Device for treating polyvinyl alcohol rectification residues
By designing a device that includes acetic acid residual liquid grooves, evaporators, and mixture mixtures, the problem of improper treatment of refined residues in polyvinol production in the production of polyvinyl alcohol has achieved the efficient recovery of acetic acid and decreased environmental pollution.
Patent Information
- Application Number
- CN202421183732.4
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-05-28
- Publication Date
- 2025-01-28
- Estimated Expiration
- 2034-05-28
AI Technical Summary
Improper distillation residues produced during polyvinyl alcohol production lead to volatilization of acetic acid, environmental pollution and increased production costs.
Design a device that treats polyethylene alcohol distillation residues, including the acetic acid residual liquid groove, the first and second residue evaporator, the mixture of the slag mixture, and the acid gas absorption tower. The recovery rate of acetic acid is reduced.
Effectively increase the recovery rate of acetic acid, reduce the pollution of the environmental residue to the environment, and reduce the waste of water resources during the production process and operation and maintenance costs.
Smart Images
Figure CN222400253U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the field of polyvinyl alcohol production, and specifically relates to a device for processing polyvinyl alcohol distillation residue. Background Art
[0002] Polyvinyl alcohol is an important chemical raw material. It can be used in fiber processing, weaving pulp, adhesives, architectural coatings, emulsion stabilizers and dispersants. It can also be used in the manufacture of acetal derivatives, degradable films, protective colloids, optical films and other products. It is widely used in textile, food, medicine, construction, agriculture and other industries.
[0003] The preparation process of polyvinyl alcohol includes: first, acetylene and acetic acid are used as raw materials to prepare vinyl acetate, vinyl acetate is polymerized under certain conditions to obtain polyvinyl acetate, and polyvinyl acetate is subjected to alcoholysis to obtain polyvinyl alcohol, wherein acetylene can be prepared by reacting calcium carbide with water. After vinyl acetate is obtained by synthesis reaction using acetylene and acetic acid, it needs to be distilled. The distillation process separates and refines the acetic acid and vinyl acetate in the synthetic reaction liquid. In the distillation process, acetic acid residue and tar and other high-boiling substances are produced. The acetic acid residue sent from each system is transported to the acetic acid residue tank for temporary storage. After the acetic acid residue is distilled, the distillation residue is obtained. About 7 kilograms of distillation residue is produced for every ton of polyvinyl alcohol produced. The distillation residue mainly contains high-boiling substances such as acetic acid, activated carbon, tar and some lipids. The composition ratio of the distillation residue is roughly as follows: about 25% acetic acid, about 30% water, about 20% activated carbon, and about 25% high-boiling substances. At present, the main treatment methods for residues in the polyvinyl alcohol industry are: 1. After simple distillation, it is sent to a pile for temporary storage, and then directly discharged into the cofferdam for drying or directly loaded onto a truck and handed over to a qualified hazardous waste treatment unit for treatment. After simple distillation, up to 80% of the acetic acid in the residue can be recovered, and the remaining acetic acid continues to evaporate during temporary storage and transportation, causing adverse effects on production and the ecological environment; 2. The distillation residue discharged during the production process is rinsed with a large amount of water, and a large amount of distillation residue water is sent to the sewage treatment process through the ditch; 3. The distillation residue is directly discharged into a special vehicle and transported to another place for treatment.
[0004] Disadvantages of the above treatment methods: Choosing a treatment method of flushing with a large amount of water and discharging it into the sewage treatment process will greatly increase the operation and maintenance cost of the sewage treatment process, and will also increase the great waste of water resources in the production process to a certain extent, as well as the increase in labor costs. The waste gas generated by the flushing process with a large amount of water will also cause serious environmental pollution problems; choosing to discharge it into the cofferdam for drying and then transporting it or directly discharge it into a special vehicle for transportation to other places for treatment will also cause great pollution to the environment or increase the cost of waste gas treatment. From this, it can be seen that it is necessary to seek a more appropriate, more economical, more efficient, and more environmentally friendly treatment method to solve the above problems to the greatest extent, so as to minimize the expenditure on manpower, material resources, and financial resources, and to improve the production and ecological environment to the greatest extent. Utility Model Content
[0005] In order to solve the adverse effects on production and the ecological environment caused by the continuous volatilization of harmful substances from the distillation residue during the above-mentioned stacking or storage process, and further reduce the consumption of acetic acid in the production process, the utility model provides a device for treating polyvinyl alcohol distillation residue, which greatly reduces the pollution to production and the ecological environment caused by the distillation residue in the production process of polyvinyl alcohol.
