CN216063307U - Catalyst preparation drying tower and catalyst preparation device - Google Patents
Catalyst preparation drying tower and catalyst preparation device Download PDFInfo
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- CN216063307U CN216063307U CN202121761983.2U CN202121761983U CN216063307U CN 216063307 U CN216063307 U CN 216063307U CN 202121761983 U CN202121761983 U CN 202121761983U CN 216063307 U CN216063307 U CN 216063307U
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Abstract
The utility model relates to a catalyst preparation drying tower (1) and a catalyst preparation device, wherein the top of the catalyst preparation drying tower (1) is provided with an active carbon feed inlet (101) and a first air inlet and outlet (102), the bottom of the tower is provided with a second air inlet and outlet (103) and a liquid inlet and outlet (104), the tower body of the catalyst preparation drying tower (1) is provided with a discharge opening (105) close to the bottom of the tower, and the tower body of the catalyst preparation drying tower (1) is provided with an overflow opening (106) close to the top of the tower. The utility model can switch between spraying method and dipping method, thereby greatly saving production cost.
Description
Technical Field
The utility model relates to a catalyst preparation drying tower and a catalyst preparation device, in particular to a catalyst preparation drying tower and a catalyst preparation device which can be applied to synthesis of vinyl acetate by a calcium carbide acetylene method.
Background
The synthesis of vinyl acetate is divided into a petroleum ethylene method, a natural gas acetylene method, a calcium carbide acetylene method and a biological ethylene method from raw material sources, the existing calcium carbide acetylene method vinyl acetate synthesis reactor is divided into a fixed bed and a fluidized bed, a fluidized bed catalyst is generally prepared in a spraying mode, and the prepared catalyst can only be used for the fluidized bed and cannot be used for the fixed bed. The domestic catalyst used for producing vinyl acetate by adopting a fixed bed is generally prepared by adopting an immersion method, has weaker catalytic performance and shorter active period, and cannot meet the production requirement of a new process. Therefore, the synthesis of the vinyl acetate by the calcium carbide acetylene method in China mainly takes a fluidized bed as a main part, and the fixed bed catalyst mainly uses an imported catalyst, but the imported catalyst has excellent performance, but is expensive, difficult to transport and long in purchase period, so that the production cost is high.
The existing spray method for preparing the fluidized bed catalyst comprises the steps of preparing the fluidized bed catalyst, adding activated carbon in a drying tower, and adding Zn (AC)2Preparing and spraying a solution; drying, unloading, storing and the like of the catalyst. Generally, zinc acetate is first addedAnd adding zinc acetate and desalted water into the solution preparation tank, and preparing a zinc acetate solution with qualified concentration after the zinc acetate is completely dissolved. When preparing zinc acetate solution, start the air exhauster to active carbon loading hopper to drying tower top adds the active carbon, guarantees the operation of little negative pressure, after the receiving condition that is equipped with in the drying tower, carries out spraying of zinc acetate solution, sprays the back and carries out the drying to the catalyst, and it is qualified to be less than 0.5% catalyst water content in the drying tower. And finally, opening a discharge valve at the lower part of the drying tower, starting a catalyst feeding fan and a dust remover, and feeding the catalyst into a feeder by system pressure until the catalyst is completely discharged. However, the preparation method of the catalyst has the problems of high loss of zinc acetate, high loss of desalted water, high loss of activated carbon and the like.
The preparation of the fixed bed catalyst by using the impregnation method has the problems of high equipment investment fund, low equipment utilization rate, waste caused by equipment idling and the like because the fixed bed catalyst is used for preparing the catalyst by using the impregnation method for only about 1 month in one year on average, so that the preparation of the catalyst by using the impregnation method is less in domestic industry at present. It can be seen that the current catalyst formulation systems using impregnation and spraying methods have a number of drawbacks when used alone. How to solve the problem of idle utilization of fixed bed catalyst preparation devices in the industry is one of the problems to be solved urgently in the whole industry at present.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a catalyst preparation drying tower and a catalyst preparation device, which can meet the preparation requirements of a fixed bed catalyst and a fluidized bed catalyst simultaneously after being reformed based on the existing fluidized bed catalyst preparation drying tower, and are applied to the preparation of a catalyst for synthesizing vinyl acetate by a calcium carbide acetylene method, thereby improving the equipment utilization rate of the catalyst preparation device.
In order to achieve the above object, the present invention provides a catalyst preparation drying tower and a catalyst preparation device, wherein the top of the catalyst preparation drying tower is provided with an activated carbon feed inlet and a first air inlet and outlet, the bottom of the catalyst preparation drying tower is provided with a second air inlet and outlet and a liquid inlet and outlet, the tower body of the catalyst preparation drying tower is provided with a discharge opening near the bottom of the tower, and the tower body of the catalyst preparation drying tower is provided with an overflow opening near the top of the tower.
According to one aspect of the utility model, the overflow port is provided with a filter head and a filter structure, and the filter structure is a filter screen or a filter cartridge.
According to one aspect of the utility model, the filter screen has a mesh number of 10, 20 or 30, a diameter of 50-100cm, preferably 80cm, a length of 80-150cm, and is made of 304 stainless steel.
According to one aspect of the utility model, the filter cylinder is formed by rolling a stainless steel plate with the thickness of 3-8mm and the material of 316L, the length of the filter cylinder is 50-120cm, preferably 100cm, the cylinder body of the filter cylinder is uniformly provided with holes with the hole diameter of 1.8mm, the diameter of the cylinder body of the filter cylinder is DN150-DN250, preferably DN200, one end of the filter cylinder is connected with the overflow port, the other end of the filter cylinder is sealed to form a blind plate, and preferably, the blind plate is provided with micropores.
According to one aspect of the utility model, switchable block valves or blind plates are arranged at the first air inlet/outlet, the second air inlet/outlet, the liquid inlet/outlet, the discharge opening and the overflow opening;
the first air inlet and outlet and the discharge opening are respectively provided with two, and one of the discharge openings is obliquely connected with an external pipeline.
According to one aspect of the utility model, a distribution plate is arranged in the catalyst preparation drying tower and close to the bottom of the tower, and the distribution plate is a spray head type distribution plate or a Z-shaped curved surface distribution plate.
