is about 3-4 times of that of other raw materials, and with the increase of PET requirements, the development of PTA production technology as the main raw material attracts wide attention.
As the main production raw material of the polyester industry, PTA has not been produced by a new PTA industrial production process in the last 10 years, but the original PTA production process technology is greatly improved. The domestic current PTA production process mainly comes from the patent technologies of several companies, such as Amoco-BP, Mitsui oiling, empire chemical (ICI) and Islaman. Among these PTA processes, Amoco high-temperature oxidation and its derivative process are the most widely used processes at present, and the PTA productivity accounts for more than 90% of the total production capacity. The process comprises two steps of oxidation and refining, wherein in the oxidation step, acetic acid is used as a solvent, cobalt acetate and manganese acetate are used as catalysts, hydrogen bromide or tetrabromoethane is used as an accelerator, air or oxygen-enriched air is introduced, and PX is oxidized at a high-temperature liquid phase to obtain an oxidation product, namely crude TA slurry. The crude TA slurry comprises components such as PTA, acetic acid, cobalt acetate, manganese acetate, hydrogen bromide or tetrabromoethane, p-carboxybenzaldehyde (4-CBA), p-toluic acid (PT acid), benzoic acid (BA acid) and the like, in order to recover acetic acid, catalyst and accelerant therein and properly reduce the impurity content therein, crystallization, separation and drying unit operations are also adopted, and finally crude TA powder is obtained and enters a refining unit bin with buffering and storing functions between oxidation and refining;
in the refining procedure, the coarse TA powder is pulped from a refining unit bin and a circulating solvent water conveying proportioning tank, and the designed concentration of TA slurry is about 25-32 wt%. The residence time of the slurry in the slurry tank is 10-20 minutes in order to buffer the fluctuations of the solid feed. The dosing tank is operated at 80-90 ℃ under normal pressure. The reaction feed is heated by five feed preheaters and two feed heaters which are connected in series, the preheater uses the flash steam of the crystallizer as a heat source, the heater uses 9MPa steam as a heat source, the normal inlet temperature of the hydrogenation reactor is 275-295 ℃, and the crude TA is fully dissolved in water at the high temperature.
After dissolved TA and high-pressure hydrogen flow enter from the top of the reactor, the dissolved TA and high-pressure hydrogen flow pass through a 4-8 mesh flaky Pd/C catalyst, and under the action of the catalyst, the 'key impurity' 4-CBA which mainly affects the polymerization performance and is close to the solubility of PTA in water is subjected to hydrogenation reaction with the PTA to generate PT acid with a great difference with the solubility of PTA in water, wherein the 4-CBA hydrogenation reaction process is as follows:
the effluent from the hydrogenation reactor (high PT acid, low 4-CBA) will be further refined in the subsequent units. Sequentially flowing into a first crystallizer, a second crystallizer, a third crystallizer, a fourth crystallizer and a fifth crystallizer, respectively separating 70%, 20%, 5% and 4.5% of PTA crystals in the first crystallizer, the second crystallizer, the third crystallizer and the fourth crystallizer, performing solid-liquid separation on slurry discharged from the fifth crystallizer by a refining centrifugal separation system, pulping and mixing filter cakes containing a small amount of PT acid, discharging the mixture to a re-pulping tank, and then feeding the mixture to a PTA rotary vacuum filter for filtering. And the filter cake is blown dry by the rotary drum through back blowing and then enters the next drying procedure.
As one of the core devices for PTA production, hydrogenation reactors generally adopt the structure and form as mentioned in the technical information of polyester technology-introduced polyester device (M), Beijing, chemical industry Press, 1 st edition of 06 months 1985, pages 318 to 320. According to the functional division, the internal space of the hydrogenation reactor can be roughly divided into a gas-liquid feeding contact dissolution area, a liquid phase layer area and a catalyst bed area from top to bottom, the catalyst bed area is provided with a flange for discharging the catalyst, a reaction product outlet and a Johnson pipe (namely a forced filter screen) for preventing the catalyst from passing through, and the gas-liquid feeding contact dissolution area is provided with a reactor top cover (provided with an emergency discharge port and a thermometer port) for filling the catalyst, a liquid inlet pipe and a distributor thereof and a hydrogen inlet pipe which are connected by the flange.