[0006] The utility model provides a device for treating polyvinyl alcohol distillation residue, which comprises an acetic acid residue tank for collecting acetic acid residues of various production systems, an acetic acid residue output pipeline of the acetic acid residue tank is connected with a low-temperature liquid inlet of a first residue evaporator, a high-temperature liquid outlet of the first residue evaporator is connected with a liquid inlet of a second residue evaporator via a pipeline, a residue output pipeline of the second residue evaporator is connected with a distillation residue inlet of a material-slag mixer, the material-slag mixer is provided with an acid gas outlet and a carbide slag inlet, a mixed material outlet for discharging mixed residues is provided at the bottom of the material-slag mixer, and the acid gas outlet is connected with an acid gas absorption tower via an acid gas delivery pipeline.
[0007] Furthermore, the gas output pipeline of the first residue evaporator is connected to the gas inlet of the residual liquid gas-liquid separator, the first residue evaporator is provided with a heating medium inlet and a heating medium outlet, a heating tube coiled from top to bottom in the first residue evaporator is connected between the heating medium inlet and the heating medium outlet, the heating medium inlet of the first residue evaporator is connected to the first heating medium input pipeline, the heating medium outlet of the first residue evaporator is connected to the first heating medium output pipeline, the acetic acid residual liquid entering the first residue evaporator from the acetic acid residual liquid output pipeline stays in the space outside the heating tube in the first residue evaporator, the high-temperature steam entering the heating tube in the first residue evaporator through the heating medium inlet of the first residue evaporator heats the acetic acid residual liquid, and the acetic acid vapor is transported to the residual liquid gas-liquid separator through the gas output pipeline of the first residue evaporator, and the heating medium may be, for example, water vapor.
[0008] Furthermore, a gas output pipeline of the second residue evaporator is connected to a gas inlet of the residue condenser, a heating medium inlet connected to a second heating medium input pipeline is opened on the second residue evaporator, the second heating medium input pipeline is communicated with an inner space of the second residue evaporator, an outlet of the second heating medium input pipeline extends to a middle and lower part of the second residue evaporator, a stirring blade is arranged inside the second residue evaporator, a jacket wrapping the second residue evaporator is arranged on an outer surface of the second residue evaporator, and the jacket is provided with a high temperature medium inlet connected to the high temperature medium input pipeline and a low temperature medium output pipeline connected to the low temperature medium output pipeline. The material outlet is preferably, the liquid inlet of the second residue evaporator is arranged in the middle and upper part, the residue output pipeline of the second residue evaporator is connected to the bottom, the high temperature medium (for example, water vapor) input into the second residue evaporator from the second heating medium input pipeline directly heats the material inside it, promotes the full decomposition of acetic anhydride and ethylene diacetate, the stirring blade stirs the material to prevent scaling, and the material in the second residue evaporator is heated by inputting high temperature medium (for example, high temperature water vapor) into the jacket, so that the acetic acid vapor in the material enters the residue condenser, and the distillation residue output from the bottom of the second residue evaporator is transported to the material-slag mixer. The function of the jacket is to ensure the temperature in the second residue evaporator, reduce temperature loss, and cooperate with the stirring blade to make the temperature in the second residue evaporator constant, so as to ensure the decomposition effect of acetic anhydride and ethylene diacetate; if there is no jacket and only steam is introduced, even with stirring blades, there will still be a temperature gradient for the second residue evaporator. For example, the temperature of the residual liquid close to the shell of the second residue evaporator is relatively low, so the decomposition effect of acetic anhydride and ethylene diacetate is relatively poor. Therefore, setting a jacket can reduce the temperature gradient and loss and keep the temperature in the second residue evaporator constant.