According to one aspect of the utility model, the spray head type distribution plate comprises a disc-shaped distribution bottom plate and a conical distribution spray head, vent holes with the diameter of 8-15mm are uniformly formed in the disc-shaped distribution bottom plate, the conical distribution spray head comprises a tubular conical rod with an opening at the bottom end and a conical cap, the conical rod penetrates through the vent holes and is fixed on the disc-shaped distribution bottom plate through nuts, the conical cap is arranged at the top end of the tubular conical rod, at least 4 air holes with the diameter of 2-3mm are symmetrically arranged on the conical surface of the conical cap along the central axis of the conical cap, and the air volume of the distribution plate is 600N3/h。
According to the bookAn aspect of the utility model, Z type curved surface distributing plate includes discoid distribution bottom and corrugate distribution layer, evenly set up the air vent that the diameter is 8-15mm on the discoid distribution bottom, corrugate distribution layer fixed connection be in on the discoid distribution bottom, corrugate distribution layer height is 2-4cm, evenly arranged on the corrugate distribution layer has the air current hole that the diameter is 2-3mm, and the distributing plate amount of wind is 3000N3/h。
According to one aspect of the utility model, the middle part of the catalyst preparation drying tower is also provided with a detachable liquid inlet pipe which horizontally extends towards the inner cavity of the tower body, and the liquid inlet pipe is provided with a spray head;
a heating coil and a heating tube array are arranged on two sides of the liquid inlet pipe in the catalyst preparation drying tower;
the heating coil is installed on the catalyst preparation drying tower through a fixing plate group, and at least 5 layers are arranged in a downward installation mode.
The catalyst preparation device is used for a calcium carbide acetylene method vinyl acetate synthesis process, and comprises a fixed bed zinc acetate preparation tank, a first zinc acetate filter, a zinc acetate recovery pump, a zinc acetate circulating pump, a first air blower and a first air preheater which are sequentially connected, an overflow pipeline connected with a filter head of the catalyst preparation drying tower, wherein the overflow pipeline is connected with the fixed bed zinc acetate preparation tank, the zinc acetate recovery pump is further communicated with a liquid inlet and a liquid outlet of the catalyst preparation drying tower and a recovery port of the fixed bed zinc acetate preparation tank, an outlet of the zinc acetate circulating pump is respectively connected with the overflow pipeline and the liquid inlet and the liquid outlet of the catalyst preparation drying tower, and the first air preheater is connected with one of the first inlet and the outlet of the catalyst preparation drying tower.
According to one aspect of the utility model, the device further comprises a dust remover, an induced draft fan and a condenser which are connected in sequence, wherein a liquid descending pipe of the condenser is connected with the overflow pipeline.
According to one aspect of the utility model, the inlet of the dust collector is connected to the second air inlet/outlet of the catalyst preparation drying tower.
According to one aspect of the utility model, the catalyst preparation drying tower further comprises a fluidized bed zinc acetate preparation tank, a second filter, a zinc acetate feeding pump set, a second air blower and a second air preheater which are sequentially connected, wherein the zinc acetate feeding pump set comprises a first feeding pump and a second feeding pump, inlets of the first feeding pump and the second feeding pump are both connected with the second filter, outlets of the first feeding pump and the second feeding pump are both connected with a liquid inlet pipe of the catalyst preparation drying tower, and the second air preheater is connected with a second air inlet and a second air outlet of the catalyst preparation drying tower.
According to one aspect of the utility model, the inlet of the dust separator is connected to a line connecting the second air preheater and the second air inlet/outlet of the catalyst preparation drying tower.
According to one aspect of the utility model, the device further comprises a bag-type dust collection group, wherein the bag-type dust collection group comprises a first bag-type dust collector and a second bag-type dust collector which are sequentially connected, and an inlet of the first bag-type dust collector is connected with the other first air inlet and outlet of the catalyst preparation drying tower.
According to one aspect of the utility model, the device further comprises a nitrogen conveying pipeline connected with the filter head of the catalyst preparation drying tower, and the connection point is close to the overflow port of the catalyst preparation drying tower.
According to one aspect of the utility model, the pipe diameter of a recovery pipe connected with a recovery port of the fixed bed zinc acetate preparation tank and a zinc acetate recovery pump is DN40-DN 80;
the pipe diameter of a lower liquid pipe of the condenser is DN50-DN 80.
According to one aspect of the utility model, the catalyst preparation drying tower further comprises a water pump and a temperature and pressure reduction device which are connected in sequence, wherein the temperature and pressure reduction device is positioned on the heating pipeline of the heating coil and the heating column of the catalyst preparation drying tower.
According to one aspect of the utility model, a tube-jacketed condenser is also included, located on the vent recovery line at the top of the fixed bed zinc acetate make-up tank.
According to one aspect of the utility model, the pipe diameter of a pipeline of the zinc acetate circulating pump communicated with the overflow pipeline is DN125-DN200, and the pipe diameter of the overflow pipeline is DN200-DN 300.
In accordance with one aspect of the present invention, bismuth subcarbonate may be added to the zinc acetate formulation tank during operation.
According to one scheme of the utility model, the tower body of the catalyst preparation drying tower is additionally provided with various openings, and the corresponding isolating valves are arranged at the openings, so that when the catalyst preparation drying tower is applied to a catalyst preparation system for a fluidized bed reactor (a spraying method) and a catalyst preparation system for a fixed bed reactor (an impregnation method), the isolating valves can isolate the two catalyst preparation systems.
According to one scheme of the utility model, a condenser is additionally arranged at the emptying part of the dust remover, and the lower liquid of the condenser returns to the zinc acetate preparation tank, so that the zinc acetate can be collected, and the production cost is reduced.
According to one scheme of the utility model, the overflow port of the catalyst preparation drying tower is additionally provided with a filtering structure which can be a filtering net or a filtering cylinder, so that the catalyst can be prevented from losing and pouring into the zinc acetate preparation tank, and the yield of the catalyst is improved. Meanwhile, the filter cartridge made of rolled steel plates has high strength and large aperture, and can avoid the situation of liquid overflow caused by activated carbon blockage.
According to one scheme of the utility model, the nitrogen pipe is additionally arranged beside the overflow port, so that nitrogen can be blown to the filtering structure of the overflow port discontinuously, the activated carbon blocked on the filtering structure can be blown off, the solution can be ensured to smoothly pass through the overflow port, the production efficiency is improved, and the production period is shortened.
According to one scheme of the utility model, the heating coil of the catalyst preparation drying tower is heightened and modified, specifically, 5 layers are heightened in a downward installation mode, so that the heat exchange area of the coil is increased, the installation mode of the coil is changed, the gap between the original coil and the tube array is filled, the drying effect is improved, and the catalyst is dried more uniformly.