In the prior art, a crude TA hydrogenation reactor is mainly a crude TA hydrogenation reactor. The method comprises the steps of adding crude TA-water slurry after heating and temperature rising dissolution from a spray (distributor) connected with a liquid inlet pipe at the top of a hydrogenation reactor, introducing hydrogen from a hydrogen inlet pipe at the top of the hydrogenation reactor, enabling the slurry to flow through a fixed bed formed by palladium-carbon catalysts from top to bottom after the slurry is saturated and dissolved with the hydrogen, arranging a forced filter screen at the bottom of the reactor to prevent the palladium-carbon catalysts in the fixed bed from being brought out by reaction products to cause a series of adverse effects (such as catalyst loss, pipeline blockage, PET polymerization influence and the like), directly feeding the hydrogenated material into a subsequent multistage crystallization, washing and drying unit, and finally carrying out the PET polymerization. However, the existing crude TA hydrogenation reaction device at least has the following defects:
1. in the process of filling the palladium-carbon catalyst, although a certain amount of pure water is added in advance in the hydrogenation reactor to buffer friction and impact between the palladium-carbon catalyst and the inner wall of the hydrogenation reactor and between the palladium-carbon catalyst, a large amount of concentrated palladium-carbon catalyst powder falling is still inevitably caused, in order to avoid the palladium-carbon catalyst powder falling entering the subsequent process, a large amount of pure water is usually adopted to wash a palladium-carbon catalyst bed layer before starting and feeding, generally, the washing time is 8-24 hours and varies according to the powder falling condition in the washing water, so that the yield and the energy consumption of the device are influenced, and a large amount of waste water containing the powder falling is also generated.
2. Even if a large amount of pure water is adopted to wash the palladium-carbon catalyst bed layer before starting and feeding, continuous and small amount of palladium-carbon catalyst powder falling is inevitably caused due to factors such as fluid scouring and bed layer vibration in the starting and feeding process, and the palladium-carbon catalyst powder falling enters the subsequent process to cause the blockage of a washing filter screen and influence the PEN polymerization.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is that current thick TA hydrogenation device is at the initial stage of driving, and "powder falling" phenomenon can not be avoided appearing in the catalyst bed, and among the active carbon powder entered into the PTA thick liquids, lead to follow-up filtration washing filter cloth (net) to block up and influence the technical problem of PET polymerization performance index, technical scheme as follows:
the settling tank for continuously removing the palladium-carbon catalyst falling powder comprises a shell (1), wherein the upper part of the shell is a transverse cylindrical barrel (13), the lower part of the shell is a longitudinal cylindrical barrel (11), and a barrel opening at the upper part of the longitudinal cylindrical barrel is communicated with the inside of the transverse cylindrical barrel; the transverse cylindrical barrel (13) is provided with a settling tank feeding port (12), and an overflow port (16) is arranged on the transverse cylindrical barrel (13) and away from the settling tank feeding port (12); a feed inlet guide plate (2), a longitudinal circular cylinder upper cylinder opening front guide plate (7), a longitudinal circular cylinder upper cylinder opening middle guide plate (4), a longitudinal circular cylinder upper cylinder opening rear guide plate (5) and an overflow plate (6) are sequentially arranged in the transverse columnar cylinder (13); the feed inlet guide plate (2), the longitudinal circular cylinder upper barrel opening preposed guide plate (7) and the longitudinal circular cylinder upper barrel opening postpositive guide plate (5) are sealed with the upper part of the inner part of the transverse cylindrical barrel (13), and the feed inlet guide plate (2), the longitudinal circular cylinder upper barrel opening preposed guide plate (7) and the longitudinal circular cylinder upper barrel opening postpositive guide plate (5) and the lower part of the inner part of the transverse cylindrical barrel (13) are provided with a channel for fluid to pass through; the upper end edge of the middle position guide plate (4) at the upper cylinder opening of the longitudinal circular cylinder is not lower than the height of the upper end edge of the overflow plate (6); the overflow plate (6) is positioned between a rear guide plate (5) at the upper cylinder opening of the longitudinal circular cylinder and the overflow outlet (16); and a liquid outlet (9) is formed at the bottom of the longitudinal circular cylinder.
Compared with the common settling tank shown in figure 4, the utility model has the advantages that as the feed inlet guide plate (2), the front guide plate (7) at the upper part of the vertical circular cylinder and the rear guide plate (5) at the upper part of the vertical circular cylinder are arranged in the horizontal cylindrical cylinder (13), the hydrogenated PTA slurry containing the fallen powder enters the settling tank for continuously removing the fallen powder of the palladium-carbon catalyst from the feed inlet (12) of the settling tank, under the combined action of the feed inlet guide plate (2), the front guide plate (7) at the upper part of the vertical circular cylinder, the middle guide plate (4) at the upper part of the vertical circular cylinder and the rear guide plate (5) at the upper part of the vertical circular cylinder, the fallen powder is more easily and thoroughly separated from the hydrogenated PTA slurry and falls into the bottom of the vertical circular cylinder (11), so as to achieve the purpose of continuously removing the fallen powder of the palladium-carbon catalyst, avoids influencing the blockage of the subsequent filtering and washing filter cloth (net) and the PET polymerization performance index.