[0009] Furthermore, the liquid output pipe of the residue condenser returns to the acetic acid residual liquid tank. The residue condenser can be, for example, a shell and tube heat exchanger. The residue condenser is provided with a cooling medium inlet and a cooling medium outlet. The cooling medium inlet is connected to the cooling medium input pipe, and the cooling medium outlet is connected to the cooling medium output pipe. The cooling medium is, for example, chilled water.
[0010] Furthermore, the liquid outlet of the residual liquid gas-liquid separator is connected to the acetic acid residual liquid tank via a pipeline, and the gas output pipeline of the residual liquid gas-liquid separator is connected to the distillation tower.
[0011] Furthermore, an acetic acid residual liquid delivery pump is provided on the acetic acid residual liquid output pipeline of the acetic acid residual liquid tank.
[0012] Furthermore, the carbide slag inlet of the slag mixer is connected to the carbide slag discharge pipe of the carbide slag hopper.
[0013] Further, a slag mixer is arranged below the second residue evaporator, and the slag mixer comprises a lower inverted conical cylinder and an upper cylinder connected to the top of the inverted conical cylinder, the bottom end opening of the inverted conical cylinder is connected to a discharge pipe, a sealing valve is arranged on the discharge pipe, and the cylinder is a jacketed structure, comprising an inner cylinder for mixing distillation residue and carbide slag and an outer cylinder sleeved on the outside of the inner cylinder, the cylinder diameter of the inner cylinder may be, for example, 600-800 mm, the diameter of the outer cylinder may be, for example, 650-900 mm, the top edge of the inverted conical cylinder is connected to the bottom edge of the inner cylinder, and a plurality of air holes are opened on the side wall of the inner cylinder, The pores are regularly or irregularly distributed, and the pore diameter can be, for example, 5-10mm. A closed annular air chamber is formed between the inner tube and the outer tube. The outer tube is made of thermal insulation material, such as rock wool board. A hot air inlet connected to a hot air input pipe is opened on the side wall of the outer tube. A fan, preferably an explosion-proof fan, is arranged on the hot air input pipe. An electric heating wire is arranged at the air outlet of the fan for heating the air. The electric heating wire is interlocked with a temperature control device. A temperature measuring device is arranged on the hot air input pipe between the electric heating wire and the hot air inlet of the outer tube of the slag mixer, and the temperature measuring device is interlocked with the temperature control device. The distillation residue inlet, acid gas outlet and carbide slag inlet are all arranged on the top wall of the inner cylinder. The ratio of the diameter or equivalent diameter of the carbide slag inlet to the diameter or equivalent diameter of the distillation residue inlet can be 1.5-2.5:1, the diameter of the carbide slag inlet is preferably consistent with the diameter of the carbide slag discharge pipe, and the diameter of the distillation residue inlet is preferably consistent with the diameter of the residue output pipeline. The cold air (the wind pressure can be 100-200KPa, for example) blown into the hot air input pipeline by the fan is heated by the electric heating wire (to 50-80°C), the hot air enters the annular air bin, and then enters the inner cylinder through the air hole. The distillation residue and carbide slag enter the inner cylinder under the action of gravity. The hot air flow is used to dry the mixture ( Because the distillation residue and carbide slag contain a certain amount of moisture, they may block the discharge pipe and therefore need to be dried). On the other hand, they are used to mix the distillation residue and carbide slag. The hot air flow gives the distillation residue and carbide slag a radial force, so that the distillation residue and carbide slag entering the inner tube are in a mixed state, promoting the mixing of the two. The mixed slag enters the inverted cone tube for storage. After the mixing is completed, the sealing valve is opened to discharge the mixed slag, and the descending speed of the distillation residue and carbide slag is controlled, so that the distillation residue and carbide slag are temporarily stored in the residue output pipeline and the carbide slag discharge pipe respectively, to prevent the acid gas from being discharged through the residue output pipeline and the carbide slag discharge pipe, and to ensure that all the acid gas enters the acid gas transmission pipeline and is transported to the acid gas absorption tower.