According to an aspect of the present invention, the distribution plate in the catalyst preparation drying tower may be a nozzle type distribution plate or a Z-curved design distribution plate, so that it can be switched to be suitable for the spraying method and the dipping method, respectively.
According to one scheme of the utility model, the pipe diameter of the self-reflux pipe of the fixed bed zinc acetate preparation tank is set to DN125-DN200, so that the stirring efficiency and the self-reflux efficiency of the preparation tank can be ensured, the components in the tank can be fully mixed and dissolved, the solution preparation time and the production period can be shortened, and the production efficiency can be improved.
According to one scheme of the utility model, the temperature and pressure reducing device and the water pump matched with the temperature and pressure reducing device are arranged on the steam main pipe, so that good temperature control can be realized, and the situations that the proper valve opening degree is difficult to master due to manual control of the steam valve group and the temperature rise is too fast or too slow in the temperature rise process due to large difference of temperature difference of steam heating and drying are avoided.
According to one scheme of the utility model, the pipe diameter of the lower liquid pipe of the condenser is set to DN50-DN80, so that the condition of material spraying caused by the fact that the pipe diameter is too small can be avoided.
According to one scheme of the utility model, the bismuth subcarbonate is added into the zinc acetate preparation tank, so that the side reaction of vinyl acetate synthesis can be reduced.
According to one scheme of the utility model, the pipe diameter of a pipeline for communicating the zinc acetate circulating pump with the overflow pipeline is set to DN125-DN200, and the pipe diameter of the overflow pipeline is DN200-DN300, so that the flow velocity of the zinc acetate solution in the overflow pipeline can be ensured, the pressure building of a catalyst preparation drying tower is avoided, and the solution in the zinc acetate preparation tank can be mixed more uniformly.
Drawings
FIG. 1 schematically shows a structural diagram of a catalyst preparation drying tower according to an embodiment of the present invention;
FIG. 2 is a schematic representation of a filter head and filter structure on a catalyst preparation drying tower according to one embodiment of the present invention;
FIG. 3 is a schematic view showing the configuration of a catalyst preparation apparatus according to a first embodiment of the present invention;
FIG. 4 is a schematic diagram showing a configuration of a catalyst preparation apparatus according to a second embodiment of the present invention.
Detailed Description
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments will be briefly described below. It is obvious that the drawings in the following description are only some embodiments of the utility model, and that for a person skilled in the art, other drawings can be derived from them without inventive effort.
In describing embodiments of the present invention, the terms "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in an orientation or positional relationship that is based on the orientation or positional relationship shown in the associated drawings, which is for convenience and simplicity of description only, and does not indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and thus, the above-described terms should not be construed as limiting the present invention.
The present invention is described in detail below with reference to the drawings and the specific embodiments, which are not repeated herein, but the embodiments of the present invention are not limited to the following embodiments.
Referring to fig. 1, the top of the catalyst preparation and drying tower 1 of the present invention is provided with an activated carbon inlet 101 and a first air inlet/outlet 102, the bottom of the tower is provided with a second air inlet/outlet 103 and a liquid inlet/outlet 104, the tower body of the catalyst preparation and drying tower 1 is provided with a discharge opening 105 near the bottom of the tower, and is provided with an overflow opening 106 near the top of the tower. Wherein, the liquid inlet and outlet 104 can be used as a liquid inlet and a liquid outlet of the zinc acetate solution in the dipping method; the second air inlet/outlet 103 may serve as an air outlet for the dipping method and an air inlet for the spraying method; the obliquely arranged discharge opening 105 is used as a discharge opening of the dipping method; the overflow port 106 is mainly used for overflowing the zinc acetate solution by the dipping method; the first air inlet/outlet 102 may serve as an air inlet for the dipping method and an air outlet for the spraying method.
Therefore, the utility model improves each opening of the catalyst preparation drying tower 1, and adds the overflow port 106 near the tower top, so that the catalyst preparation drying tower 1 can be simultaneously applied to a spray method fluidized bed catalyst preparation system and an immersion method solidified bed catalyst preparation system. Furthermore, switchable block valves or blind plates are arranged at the first air inlet/outlet 102, the second air inlet/outlet 103, the liquid inlet/outlet 104, the discharge opening 105 and the overflow opening 106. Thus, the isolation of the two catalyst preparation modes can be realized by switching the block valves or the blind plates distributed at the openings of the tower body of the catalyst preparation drying tower 1. In addition, two first air inlets and outlets 102 and two discharge ports 105 are provided, and an external line of one of the discharge ports 105 is obliquely provided, thereby being suitable for the preparation of a fluidized bed catalyst and a fixed bed catalyst, respectively. The fluidized bed catalyst has higher strength and higher yield, so that the fluidized bed catalyst discharge opening is connected with the feeder, the air conveying pipeline and the induced draft fan and used for conveying the fluidized bed catalyst to the storage bin through air, thereby saving manpower; because the fixed bed catalyst has low strength, the fixed bed catalyst can be prevented from being damaged by transportation in a pipeline by adopting a mode of directly discharging the fixed bed catalyst into a packaging bag through an inclined pipeline.
In order to prevent the catalyst from losing and being poured into the zinc acetate preparation tank, the utility model also provides a filter head 107 and a filter structure 108 at the overflow port 106, so as to avoid the above-mentioned backflow situation of the catalyst and improve the yield of the catalyst. In the present invention, the filter structure 108 may be a filter screen or a filter cartridge. If the filter screen is selected, the mesh number of the filter screen is 10, 20 or 30, the diameter (which can be regarded as the length of the filter opening) is 60-100cm, the length is 90-150cm, and the material is 304 stainless steel. If the filter cartridge is selected, holes are uniformly formed in the cartridge body of the filter cartridge, the hole diameter of each hole is 1.8mm, the diameter of each hole is DN150-DN250, the length (which can be regarded as the length of a filter opening) of each hole is 50-120cm, and each hole is formed by rolling a stainless steel plate which is 3-8mm thick and is made of 316L materials. The filter cartridge is relatively high in strength and large in pore size, so that the situation that liquid overflows due to blockage of the activated carbon can be avoided.