In the above technical solution, it is preferable that the horizontal cylindrical tube (13) is provided with an air inlet (3) and the vertical cylindrical tube (11) which are divided into a lower discharge chamber (14) by a filter layer (10). The filter layer (10) is preferably a filter screen, preferably a metal screen, the pore size of which is set to allow the slurry to pass through while retaining catalyst fines.
The filter layer (10) divides the lower discharge chamber (14) to obtain a hydrogenated PTA slurry from which the 'dust falling' is removed from the discharge chamber (14). And due to the arrangement of the air inlet (3), after more powder falls are accumulated above the filter layer (10), the pressure is applied to the mixture of the powder fall and the slurry above the filter layer (10) by closing the feeding hole (12) and the overflow hole (16) of the settling tank and introducing compressed gas through the air inlet (3), so that the powder fall and the slurry are fully separated, and the part of the slurry is recovered.
In the above technical solution, preferably, the filter layer (10) is clamped and fixed by a flange (8). Through the structure, the filter layer (10) divides the structure of the lower liquid discharge chamber (14), so that hydrogenated PTA slurry without fallen powder can be obtained from the liquid discharge chamber (14), and when the catalyst fallen powder is accumulated to a certain degree above the filter layer (10), the pressure is applied to the mixture of the fallen powder and the slurry above the filter layer (10) by closing the feeding hole (12) of the settling tank, the overflow hole (16) and introducing compressed gas through the gas inlet (3), so that the fallen powder and the slurry can be sufficiently separated, and the part of the slurry can be recovered. And then the filter layer (10) is cleaned after the falling powder is unloaded through the disassembling flange.
In the technical scheme, the powder falling discharge port (17) is preferably arranged on the wall of the longitudinal circular cylinder (11) close to the filter layer (10). The arrangement of the powder drop outlet (17) facilitates the discharge of the accumulated powder drop without having to detach the filter layer (10) from the longitudinal cylinder (11). Those skilled in the art will appreciate that the powder drop outlet (17) is preferably provided with a removable blind plate. The powder falling discharge port (17) is normally closed in the actual use process, and only when the powder falling accumulates to a certain degree in the filter layer (10), the powder falling discharge port (16) is arranged relative to the feeding port (12) of the settling tank, and compressed gas is introduced through the gas inlet (3) to apply pressure to the mixture of the powder falling and the slurry above the filter layer (10), so that the powder falling and the slurry are fully separated to recover the part of the slurry. Then washing water is reversely introduced through a liquid outlet (9), and falling powder is discharged through a powder falling outlet (17) and the filter layer (10) is cleaned.
In the above technical solution, preferably, the transverse cylindrical barrel (13) is a square barrel or a circular barrel.
In the technical solution, the volume ratio of the longitudinal circular cylinder (11) to the transverse cylindrical cylinder (13) is preferably a, and a is 0.5 to 1, for example, but not limited to, a may be 0.55, 0.60, 0.65, 0.70, 0.75, 0.8, 0.85, 0.9, 0.95, and the like; more preferably 0.65 to 0.9, most preferably 0.75 to 0.8.
In the above technical solution, the volume ratio of the drainage chamber (14) to the precipitation chamber (15) is preferably b, and b is 0.05 to 0.5, for example, but not limited to, b may be 0.055, 0.060, 0.065, 0.070, 0.075, 0.080, 0.085, 0.090, 0.095, 0.10, 0.15, 0.20, 0.25, 0.30, 0.35, 0.40, 0.45, or the like; more preferably 0.075 to 0.3, most preferably 0.1 to 0.25.
In the above technical scheme, the filtering layer (10) is preferably a metal mesh, a porous plate, a filter cloth or a porous filler.