[0014] Furthermore, a waste transfer vehicle is provided below the discharge pipe of the material-slag mixer, and the waste transfer vehicle is provided with a truck bucket for receiving the mixed material-slag.
[0015] Beneficial effects of the utility model:
[0016] The acetic acid residual liquid is heated and evaporated multiple times by the first residue evaporator and the second residue evaporator, thereby improving the recovery rate of acetic acid; by adding a slag mixer under the second residue evaporator, the second residue evaporator can completely discharge slag in a closed state, greatly reducing the environmental pollution caused by the overflow of acid gas; by inputting hot air into the slag mixer, the hot air mixes the distillation residue and the carbide slag and removes the moisture in the mixed slag, and at the same time, the hot air pushes the acid gas into the acid gas transmission pipeline, so that the acid gas enters the acid gas absorption tower to prevent the acid gas from overflowing. BRIEF DESCRIPTION OF THE DRAWINGS
[0017] Figure 1 The utility model is a schematic diagram of a device for treating polyvinyl alcohol distillation residue.
[0018] Figure 2 This is a schematic structural diagram of the slag mixer from the first perspective.
[0019] Figure 3 This is a schematic structural diagram of the slag mixer from a second perspective.
[0020] Figure 4 Schematic diagram of the inner cylinder.
[0021] Figure 5 This is a longitudinal section of the slag mixer.
[0022] Reference numerals:
[0023] 1- acetic acid residual liquid tank, 2- acetic acid residual liquid delivery pump, 3- residual liquid gas-liquid separator, 4- first residue evaporator, 5- second residue evaporator, 6- residue condenser, 7- material slag mixer, 71- distillation residue inlet, 72- acid gas outlet, 73- carbide slag inlet, 74- inverted cone cylinder, 75- cylinder, 751- inner cylinder, 752- outer cylinder, 753- air hole, 754- annular gas bin, 8- carbide slag hopper, 81- carbide slag discharge pipe, 9- electric heating wire, 10- fan, 11- waste transfer vehicle, 12- acid gas absorption tower, 13- discharge pipe, 14- stirring blade, 15- jacket;
[0024] L1-acetic acid residual liquid output pipeline, L2-first heating medium input pipeline, L3-first heating medium output pipeline, L4-second heating medium input pipeline, L5-high temperature medium input pipeline, L6-low temperature medium output pipeline, L7-residue output pipeline, L8-gas output pipeline of the second residue evaporator, L9-acid gas transmission pipeline, L10-hot air input pipeline. DETAILED DESCRIPTION
[0025] The utility model is further described below in conjunction with the accompanying drawings.
[0026] like Figure 1-5As shown, the utility model provides a device for treating polyvinyl alcohol distillation residue, which includes an acetic acid residue tank 1 for collecting acetic acid residues of various production systems, the acetic acid residue output pipeline L1 of the acetic acid residue tank 1 is connected to the low-temperature liquid inlet of the first residue evaporator 4, the high-temperature liquid outlet of the first residue evaporator 4 is connected to the liquid inlet of the second residue evaporator 5 through a pipeline, the residue output pipeline L7 of the second residue evaporator 5 is connected to the distillation residue inlet 71 of the material-slag mixer 7, the material-slag mixer 7 is provided with an acid gas outlet 72 and a carbide slag inlet 73, the bottom of the material-slag mixer 7 is provided with a mixed material outlet for discharging the mixed residue, and the acid gas outlet 72 is connected to the acid gas absorption tower 12 through the acid gas delivery pipeline L9.