In the utility model, a distribution plate 109 is arranged in the catalyst preparation drying tower 1 near the bottom of the tower, and the distribution plate 109 can be a spray head type distribution plate or a Z-shaped curved surface distribution plate. The spray head type distribution plate is suitable for a spraying method, and the Z-shaped curved surface distribution plate is suitable for an immersion method, so that the two methods can be switched conveniently; the spray head type distribution plate has the functions of ensuring uniform air volume distribution, avoiding channeling caused by direct blowing, being beneficial to drying the fluidized active carbon in the drying tower, avoiding the downward leakage of granular active carbon from the vent holes of the distribution plate, ensuring the strength of the distribution plate, ensuring the aperture ratio and preventing blockage. Wherein, the bottom plate of Z type curved surface distributing plate has the air vent and plays and supports and the air inlet effect, and the face shape of Z type curved surface distributing plate is actually for following the corrugate of "Z" style of calligraphy formation to can increase the gas pocket area, in order to accelerate drying rate, and can prevent the tower interior suppress the pressure, guarantee circulating liquid throughput simultaneously, ensure that the flooding reaches the intended effect. In addition, in order to meet the use requirement of the spraying method, the utility model also arranges a detachable liquid inlet pipe 110 which horizontally extends towards the inner cavity of the tower body in the middle of the catalyst preparation drying tower 1 and is used for the liquid inlet of the zinc acetate solution in the spraying method. The liquid inlet pipe 110 is provided with a spray head 111, preferably an atomizing spray head, for spraying the zinc acetate solution onto the activated carbon on the distribution plate 109 in the spraying method. The heating coil 112 and the heating tube array 113 are respectively arranged at the upper side and the lower side of the liquid inlet pipe 110 in the catalyst preparation drying tower 1.
The heating coils 112 are installed on the catalyst preparation drying tower 1 by means of a fixed plate set and are provided in a downward installation manner with at least 5 layers, preferably 8 layers. Thus, the heating coil 112 on the catalyst preparation drying tower 1 is heightened and modified, and the traditional upward installation is replaced by the downward installation mode, so that the heat exchange area of the coil is increased, the installation mode of the coil is changed, the gap between the original coil and the tube array is filled, for the preparation of the fixed bed catalyst, the heat exchange area of the catalyst is increased, the drying effect is improved, and the catalyst is dried more uniformly.
Referring to fig. 3, the catalyst preparation apparatus of the present invention includes a fixed bed zinc acetate preparation tank 2, a first zinc acetate filter 3, a zinc acetate recovery pump 4, a zinc acetate circulation pump 5, and a first air blower 6 and a first air preheater 7 connected in sequence. In addition, the catalyst preparation apparatus further includes an overflow line 8 connected to the filter head 107 of the catalyst preparation drying tower 1, and the overflow line 8 is connected to the fixed bed zinc acetate preparation tank 2. In addition, the zinc acetate recovery pump 4 is also communicated with the liquid inlet and outlet 104 of the catalyst preparation drying tower 1 and the recovery port of the fixed bed zinc acetate preparation tank 2. The outlet of the zinc acetate circulating pump 5 is respectively connected with the overflow pipeline 8 and the liquid inlet and outlet 104 of the catalyst preparation drying tower 1, and the first air preheater 7 is connected with one of the first air inlet and outlet 102 of the catalyst preparation drying tower 1.
In addition, the catalyst preparation device also comprises a dust remover 9, an induced draft fan 10 and a condenser 11 which are connected in sequence, and a liquid descending pipe of the condenser 11 is connected with the overflow pipeline 8. Therefore, the lower liquid of the condenser 11 additionally arranged in the utility model can return to the zinc acetate preparation tank 2, thereby realizing the purpose of recovering the zinc acetate and reducing the production cost. In addition, if the pipe fitting of the downcomer of the condenser 11 is designed to be smaller, for example, the pipe diameter of the downcomer is DN40, which may cause the material spraying condition in the downcomer of the condenser 11, and research and experiments find that the material spraying phenomenon can be eliminated when the inner diameter of the downcomer is 50mm or more, so the pipe diameter of the downcomer of the condenser 11 is set to be DN50-DN 80. In addition, research tests show that the pipe diameter of a pipeline for communicating the zinc acetate circulating pump 5 with the overflow pipeline 8 is set to DN125-DN200, so that the solution in the preparation tank can be mixed more uniformly.
According to the embodiment shown in fig. 3, the inlet of the dust remover 9 is connected with the second air inlet/outlet 103 of the catalyst preparation drying tower 1 through a corresponding pipeline, a condenser 11 is additionally arranged at the emptying part of the dust remover 9, and meanwhile, a part of process pipelines, preparation tanks and other equipment are additionally arranged, so that the purposes of dust removal and zinc acetate solution recovery during the preparation of the fixed bed catalyst for drying are achieved.
In the case of the dipping method, for example, when the catalyst preparation apparatus of the present invention is used for production, a zinc acetate solution is first prepared. Specifically, firstly adding desalted water into a zinc acetate preparation tank, wherein the adding amount is about 17m3And adding the mixture until the liquid level reaches 70 percent of the zinc acetate preparation tank. The first air preheater was then operated to heat up to 80 ℃ with steam and held at constant temperature. After the temperature is raised, the stirrer and the zinc acetate circulating pump 5 are started, and a return pipe valve of the fixed bed zinc acetate preparation tank 2 is opened, so that the solution circulation is carried out. And Zn (AC) was slowly added to the fixed bed zinc acetate preparation tank 22Then HAC is added. Specifically, whether or not to continue the addition and the addition amount can be determined according to the pH value. Bismuth subcarbonate was also added during this period to bring the liquid level to 90%. Fixed bed zinc acetate preparation tank 2 was sampled for Zn (AC)2Content and pH, and water or HAC, Zn (AC)2. After complete dissolution, sampling analysis was continued until Zn (AC)2When the concentration is 20-25% and the pH value is 4-6, regulating the steam flow to raise the temperature of the solution to 90 deg.c.
After the preparation of the zinc acetate solution is finished, adding activated carbon, specifically adding the activated carbon into the catalyst preparation drying tower 1, wherein the adding amount of the activated carbon is limited to be not more than the plane of an overflow port of the catalyst preparation drying tower 1, the activated carbon cannot be impregnated when more than the overflow port is added, the preparation yield is low when less than the overflow port is added, the reasonable height is determined by calculation and experiments, and the adding amount of the activated carbon is preferably 2-5m3More preferably 3.5m3. During the first activated carbon filling process, about 3.5m of activated carbon was added3Then, the filling height of the activated carbon in the catalyst preparation and drying tower 1 is observed, and the activated carbon can be added to the position 20cm above the coil pipe in the catalyst preparation and drying tower 1. If the amount of the activated carbon added at this time does not reach the specified value, the amount of the activated carbon added 20cm above the coil pipe in the catalyst preparation and drying tower 1 at this time is taken as the standard. If the specified amount of activated carbon is added, the top of the coil pipe is covered but the position of 20cm above the coil pipe is not reached, the specified value is still used as the standard. If the specified activated carbon is added and the top of the coil pipe is not covered, the activated carbon is continuously added until the activated carbon covers the top of the coil pipe, and the amount of the activated carbon is added at the momentThe amount of activated carbon added to the top of the coil when covered is based.