In the above technical solution, preferably, the ratio of the area of the feed inlet baffle (2), the front baffle (7) at the upper cylinder mouth of the longitudinal circular cylinder and the area of the rear baffle (5) at the upper cylinder mouth of the longitudinal circular cylinder to the area of the passage for the fluid to pass through below the inside of the transverse cylindrical cylinder (13) to the cross-sectional area of the transverse cylindrical cylinder (13) is c, and c is 0.05 to 0.6, for example, but not limited to, c may be 0.055, 0.060, 0.065, 0.070, 0.075, 0.080, 0.085, 0.090, 0.095, 0.10, 0.15, 0.20, 0.25, 0.30, 0.35, 0.40, 0.45, 0.50, 0.55, and the like; more preferably 0.075 to 0.45, and most preferably 0.1 to 0.3.
In the above technical solution, the height ratio of the overflow plate (6) to the middle baffle (4) at the upper nozzle of the longitudinal cylinder is preferably d, where d is 0.5 to 1.0, and for example, but not limited thereto, d may be 0.55, 0.60, 0.65, 0.70, 0.75, 0.80, 0.85, 0.90, 0.95, or the like; more preferably 0.65 to 0.95, most preferably 0.8 to 0.9.
Drawings
FIG. 1 is a schematic diagram of a first embodiment of a settling tank for continuously removing falling palladium-carbon catalyst powder.
FIG. 2 is a schematic diagram of a second embodiment of the settling tank for continuously removing the falling powder of the palladium-carbon catalyst.
FIG. 3 is a schematic diagram of a third embodiment of the settling tank for continuously removing the falling powder of the palladium-carbon catalyst.
Fig. 4 is a schematic view of a conventional settling tank.
In fig. 1 to 4:
1 is a shell;
2 is a feed inlet guide plate;
3 is an air inlet;
4 is a middle guide plate at the upper cylinder opening of the longitudinal circular cylinder;
5 is a guide plate arranged at the rear part of the upper cylinder opening of the longitudinal circular cylinder;
6 is an overflow plate;
7 is a front guide plate at the upper cylinder mouth of the longitudinal circular cylinder;
8 is a flange;
9 is a liquid outlet;
10 is a filter layer;
11 is a longitudinal circular cylinder;
12 is a feed inlet of the settling tank;
13 is a transverse columnar cylinder;
14 is a drainage chamber;
15 is a settling chamber;
16 is an overflow outlet;
and 17 is a powder falling outlet.
Detailed Description
The first embodiment of the present invention
As shown in fig. 1.
A settling tank for continuously removing palladium-carbon catalyst falling powder comprises a shell (1), wherein the upper part of the shell is a transverse cylindrical barrel (13), the lower part of the shell is a longitudinal cylindrical barrel (11), the transverse cylindrical barrel (13) is provided with a settling tank feed inlet (12), an overflow outlet (16) is arranged in the transverse cylindrical barrel (13) and away from the settling tank feed inlet (12), a feed inlet guide plate (2), a longitudinal cylindrical barrel upper barrel opening front guide plate (7), a longitudinal cylindrical barrel upper barrel opening middle guide plate (4), a longitudinal cylindrical barrel upper barrel opening rear guide plate (5) and an overflow plate (6) are arranged in the transverse cylindrical barrel (13), the feed inlet guide plate (2), the longitudinal cylindrical barrel upper barrel opening front guide plate (7) and the longitudinal cylindrical barrel upper barrel opening rear guide plate (5) are sealed with the upper part of the transverse cylindrical barrel (13), a channel for fluid to pass is reserved below the inner part of the transverse cylindrical barrel (13) by the feed inlet guide plate (2), the front guide plate (7) of the upper barrel opening of the longitudinal circular barrel and the rear guide plate (5) of the upper barrel opening of the longitudinal circular barrel, and the upper end edge of the middle guide plate (4) in the upper barrel opening of the longitudinal circular barrel is not lower than the height of the upper end edge of the overflow plate (6). The overflow plate (6) is positioned between the rear guide plate (5) at the upper cylinder opening of the longitudinal circular cylinder and the overflow outlet (16); the bottom of the longitudinal round cylinder is provided with a liquid outlet (9).
The transverse cylindrical barrel (13) is a circular barrel.
The volume ratio of the longitudinal circular cylinder (11) to the transverse cylindrical cylinder (13) is a, and a is 0.75-0.8.
Feed inlet guide plate (2), leading guide plate of vertical circular cylinder upper portion tube mouth (7) and the rearmounted guide plate of vertical circular cylinder upper portion tube mouth (5), and the area and the horizontal cylindrical section of thick bamboo (13) cross sectional area ratio that the inside below of horizontal cylindrical section of thick bamboo (13) left the passageway that supplies the fluid to pass through are c, and c is 0.1 ~ 0.3.