[0027] The carbide slag inlet 73 of the slag mixer 7 is connected to the carbide slag discharge pipe 81 of the carbide slag hopper 8. The slag mixer 7 is arranged below the second residue evaporator 5. The slag mixer 7 includes a lower inverted conical cylinder 74 and an upper cylinder 75 connected to the top of the inverted conical cylinder 74. The bottom end opening of the inverted conical cylinder 74 is connected to the discharge pipe 13. The discharge pipe 13 is provided with a sealing valve. The cylinder 75 is a jacketed structure. The cylinder 75 includes an inner cylinder 751 and an annular ring for mixing the distillation residue and the carbide slag. The outer cylinder 752 is sleeved on the outer side of the inner cylinder 751. The diameter of the inner cylinder 751 can be, for example, 600-800 mm, and the diameter of the outer cylinder 752 can be, for example, 650-900 mm. The top edge of the inverted cone cylinder 74 is connected to the bottom edge of the inner cylinder 751. A plurality of air holes 753 are opened on the side wall of the inner cylinder 751. The air holes 753 are regularly or irregularly distributed. The diameter of the air holes 753 can be, for example, 5-10 mm. A closed annular air chamber 754 is formed between the inner cylinder 751 and the outer cylinder 752. The outer cylinder 752 is made of thermal insulation material, for example, it can be a rock wool board. A hot air inlet connected to the hot air input pipe L10 is opened on the side wall of the outer cylinder 752. The hot air input pipe L10 is provided with a fan 10, which is preferably an explosion-proof fan to ensure safe operation on site. The air outlet of the fan 10 is provided with an electric heating wire 9 for heating the air. The electric heating wire is interlocked with the temperature control device. The hot air input pipe L10 between the electric heating wire and the hot air inlet of the outer cylinder of the slag mixer 7 is provided with a temperature measuring device. The temperature measuring device is interlocked with the temperature control device. The temperature measuring device can be, for example, a temperature sensor, and the temperature control device can be, for example, a programmable logic controller. With this arrangement, the temperature measuring device transmits the measured temperature of the air in the hot air input pipe to the temperature control device. The temperature control device adjusts the power of the electric heating wire 9 according to the air temperature. When the air temperature is higher than the set temperature, the power of the electric heating wire 9 is turned down; when the air temperature is lower than the set temperature, the power of the electric heating wire 9 is increased.The distillation residue inlet 71, the acid gas outlet 72 and the carbide slag inlet 73 are all arranged on the top wall of the inner cylinder 751. The ratio of the diameter or equivalent diameter of the carbide slag inlet 73 to the diameter or equivalent diameter of the distillation residue inlet 71 can be 1.5-2.5:1. The diameter of the carbide slag inlet 73 is preferably consistent with the diameter of the carbide slag discharge pipe 81. The diameter of the distillation residue inlet 71 is preferably consistent with the diameter of the residue output pipeline L7. The cold air blown into the hot air input pipeline L10 by the fan 10 is heated by the electric heating wire 9 (to 50-80°C), and the hot air enters the annular air bin 754, and then enters the inner cylinder 751 through the air hole 753. The distillation residue and the carbide slag enter the inner cylinder 751 under the action of gravity. The hot air flow is used to dry the mixture. The hot air flow exerts radial force on the distillation residue and the carbide slag, so that the distillation residue and the carbide slag entering the inner cylinder 751 are in a mixed state, which promotes the mixing of the two. The mixed slag enters the inverted cone cylinder 74 for storage. After the mixing is completed, the sealing valve is opened to discharge the mixed slag, and the descending speed of the distillation residue and the carbide slag is controlled, so that the distillation residue and the carbide slag are temporarily stored in the residue output pipeline L7 and the carbide slag discharge pipe 81 respectively, to prevent the acid gas from being discharged through the residue output pipeline L7 and the carbide slag discharge pipe 81, and to ensure that all the acid gas enters the acid gas delivery pipeline L9 and is delivered to the acid gas absorption tower.