And then, carrying out a dipping step, namely closing an outlet butterfly valve of the preheater, an outlet butterfly valve at the bottom of the catalyst preparation drying tower 1, a zinc acetate recovery pump 4, an inlet and outlet valve of a zinc acetate circulating pump 5, and a related pressure sampling valve, a sampling valve and an air guide valve, so as to isolate the system. Then, the preparation adsorption system is ready to operate, the pneumatic valve at the outlet of the overflow pipe is opened, the pump inlet valve of the zinc acetate circulating pump 5 is opened, and the zinc acetate circulating pump 5 is started. Adjusting outlet valve of zinc acetate circulation pump 5, controlling flow rate to make solution 10-50m3The flow rate of the solution is increased to 80-120m after half an hour3Circulating for h time, and stably controlling the circulating amount to be 80-120m3H is used as the reference value. The steam flow was adjusted to maintain the temperature of the fixed bed zinc acetate preparation tank 2 at 90 ℃. + -. 5.0 ℃ during the impregnation. After the activated carbon is soaked for 2.5 hours, the solution in the fixed bed zinc acetate preparation tank 2 is taken every half hour to detect the content of the zinc acetate. And if the difference between the two adjacent detection results is within 0.5%, the activated carbon is considered to be adsorbed and saturated, namely the impregnation is finished. After the adsorption is finished, closing the zinc acetate circulating pump 5 and an outlet valve thereof, opening a pump inlet valve of the zinc acetate recovery pump 4, starting the zinc acetate recovery pump 4, opening a lead-out valve and a pressure collecting valve, returning the liquid in the catalyst preparation drying tower 1 to the solid bed zinc acetate preparation tank 2, draining the solution in the catalyst preparation drying tower 1, and dripping for 5 hours. Of course, the dripping-off time should be as long as possible. In the dripping process, the zinc acetate recovery pump 4 is started every half hour, and the liquid dripped in the catalyst preparation drying tower 1 is sent to the fixed bed zinc acetate preparation tank 2 for recycling.
And (3) drying after the impregnation step is completed, firstly, converting the system, specifically, closing an outlet (namely an overflow port 106) pneumatic valve of an overflow pipe of the catalyst preparation drying tower 1, closing an emptying valve at the bottom of the catalyst preparation drying tower 1, an inlet and an outlet valve of a zinc acetate recovery pump 4 and a zinc acetate circulating pump 5, starting a dust remover 9 and an induced draft fan 10, and opening an outlet valve of a first air preheater 7, so that the catalyst preparation drying tower 1 is switched to a drying mode. And then starting the first air blower 6, putting the first air preheater 7 into operation, opening a preheater steam valve and a drain valve group, heating air by adjusting the steam flow entering the preheater, and blowing hot air through the first air inlet and outlet 102 to heat the catalyst in the catalyst preparation drying tower 1. If the temperature rise speed of the catalyst preparation drying tower 1 is low, then the valves of the coil pipes and the tube steam pipes of the catalyst preparation drying tower 1 are opened, and the temperature rise of the catalyst preparation drying tower 1 is carried out through the coil pipes and the tube steam pipes. The temperature rising speed is controlled by adopting a temperature programming mode as follows: heating at a rate of 10-15 deg.C/h before 70 deg.C, heating at a rate of 8-10 deg.C/h at 70-90 deg.C, heating at a rate of 3-5 deg.C/h after 90 deg.C, and ensuring that the temperature does not exceed 102 deg.C. The temperature of the catalyst preparation drying tower 1 takes the temperature of the middle section of the catalyst preparation drying tower 1 as a main monitoring point, the bottom temperature as a secondary monitoring point, and other temperature control points as auxiliary judgment basis.
After the research of the applicant, the activity and the service life of the fixed bed catalyst are also greatly related to the drying treatment process of the impregnated catalyst.
Research shows that when air temperature rise is carried out to dry the catalyst after the dipping solution is drained, if conventional preheated air is adopted to enter from the bottom of the catalyst preparation drying tower 1, airflow upwards contacts with a wet catalyst to dry the catalyst, the catalyst at the bottom of the catalyst preparation drying tower 1 is excessively dried, zinc acetate on the surfaces of active carbon particles is seriously crystallized, and the moisture of the catalyst at the upper layer of the catalyst preparation drying tower 1 exceeds the standard. In the embodiment, preheated air is adopted to enter from the top of the catalyst preparation drying tower 1, namely, air enters from the upper part and exits from the lower part, hot air flows move along the bed layer of the catalyst preparation drying tower 1 from the upper part to the lower part, on one hand, the dehydration and drying of the catalyst can be accelerated by following the downward collection of liquid in the early stage of drying, on the other hand, the steam formed in the drying process has the power of returning from the bottom to the upper part, and the part of the returning steam can play a role in partially reducing the influence of zinc acetate crystals on the surfaces of carbon particles in the drying process of the activated carbon, so that the catalyst with the same zinc acetate loading capacity is prepared. In addition, the mode of upper inlet and lower outlet is adopted, the integrity of active carbon particles can be ensured, the active carbon in the catalyst preparation drying tower 1 can be compacted by the mode, and the problem that the active carbon is in a fluidized state due to high air speed and collides with each other to cause the breakage of the active carbon particles and the loss of the catalyst in the traditional drying mode of lower inlet and upper outlet is avoided.
The research also finds that the zinc acetate on the surface of the activated carbon particles is not easy to crystallize under the condition of the same zinc acetate loading amount by controlling the temperature of the dried activated carbon in a mode of temperature programming to the impregnated activated carbon particle pile. The reason is that the gradual temperature rise and drying are carried out by adopting a segmented temperature program way, so that the zinc acetate adsorbed by the surface gaps of the activated carbon can be inhibited from moving to the particle surface, namely the crystallization of the zinc acetate on the particle surface of the activated carbon and in the micropores is inhibited, the micropore blockage of the activated carbon is avoided, the loading performance of the activated carbon on the active component zinc acetate is effectively improved, the high activity and the long service life under the condition of high zinc acetate loading capacity are maintained, and the catalyst efficiency is obviously improved.