The height ratio of the overflow plate (6) to the middle guide plate (4) at the upper cylinder opening of the longitudinal circular cylinder is d, and d is 0.8-0.9.
The hydrogenated PTA slurry without the fallen powder overflows from the upper end edge of the overflow plate (6) and flows out through an overflow outlet (16) to enter the subsequent process, and the hydrogenated PTA slurry enriched with the fallen powder is periodically discharged from a liquid discharge port (9).
Compared with the common settling tank shown in fig. 4, the first embodiment of the invention is characterized in that a feed inlet guide plate (2), a longitudinal circular cylinder upper barrel opening front guide plate (7), a longitudinal circular cylinder upper barrel opening middle guide plate (4), a longitudinal circular cylinder upper barrel opening rear guide plate (5) are arranged inside a transverse cylindrical barrel (13), hydrogenated PTA slurry containing 'powder falling' enters the settling tank for continuously removing Pd-C catalyst powder falling from a settling tank feed inlet (12), under the combined action of the feed inlet guide plate (2), the longitudinal circular cylinder upper barrel opening front guide plate (7), the longitudinal circular cylinder upper barrel opening middle guide plate (4) and the longitudinal circular cylinder upper barrel opening rear guide plate (5), the 'powder falling' is easier and more thoroughly separated from the hydrogenated PTA slurry and falls into the bottom of the longitudinal circular cylinder (11), the 'powder falling down' into the bottom of the longitudinal circular cylinder (11) is periodically discharged, so that the aim of continuously removing the powder falling down of the palladium-carbon catalyst is fulfilled, and the phenomena that the subsequent filtering and washing filter cloth (net) is blocked and the PET polymerization performance index is influenced are avoided.
The second embodiment of the present invention
As shown in fig. 2.
A settling tank for continuously removing palladium-carbon catalyst falling powder comprises a shell (1), wherein the upper part of the shell is a transverse cylindrical barrel (13), the lower part of the shell is a longitudinal cylindrical barrel (11), the transverse cylindrical barrel (13) is provided with a settling tank feed inlet (12), an overflow outlet (16) is arranged in the transverse cylindrical barrel (13) and away from the settling tank feed inlet (12), a feed inlet guide plate (2) is arranged in the transverse cylindrical barrel (13), a longitudinal cylindrical barrel upper barrel opening preposed guide plate (7), a longitudinal cylindrical barrel upper barrel opening middle guide plate (4), a longitudinal cylindrical barrel upper barrel opening postpositive guide plate (5) and an overflow plate (6), the feed inlet guide plate (2), the longitudinal cylindrical barrel upper barrel opening preposed guide plate (7) and the longitudinal cylindrical barrel upper barrel opening postpositive guide plate (5) are sealed with the upper part of the transverse cylindrical barrel (13), and the feed inlet guide plate (2) and the longitudinal cylindrical, A front guide plate (7) at the upper cylinder opening of the longitudinal circular cylinder and a rear guide plate (5) at the upper cylinder opening of the longitudinal circular cylinder are provided with a channel for fluid to pass through with the inner lower part of the transverse cylindrical cylinder (13), and the upper end edge of a middle guide plate (4) at the upper cylinder opening of the longitudinal circular cylinder is not lower than the height of the upper end edge of an overflow plate (6). The overflow plate (6) is positioned between the rear guide plate (5) at the upper cylinder opening of the longitudinal circular cylinder and the overflow outlet (16); the bottom of the longitudinal round cylinder is provided with a liquid outlet (9).
The transverse cylindrical barrel (13) is provided with an air inlet (3) and a longitudinal circular barrel (11) which are divided into a lower liquid discharge chamber (14) through a filter layer (10).
The filter layer (10) is clamped and fixed through the flange (8).
The transverse cylindrical barrel (13) is a circular barrel.
The volume ratio of the longitudinal circular cylinder (11) to the transverse cylindrical cylinder (13) is a, and a is 0.75-0.8.
The volume ratio of the drainage chamber (14) to the precipitation chamber (15) is b, and b is 0.1-0.25.
The filter layer (10) is a metal net.
The area of a channel for fluid to pass through is reserved below the inner parts of the feed inlet guide plate (2), the front guide plate (7) of the upper cylinder opening of the longitudinal circular cylinder, the rear guide plate (5) of the upper cylinder opening of the longitudinal circular cylinder and the transverse cylindrical cylinder (13), and the area ratio of the cross section area of the transverse cylindrical cylinder (13) is c, wherein the c is 0.1-0.3.