[0028] The gas output pipeline of the first residue evaporator 4 is connected to the gas inlet of the residual liquid gas-liquid separator 3. The first residue evaporator 4 is provided with a heating medium inlet and a heating medium outlet. A heating pipe is connected between the heating medium inlet and the heating medium outlet and is coiled from top to bottom in the first residue evaporator 4. The heating medium inlet of the first residue evaporator 4 is connected to the first heating medium input pipeline L2, and the heating medium outlet of the first residue evaporator 4 is connected to the first heating medium output pipeline L3. The acetic acid residual liquid entering the first residue evaporator 4 from the acetic acid residual liquid output pipeline L1 stays in the space outside the heating pipe in the first residue evaporator 4, enters the acetic acid residual liquid through the heating medium inlet of the first residue evaporator 4, and is heated by the high-temperature steam of the first residue evaporator 4. The acetic acid vapor generated by the heating is transported to the residual liquid gas-liquid separator 3 through the gas output pipeline of the first residue evaporator 4. The heating medium may be, for example, water vapor.
[0029] The gas output pipeline L8 of the second residue evaporator 5 is connected to the gas inlet of the residue condenser 6, the second residue evaporator 5 is provided with a heating medium inlet connected to the second heating medium input pipeline L4, the second heating medium input pipeline L4 is communicated with the internal space of the second residue evaporator 5, the second heating medium input pipeline L4 extends to the middle and lower part of the second residue evaporator 5, a stirring blade 14 is provided inside the second residue evaporator 5, the outer surface of the second residue evaporator 5 is provided with a jacket 15 wrapping the second residue evaporator 5, the jacket 15 is provided with a high temperature medium inlet connected to the high temperature medium input pipeline L5 and a low temperature medium output pipeline L6 connected to the low temperature medium output pipeline L6. Medium outlet, preferably, the liquid inlet of the second residue evaporator 5 is arranged in the middle and upper part, the residue output pipe L7 of the second residue evaporator 5 is connected to the bottom, and the high-temperature medium (for example, water vapor) input into the second residue evaporator 5 from the second heating medium input pipe L4 directly heats the material inside it, promotes the full decomposition of acetic anhydride and ethylene diacetate, and the stirring blade 14 stirs the material to prevent scaling. By inputting high-temperature medium (for example, high-temperature water vapor) into the jacket 15 to heat the material in the second residue evaporator 5, the acetic acid vapor in the material is prompted to enter the residue condenser 6, and the distillation residue output from the bottom of the second residue evaporator 5 is transported to the material-slag mixer 7.
[0030] The liquid output pipeline of the residue condenser 6 returns to the acetic acid residual liquid tank 1. The residue condenser 6 can be, for example, a shell and tube heat exchanger. The residue condenser 6 is provided with a cooling medium inlet and a cooling medium outlet. The cooling medium inlet is connected to the cooling medium input pipeline, and the cooling medium outlet is connected to the cooling medium output pipeline. The cooling medium is, for example, chilled water.
[0031] The liquid outlet of the residual liquid gas-liquid separator 3 is connected to the acetic acid residual liquid tank 1 through a pipeline, and the gas output pipeline of the residual liquid gas-liquid separator 3 is connected to the distillation tower.
[0032] An acetic acid residual liquid delivery pump 2 is provided on the acetic acid residual liquid output pipeline L1 of the acetic acid residual liquid tank 1 .