After the temperature is raised to 90 ℃, the condensate of the condenser 11 at the outlet of the dust remover 9 is taken for analyzing the HAC content, one sample is taken half an hour before 95 ℃, one sample is taken 15 minutes after 95 ℃, and the analysis that the acetic acid content in the sample is more than 50g/L is qualified after drying. In addition, HAC content in the solution is 50-200g/L as a control index, i.e. H is not allowed2HAC in O exceeds 200g/L to prevent the strength of the catalyst from being reduced and the brittleness of the catalyst from being improved due to over-drying. When the active carbon in the tower is dried to be qualified, the flow of the steam at the inlet of the first air preheater is gradually reduced to reduce the temperature, so that the temperature is reduced at a speed of not more than 20 ℃/h, and the temperature of the catalyst preparation drying tower 1 is predicted to be reduced to below 50 ℃ after 3 hours. Closing a steam valve of the catalyst preparation drying tower 1, stopping heating, closing a first air preheater 7 to heat a steam inlet valve, stopping a first air blower 6, closing a butterfly valve of an outlet of the preheater, opening a discharge valve 105, and automatically discharging the catalyst by gravity. And then taking the catalyst to prepare the discharging material of the drying tower 1, namely the prepared catalyst, and detecting the loading capacity and the moisture of the zinc acetate. The concrete indexes meet the production requirements that the loading capacity is 33% +/-2%, and the moisture content is<10％。
In the embodiment, because the catalyst preparation drying tower 1 is adopted, after the catalyst impregnation is completed, the impregnated catalyst to be dried is not required to be discharged from the impregnation tank and transferred to the drying equipment for drying treatment like the traditional fixed bed catalyst preparation process, so that the loss of catalyst damage and the like caused in the catalyst transfer process is avoided, the process is simple, the continuous operation can be realized, and the catalyst preparation efficiency is improved.
And finally, supplementing the solution, specifically, recovering the condensate to the solid bed zinc acetate preparation tank 2 while drying the catalyst, and analyzing Zn (AC) in the solid bed zinc acetate preparation tank 2 after drying2Content, Zn (AC) measured from the level meter reading and analysis of the solution at that time2The content is calculated, when the solution is supplemented to the liquid level of 90 percent and the concentration of the zinc acetate is 20 to 25 percent, the desalted water and Zn (AC) are added into the solid bed zinc acetate preparation tank 22The amount of (c). Adding desalted water, Zn (AC) according to the calculated amount2And bismuth subcarbonate, after complete dissolution, sampling the solution for analysis of Zn (AC)2Content and pH. According to the result of the solution detection analysis, HAC, desalted water or Zn (AC) are selectively and continuously supplemented according to the requirement2And adjusting the steam flow until the solution concentration is 20-25%, the pH value is in the range of 4-6 and the reading of the liquid level meter is about 90%, and heating the solution to 90 ℃ for later use.
According to the embodiment shown in fig. 4, the catalyst preparation apparatus further comprises a fluidized bed zinc acetate preparation tank 12, a second filter 13, a zinc acetate feed pump unit 14, and a second air blower 15 and a second air preheater 16, which are connected in sequence. The zinc acetate feed pump unit 14 comprises a first feed pump 141 and a second feed pump 142, the inlets of which are connected with the second filter 13, the outlets of the first feed pump 141 and the second feed pump 142 are connected with the liquid inlet pipe 110 of the catalyst preparation drying tower 1, and the second air preheater 16 is connected with the second air inlet/outlet 103 of the catalyst preparation drying tower 1. In the present embodiment, the inlet of the dust collector 9 is also connected to a line connecting the second air preheater 16 and the second air inlet/outlet 103 of the catalyst preparation/drying tower 1, and in order to switch the use of the fixed bed catalyst preparation system and the fluidized bed catalyst preparation system, a blocking valve is further provided on a connecting line connecting the first air preheater 7 and the first air inlet/outlet 102 on the top of the catalyst preparation/drying tower 1. The catalyst preparation device in this embodiment further includes a bag dust removal group 17, which includes a first bag dust remover 171 and a second bag dust remover 172 connected in sequence, and an inlet of the first bag dust remover 171 is connected to another first air inlet/outlet 102 of the catalyst preparation drying tower 1. The fixed bed catalyst preparation apparatus of this embodiment is used in a manner similar to that shown in fig. 3, and therefore, will not be described in detail.
According to the embodiment shown in fig. 4, when the device is used for the spraying fluidized bed catalyst preparation, first, the switchable block valves or blind plates arranged at the first air inlet/outlet 102, the second air inlet/outlet 103, the liquid inlet/outlet 104, the discharge opening 105 and the overflow opening 106 are closed to cut off the dipping fixed bed catalyst preparation system. Secondly, the distribution plate 9 in the catalyst preparation drying tower 1 is replaced by a spray head type distribution plate, the heating coil 112 is replaced by an upward installation mode suitable for the preparation of the fluidized bed catalyst by a spraying method, a liquid inlet pipe 110 horizontally extending towards the inner cavity of the tower body is additionally arranged at the middle part of the catalyst preparation drying tower 1, and 4-8 groups of atomizing spray heads 111 are uniformly distributed on the liquid inlet pipe 110. When the catalyst preparation drying tower 1 is ready, the activated carbon addition, Zn (AC), can be carried out according to the traditional spraying method fluidized bed catalyst preparation and use method2Preparing and spraying the solution, and drying, unloading and storing the catalyst.
Therefore, the embodiment shown in fig. 4 is equivalent to that equipment such as a preparation tank meeting the preparation requirement of a fixed bed is added on the basis of the existing fluidized bed catalyst preparation system, and the structure, the internal special structural member and the installation mode of the catalyst preparation drying tower 1 are matched for adaptive modification, so that the modified device has the function of preparing both a fluidized bed and a fixed bed catalyst.
The two embodiments have the same point that the catalyst preparation drying tower 1 of the present invention can be used for preparing a fixed bed catalyst, but the embodiment shown in fig. 4 needs to add a set of zinc acetate preparation equipment meeting the requirement of preparing a fluidized bed catalyst, and can also be used for preparing the fluidized bed catalyst under the condition of adjusting internal components such as a distribution plate, a liquid inlet pipe, a heating coil and the like of the catalyst preparation drying tower 1 and switching an isolating valve or a blind plate.