The height ratio of the overflow plate (6) to the middle guide plate (4) at the upper cylinder opening of the longitudinal circular cylinder is d, and d is 0.8-0.9.
The hydrogenated PTA slurry without the fallen powder overflows from the upper end edge of the overflow plate (6) and flows out through an overflow outlet (16) to enter the subsequent process, and the hydrogenated PTA slurry enriched with the fallen powder periodically adopts the following operations: the feed inlet (12) and the overflow outlet (16) of the settling tank are closed, compressed gas is introduced through the gas inlet (3), pressure is applied to the mixture of the falling powder and the slurry above the filter layer (10), and the falling powder and the slurry are fully separated to recover the part of the slurry. And unloading the dropped powder through a disassembling flange (8) and cleaning the metal mesh of the filter layer (10).
Compared with the common settling tank shown in fig. 4, the second embodiment of the invention is characterized in that a feed inlet guide plate (2), a longitudinal circular cylinder upper barrel opening front guide plate (7), a longitudinal circular cylinder upper barrel opening middle guide plate (4), a longitudinal circular cylinder upper barrel opening rear guide plate (5) are arranged inside a transverse cylindrical barrel (13), hydrogenated PTA slurry containing 'powder falling' enters the settling tank for continuously removing Pd-C catalyst powder falling from a settling tank feed inlet (12), under the combined action of the feed inlet guide plate (2), the longitudinal circular cylinder upper barrel opening front guide plate (7), the longitudinal circular cylinder upper barrel opening middle guide plate (4) and the longitudinal circular cylinder upper barrel opening rear guide plate (5), the 'powder falling' is easier and more thoroughly separated from the hydrogenated PTA slurry and falls into the upper part of a filter layer (10) metal mesh, and the 'powder falling' enriched hydrogenation PTA slurry can be divided into hydrogenation PTA slurry without 'powder falling' and 'powder falling' to be discharged periodically, so that the aim of continuously removing the powder falling of the palladium-carbon catalyst is fulfilled, and the phenomena that the subsequent filtration and washing filter cloth (net) is blocked and the PET polymerization performance index is influenced are avoided.
The third embodiment of the present invention
As shown in fig. 3.
A settling tank for continuously removing palladium-carbon catalyst falling powder comprises a shell (1), wherein the upper part of the shell is a transverse cylindrical barrel (13), the lower part of the shell is a longitudinal cylindrical barrel (11), the transverse cylindrical barrel (13) is provided with a settling tank feed inlet (12), an overflow outlet (16) is arranged in the transverse cylindrical barrel (13) and away from the settling tank feed inlet (12), a feed inlet guide plate (2) is arranged in the transverse cylindrical barrel (13), a longitudinal cylindrical barrel upper barrel opening preposed guide plate (7), a longitudinal cylindrical barrel upper barrel opening middle guide plate (4), a longitudinal cylindrical barrel upper barrel opening postpositive guide plate (5) and an overflow plate (6), a feed inlet guide plate (2), a longitudinal cylindrical barrel upper barrel opening preposed guide plate (7), a longitudinal cylindrical barrel upper barrel opening postpositive guide plate (5) are sealed with the upper part of the transverse cylindrical barrel (13), and the feed inlet of the guide plate (2) is sealed, A front guide plate (7) at the upper cylinder opening of the longitudinal circular cylinder and a rear guide plate (5) at the upper cylinder opening of the longitudinal circular cylinder are provided with a channel for fluid to pass through with the inner lower part of the transverse cylindrical cylinder (13), and the upper end edge of a middle guide plate (4) at the upper cylinder opening of the longitudinal circular cylinder is not lower than the height of the upper end edge of an overflow plate (6). The overflow plate (6) is positioned between the rear guide plate (5) at the upper cylinder opening of the longitudinal circular cylinder and the overflow outlet (16); the bottom of the longitudinal round cylinder is provided with a liquid outlet (9).
The transverse cylindrical barrel (13) is provided with an air inlet (3) and a longitudinal circular barrel (11) which are divided into a lower liquid discharge chamber (14) through a filter layer (10).
The filter layer (10) is clamped and fixed through the flange (8).
The transverse cylindrical barrel (13) is a circular barrel.
The volume ratio of the longitudinal circular cylinder (11) to the transverse cylindrical cylinder (13) is a, and a is 0.75-0.8.
The volume ratio of the drainage chamber (14) to the precipitation chamber (15) is b, and b is 0.1-0.25.
The filter layer (10) is a metal net.