In the present invention, the catalyst preparation apparatus further comprises a nitrogen gas transfer line 18 connected to a filter head 107 of the catalyst preparation drying tower 1 at a point near the overflow port 106 of the catalyst preparation drying tower 1. Thus, the solution had a thickness of 10m3The/h is gradually increased to 100m3In the process of/h, nitrogen is intermittently blown into the filter head 107 at the overflow port 106 of the catalyst preparation drying tower 1, so that the activated carbon blocked on the filter structure 108 can be blown off, and the solution can smoothly pass through the overflow port 106, thereby improving the efficiency and production efficiency and shortening the production period.
In addition, because the stirring and self-refluxing of the traditional zinc acetate preparation tank have defects, the solid and liquid components in the tank cannot be efficiently and fully mixed and dissolved, the solution preparation time and the production period are prolonged, and the production efficiency is reduced. Therefore, in the utility model, the pipe diameter of the return pipe connecting the zinc acetate circulating pump 5 and the overflow pipeline 8 is set to DN125-DN200, thereby eliminating the defect and ensuring the production efficiency. Meanwhile, the pipe diameter of the overflow pipeline is DN200-DN300, so that the flow rate of the zinc acetate solution in the overflow pipeline is ensured, and the pressure building of a drying tower for preparing the catalyst is avoided.
In addition, because the steam valves of air heater and catalyst preparation drying tower 1's coil pipe and the steam valves of tubulation generally rely on manual control to be difficult to master suitable valve aperture, simultaneously again because adopt superheated steam heating drying to differ great because of the difference in temperature, can lead to the condition that the programming rate is too fast or slow often to appear among the intensification process, thereby be unfavorable for the control to drying process. Therefore, the catalyst preparation device of the present invention is further provided with a water pump 19 and a temperature and pressure reducing device 20 which are connected in sequence, and the temperature and pressure reducing device 20 is located on the heating pipeline (i.e. steam main) of the heating coil 112 and the heating pipe 113 of the catalyst preparation drying tower 1, so that the water pump 19 can be used for pumping demineralized water into the temperature and pressure reducing device 20, thereby realizing the temperature control function.
The utility model also arranges a pipeline jacketed condenser 22 on the emptying recovery pipeline 21 at the top of the fixed bed zinc acetate preparation tank 2, thereby avoiding the overhigh temperature of the emptying recovered materials. In addition, in the aspect of materials, the bismuth subcarbonate is added in the zinc acetate preparation tank, so that the side reaction of vinyl acetate synthesis can be effectively reduced.
In conclusion, the catalyst preparation device can simultaneously meet the requirements of preparing a fixed bed synthetic vinyl acetate catalyst by an impregnation method and preparing a fluidized bed synthetic vinyl acetate catalyst by a spraying method, namely has the function of preparing and producing the fixed bed catalyst and the fluidized bed catalyst in the same device, thereby improving the utilization rate of equipment and saving the production cost by about 405 ten thousand yuan per bed. The discharging liquid of the condenser at the emptying position of the newly added dust remover can return to the zinc acetate preparation tank, so that the zinc acetate can be collected, and the production cost is reduced. In addition, the newly added filtering structure at the overflow port of the catalyst preparation drying tower can prevent the active carbon from flowing into the overflow pipe and then entering the zinc acetate preparation tank, thereby preventing the reduction of the catalyst yield and preventing the overflow caused by the blockage of the filter head. The utility model also carries out lengthening transformation and installation mode adjustment on the coil pipe of the catalyst preparation drying tower, fills the gap between the original coil pipe and the tube nest in the catalyst preparation drying tower, not only increases the heat exchange area of the coil pipe, but also greatly improves the drying effect, and leads the catalyst to be dried more uniformly. In addition, the dipping type preparation system adopts a Z-shaped curved surface to design the distribution plate, and the structure increases the air hole area by 30 percent on the basis of preventing the activated carbon from leaking downwards, thereby accelerating the drying speed, preventing the pressure build-up in the tower, simultaneously satisfying the throughput of circulating liquid and ensuring that the dipping achieves the expected effect.
In addition, the catalyst produced by the impregnation method can replace imported catalysts, the performance index of the catalyst is superior to that of the imported catalysts, and the yield of vinyl acetate produced by the catalyst is higher.
Table 1 comparison of the activity of the utility model with other catalysts
As can be seen from Table 1, the space-time yield of the fixed-bed catalyst of the present invention is from 1.9 to 2.1t/m, as compared with the catalyst imported from the same company, at a smaller catalyst loading under the same reaction temperature conditions3d is increased to 2.2-2.4t/m3d, the immediate empty yield is obviously improved by 26.3 percent at most. The fixed bed catalyst prepared by the utility model has higher activity.
TABLE 2 comparison of the Life of the utility model with other catalysts
Table 2 compares the life of the fixed bed catalyst of the utility model with the life of the imported catalyst. As can be seen from Table 2, under the continuous long-period operation production conditions at the same reaction temperature, the catalyst of the utility model has better activity reduction rate than that of the imported catalyst even when the reaction time is 7200 hours and far exceeds the operation time (5760 hours) of the imported catalyst, and the catalyst of the utility model has longer service life and longer period operation capability.
TABLE 3 comparison results of reaction solutions of the present invention with other catalysts
As can be seen from table 3, at the same reaction temperature, compared with the imported catalyst, the catalyst of the present invention has better selectivity, and the acetaldehyde content and the crotonaldehyde content in the reaction solution are lower, while the specific activity index (i.e. the index for detecting the specific activity of acetic acid in the reaction solution in the industry) can be reduced to 40s, which indicates that the fixed bed catalyst of the present invention has better selectivity and generates less impurities.
The above description is only one embodiment of the present invention, and is not intended to limit the present invention, and it is apparent to those skilled in the art that various modifications and variations can be made in the present invention. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (19)
1. The catalyst preparation drying tower (1) is characterized in that an activated carbon feeding hole (101) and a first air inlet and outlet (102) are formed in the top of the tower, a second air inlet and outlet (103) and a liquid inlet and outlet (104) are formed in the bottom of the tower, a discharging opening (105) is formed in the position, close to the bottom of the tower, of the tower body of the catalyst preparation drying tower (1), and an overflow opening (106) is formed in the position, close to the top of the tower, of the tower body of the catalyst preparation drying tower (1).