Feed inlet guide plate (2), leading guide plate of vertical circular cylinder upper portion tube mouth (7) and the rearmounted guide plate of vertical circular cylinder upper portion tube mouth (5), and the area and the horizontal cylindrical section of thick bamboo (13) cross sectional area ratio that the inside below of horizontal cylindrical section of thick bamboo (13) left the passageway that supplies the fluid to pass through are c, and c is 0.1 ~ 0.3.
The height ratio of the overflow plate (6) to the middle guide plate (4) at the upper cylinder opening of the longitudinal circular cylinder is d, and d is 0.8-0.9.
A powder falling outlet (17) is arranged at the bottom of the settling chamber (15) close to the filter layer (10).
The hydrogenated PTA slurry without the fallen powder overflows from the upper end edge of the overflow plate (6) and flows out through an overflow outlet (16) to enter the subsequent process, and the hydrogenated PTA slurry enriched with the fallen powder periodically adopts the following operations: the feeding hole (12) and the overflow hole (16) of the settling tank are closed, the air inlet (3) is opened, the hydrogenated PTA slurry containing the fallen powder in the shell (1) is filtered by the filter layer (10), and the hydrogenated PTA slurry without the fallen powder is discharged from the liquid outlet (9). After the discharging is finished, the air inlet (3) is closed, pure water is connected through the liquid outlet (9) after the pressure is relieved, the metal mesh of the filter layer (10) is washed reversely, the powder falling outlet (17) is opened, the washing liquid containing the falling powder is discharged, and the filter layer (10) is cleaned.
Compared with the common settling tank shown in fig. 4, the third embodiment of the invention is characterized in that a feed inlet guide plate (2), a longitudinal circular cylinder upper barrel opening front guide plate (7), a longitudinal circular cylinder upper barrel opening middle guide plate (4), a longitudinal circular cylinder upper barrel opening rear guide plate (5) are arranged inside a transverse cylindrical barrel (13), hydrogenated PTA slurry containing 'powder falling' enters the settling tank for continuously removing Pd-C catalyst powder falling from a settling tank feed inlet (12), under the common action of the feed inlet guide plate (2), the longitudinal circular cylinder upper barrel opening front guide plate (7), the longitudinal circular cylinder upper barrel opening middle guide plate (4) and the longitudinal circular cylinder upper barrel opening rear guide plate (5), the 'powder falling' is easier and more thoroughly separated from the PTA slurry and falls into the upper part of the filter layer (10) metal mesh, the method can divide the hydrogenation PTA slurry enriched with the fallen powder into the hydrogenation PTA slurry without the fallen powder and the fallen powder to be discharged periodically, and the metal net of the filter layer (10) is not required to be disassembled, so that the metal net of the filter layer (10) is directly cleaned, the purpose of continuously removing the fallen powder of the palladium-carbon catalyst is more effectively achieved, and the filter cloth (net) blockage of subsequent filtering and washing and the influence on the PET polymerization performance index are avoided.
Implementation of the conventional technology
As shown in fig. 4.
The difference of the utility model is that the device does not comprise a feed inlet guide plate (2), a front guide plate (7) of a cylinder opening on the upper part of a vertical circular cylinder, a middle guide plate (4) of a cylinder opening on the upper part of a vertical circular cylinder, a rear guide plate (5) of a cylinder opening on the upper part of a vertical circular cylinder, a filter layer (10), an air inlet (3), a flange (8) and a powder discharge port (17).
The method specifically comprises the following steps:
a common settling tank comprises a shell (1), wherein the upper part of the shell is a transverse cylindrical barrel (13), the lower part of the shell is a longitudinal circular barrel (11), the transverse cylindrical barrel (13) is provided with a settling tank feed inlet (12), and an overflow outlet (16) is arranged on the transverse cylindrical barrel (13) away from the settling tank feed inlet (12).
The transverse cylindrical barrel (13) is a circular barrel.
The volume ratio of the longitudinal circular cylinder (11) to the transverse cylindrical cylinder (13) is a, and a is 0.75-0.8.
And a liquid discharge port (9) is arranged at the bottom of the longitudinal round cylinder (11).
Claims (18)
1. The settling tank for continuously removing the palladium-carbon catalyst falling powder comprises a shell (1), wherein the upper part of the shell is a transverse cylindrical barrel (13), the lower part of the shell is a longitudinal cylindrical barrel (11), and a barrel opening at the upper part of the longitudinal cylindrical barrel is communicated with the inside of the transverse cylindrical barrel; the transverse cylindrical barrel (13) is provided with a settling tank feeding port (12), and an overflow port (16) is arranged on the transverse cylindrical barrel (13) and away from the settling tank feeding port (12); a feed inlet guide plate (2), a longitudinal circular cylinder upper cylinder opening front guide plate (7), a longitudinal circular cylinder upper cylinder opening middle guide plate (4), a longitudinal circular cylinder upper cylinder opening rear guide plate (5) and an overflow plate (6) are sequentially arranged in the transverse columnar cylinder (13); the feed inlet guide plate (2), the longitudinal circular cylinder upper barrel opening preposed guide plate (7) and the longitudinal circular cylinder upper barrel opening postpositive guide plate (5) are sealed with the upper part of the inner part of the transverse cylindrical barrel (13), and a channel for fluid to pass through is reserved below the feed inlet guide plate (2), the longitudinal circular cylinder upper barrel opening preposed guide plate (7), the longitudinal circular cylinder upper barrel opening postpositive guide plate (5) and the inner part of the transverse cylindrical barrel (13); the upper end edge of the middle position guide plate (4) at the upper cylinder opening of the longitudinal circular cylinder is not lower than the height of the upper end edge of the overflow plate (6); the overflow plate (6) is positioned between a rear guide plate (5) at the upper cylinder opening of the longitudinal circular cylinder and the overflow outlet (16); and a liquid outlet (9) is formed at the bottom of the longitudinal circular cylinder.
2. The settler for continuous removal of fallen palladium-carbon catalyst as defined in claim 1, wherein said horizontal cylindrical drum (13) is provided with an air inlet (3) and said vertical cylindrical drum (11) is divided by a filter layer (10) into a lower effluent chamber (14).
3. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 2, wherein the filter layer (10) is held and fixed by a flange (8).
4. The settler for continuously removing the falling powder of palladium-carbon catalysts as claimed in claim 2, wherein the outlet (17) for the falling powder is arranged on the wall of the longitudinal cylinder (11) in the immediate vicinity of the filter layer (10).
5. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 1, wherein the transverse cylindrical barrel (13) is a square barrel or a round barrel.
6. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst, as claimed in claim 1, wherein the volume ratio of the longitudinal cylindrical barrel (11) to the transverse cylindrical barrel (13) is a, and a is 0.5-1.
7. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 6, wherein a is 0.65-0.9.
8. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 7, wherein a is 0.75-0.8.
9. The settling tank for continuously removing the palladium-carbon catalyst falling powder as claimed in claim 2, wherein the volume ratio of the drainage chamber (14) to the settling chamber (15) is b, and b is 0.05-0.5.
10. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 9, wherein b is 0.075-0.3.
11. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 10, wherein b is 0.1-0.25.
12. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 2, wherein the filter layer (10) is a metal mesh, a porous plate, a filter cloth or a porous filler.
13. The settling tank for continuously removing the palladium-carbon catalyst falling powder as claimed in claim 1, wherein the ratio of the area of the feed inlet guide plate (2), the front guide plate (7) at the upper cylinder opening of the longitudinal circular cylinder and the rear guide plate (5) at the upper cylinder opening of the longitudinal circular cylinder to the area of the channel for the fluid to pass through below the inner part of the transverse cylindrical cylinder (13) to the cross section area of the transverse cylindrical cylinder (13) is independently c, and c is 0.05-0.6.
14. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 13, wherein c is 0.075-0.45.
15. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 14, wherein c is 0.1-0.3.
16. The settling tank for continuously removing the palladium-carbon catalyst falling powder as claimed in claim 1, wherein the height ratio of the overflow plate (6) to the middle position guide plate (4) at the upper cylinder opening of the longitudinal circular cylinder is d, and d is 0.5-1.0.
17. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 16, wherein d is 0.65-0.95.
18. The settling tank for continuously removing the falling powder of the palladium-carbon catalyst as claimed in claim 17, wherein d is 0.8-0.9.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921456626.8U CN211189219U (en) | 2019-09-04 | 2019-09-04 | Settling tank for continuously removing falling powder of palladium-carbon catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921456626.8U CN211189219U (en) | 2019-09-04 | 2019-09-04 | Settling tank for continuously removing falling powder of palladium-carbon catalyst |
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| Publication Number | Publication Date |
|---|---|
| CN211189219U true CN211189219U (en) | 2020-08-07 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201921456626.8U Active CN211189219U (en) | 2019-09-04 | 2019-09-04 | Settling tank for continuously removing falling powder of palladium-carbon catalyst |
Country Status (1)
| Country | Link |
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| CN (1) | CN211189219U (en) |
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2019
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