2. The catalyst formulation drying tower (1) according to claim 1, wherein a filter head (107) and a filter structure (108) are provided at the overflow port (106), and the filter structure (108) is a filter net or a filter cartridge.
3. The catalyst preparation drying tower (1) according to claim 2, wherein the filter mesh is 10, 20 or 30 mesh, 60-100cm in diameter, 90-150cm in length, and 304 stainless steel.
4. The catalyst preparation drying tower (1) according to claim 2, wherein the filter cartridge is made by rolling a stainless steel plate with a thickness of 3-8mm and a material of 316L, the length of the filter cartridge is 50-120cm, the cylinder body of the filter cartridge is uniformly provided with holes with a hole diameter of 1.8mm, and the diameter of the cylinder body of the filter cartridge is DN150-DN 250.
5. The catalyst formulation drying tower (1) according to claim 1, wherein switchable block valves or blind plates are arranged at the first air inlet/outlet (102), the second air inlet/outlet (103), the liquid inlet/outlet (104), the discharge port (105) and the overflow port (106);
the first air inlet and outlet (102) and the discharge opening (105) are respectively provided with two, and an external pipeline of one discharge opening (105) is obliquely arranged.
6. The catalyst preparation drying tower (1) according to claim 1, wherein a distribution plate (109) is arranged in the catalyst preparation drying tower (1) near the bottom of the tower, and the distribution plate (109) is a nozzle type distribution plate or a Z-shaped curved distribution plate.
7. The catalyst preparation drying tower (1) according to claim 1, wherein a detachable liquid inlet pipe (110) horizontally extending to the inner cavity of the tower body is further arranged in the middle of the catalyst preparation drying tower (1), and a spray head (111) is arranged on the liquid inlet pipe (110);
a heating coil (112) and a heating pipe array (113) are arranged on two sides of the liquid inlet pipe (110) in the catalyst preparation drying tower (1);
the heating coil (112) is installed on the catalyst preparation drying tower (1) through a fixing plate group, and at least 5 layers are arranged in a downward installation mode.
8. A catalyst preparation device using the catalyst preparation drying tower (1) of any one of claims 1 to 7, which is used for a calcium carbide acetylene method vinyl acetate synthesis process, and is characterized by comprising a fixed bed zinc acetate preparation tank (2), a first zinc acetate filter (3), a zinc acetate recovery pump (4), a zinc acetate circulating pump (5), a first air blower (6) and a first air preheater (7) which are sequentially connected, and an overflow pipeline (8) connected with a filter head (107) of the catalyst preparation drying tower (1), wherein the overflow pipeline (8) is connected with the fixed bed zinc acetate preparation tank (2), the zinc acetate recovery pump (4) is also communicated with a liquid inlet and outlet (104) of the catalyst preparation drying tower (1) and a recovery port of the fixed bed zinc acetate preparation tank (2), the outlet of the zinc acetate circulating pump (5) is respectively connected with the overflow pipeline (8) and the liquid inlet and outlet (104) of the catalyst preparation drying tower (1), and the first air preheater (7) is connected with one of the first air inlet and outlet (102) of the catalyst preparation drying tower (1).
9. The catalyst preparation device according to claim 8, further comprising a dust collector (9), an induced draft fan (10) and a condenser (11) which are connected in sequence, wherein a liquid descending pipe of the condenser (11) is connected with the overflow pipeline (8).
10. The catalyst preparation apparatus according to claim 9, wherein an inlet of the dust collector (9) is connected to a second air inlet/outlet (103) of the catalyst preparation drying tower (1).
11. The catalyst preparation device according to claim 9, further comprising a fluidized bed zinc acetate preparation tank (12), a second filter (13), a zinc acetate feed pump set (14), and a second air blower (15) and a second air preheater (16) which are connected in sequence, wherein the zinc acetate feed pump set (14) comprises a first feed pump (141) and a second feed pump (142) which are connected with the second filter (13) at inlet ends, the first feed pump (141) and the second feed pump (142) are connected with the liquid inlet pipe (110) of the catalyst preparation drying tower (1) at outlet ends, and the second air preheater (16) is connected with the second air inlet/outlet (103) of the catalyst preparation drying tower (1).
12. The catalyst formulation apparatus according to claim 11, wherein the inlet of the dust separator (9) is connected to a line connecting the second air preheater (16) and the second air inlet/outlet (103) of the catalyst formulation drying tower (1).
13. The catalyst preparation device according to claim 11, further comprising a bag dust collector group (17) comprising a first bag dust collector (171) and a second bag dust collector (172) connected in sequence, wherein an inlet of the first bag dust collector (171) is connected to the other first air inlet/outlet (102) of the catalyst preparation drying tower (1).
14. The catalyst formulation apparatus according to any one of claims 8 to 13, further comprising a nitrogen gas feed line (18) connected to a filter head (107) of the catalyst formulation drying column (1) at a point near an overflow (106) of the catalyst formulation drying column (1).
15. The catalyst preparation apparatus according to any one of claims 11 to 13, wherein the recovery pipe connecting the recovery port of the fixed bed zinc acetate preparation tank (2) to the zinc acetate recovery pump (4) has a pipe diameter of DN40-DN 80;
the pipe diameter of a lower liquid pipe of the condenser (11) is DN50-DN 80.
16. The catalyst preparation apparatus according to any one of claims 8 to 13, further comprising a water pump (19) and a temperature and pressure reducing device (20) connected in series, wherein the temperature and pressure reducing device (20) is located on a heating line of the heating coil (112) and the heating column (113) of the catalyst preparation drying tower (1).
17. The catalyst formulation plant according to any of claims 8 to 13, further comprising a tube jacketed condenser (22) located on the vent recovery line (21) at the top of the fixed bed zinc acetate formulation tank (2).
18. The catalyst preparation device according to any one of claims 8 to 13, wherein the pipe diameter of the pipe connecting the zinc acetate circulating pump (5) and the overflow pipe (8) is DN125-DN200, and the pipe diameter of the overflow pipe is DN200-DN 300.
19. A catalyst formulation arrangement according to any one of claims 8 to 13, wherein bismuth subcarbonate is added to the zinc acetate formulation tank during operation.
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| CN113499803B (en) * | 2021-07-30 | 2024-07-09 | 内蒙古双欣环保材料股份有限公司 | Catalyst preparation drying tower, catalyst preparation device and method |
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