[0033] A waste transfer vehicle 11 is provided below the discharge pipe 13 of the material-slag mixer 7 , and the waste transfer vehicle 11 is provided with a bucket for receiving the mixed material-slag. Example
[0034] (1) The acetic acid residue (80-85% acetic acid, 1-2% water, 6-10% ethylene diacetate, and other impurities such as crotonaldehyde and acetaldehyde, with a flow rate of about 25L / min) enters the first residue evaporator through the acetic acid residue output pipeline, enters the first residue evaporator through the heating medium inlet of the first residue evaporator, and heats the acetic acid residue with water vapor at about 220-240°C. The acetic acid vapor output from the top of the first residue evaporator is transported to the residue gas-liquid separator (the function of the residue gas-liquid separator is to separate the acetic acid vapor from the top of the first residue evaporator into gas and liquid). The liquid phase separated by the residue gas-liquid separator is returned to the acetic acid residue tank, and the separated gas phase is transported to the distillation tower as a raw material. The liquid output from the bottom of the first residue evaporator (60% acetic acid, about 30% acid anhydride, ethylene diacetate, etc., and about 10% activated carbon powder) enters the second residue evaporator;
[0035] (2) Steam at about 220-240°C is inputted into the second residue evaporator from the second heating medium input pipeline to directly heat the material in the second residue evaporator, promoting the full decomposition of acetic anhydride and ethylene diacetate. The stirring blade stirs the material to prevent scaling. At the same time, steam at about 220-240°C is inputted into the jacket to heat the material in the second residue evaporator, causing the acetic acid vapor in the material to enter the residue condenser. After condensation in the residue condenser, it is transported to the acetic acid residual liquid tank for circulation. The distillation residue (the mass proportion of each component is: acetic acid about 20-30%, water about 10-15%, activated carbon powder about 20%, tar and ethylene ester high boiling products about 20% and other impurities) outputted from the bottom of the second residue evaporator is transported to the material-slag mixer;
[0036] (3) The carbide slag in the carbide slag hopper (average particle size is 14 mesh, the mass proportion of each component is: calcium hydroxide and magnesium hydroxide about 88%, aluminum trioxide, iron trioxide and silicon dioxide about 9%, water about 3%) is discharged into the inner cylinder of the slag mixer. The feeding rate of the carbide slag is 50L / min. After being mixed with the distillation residue entering the inner cylinder (feeding rate is 25L / min), it is temporarily stored in the inverted cone cylinder. At the same time, the electric heating wire and the fan are turned on to deliver hot air to the annular air bin. The temperature is 50-80℃, the wind pressure is 100-200KPa, and the hot air The acid gas generated during the mixing process enters the inner cylinder through the air holes. The acid gas transported to the acid gas absorption tower through the acid gas transmission pipeline. After the mixing is completed, the sealing valve is opened to discharge the mixed material residue (the mass proportion of the components is: calcium hydroxide, magnesium hydroxide, calcium acetate, magnesium acetate is about 73.5%, water is about 0.5%, carbon powder is about 5%, tar and ethylene ester high boiling products are about 5%, aluminum oxide, iron oxide and silicon dioxide are about 6.75%) to the truck bed of the transfer vehicle, and then transported to the designated area (such as the cement plant incinerator). The incinerated mixed material residue can be supplied to the cement plant to prepare cement products.
[0037] The above describes the preferred embodiments of the present invention, however, the above description is not intended to be limiting. A person skilled in the art may make many changes or modifications to the present invention without departing from the spirit and scope of the present invention. The changes or modifications should be included in the scope of the appended claims.
Claims
1. A device for treating polyvinyl alcohol distillation residue, characterized in that: The invention comprises an acetic acid residual liquid tank (1) for collecting acetic acid residual liquid of each production system, an acetic acid residual liquid output pipeline (L1) of the acetic acid residual liquid tank (1) is connected to a low-temperature liquid inlet of a first residue evaporator (4), a high-temperature liquid outlet of the first residue evaporator (4) is connected to a liquid inlet of a second residue evaporator (5) via a pipeline, a residue output pipeline (L7) of the second residue evaporator (5) is connected to a rectification residue inlet (71) of a material-slag mixer (7), the material-slag mixer (7) is provided with an acid gas outlet (72) and a carbide slag inlet (73), a mixed material outlet for discharging mixed residue is provided at the bottom of the material-slag mixer (7), and the acid gas outlet (72) is connected to an acid gas absorption tower (12) via an acid gas delivery pipeline (L9).
2. The device for treating polyvinyl alcohol distillation residue according to claim 1, characterized in that: The carbide slag inlet (73) of the material-slag mixer (7) is connected to the carbide slag discharge pipe (81) of the carbide slag hopper (8), and the material-slag mixer (7) is arranged below the second residue evaporator (5).
3. The device for treating polyvinyl alcohol distillation residue according to claim 1 or 2, characterized in that: The material-slag mixer (7) comprises a lower inverted conical cylinder (74) and an upper cylinder (75) connected to the top of the inverted conical cylinder (74). The bottom opening of the inverted conical cylinder (74) is connected to a discharge pipe (13). A sealing valve is provided on the discharge pipe (13). The cylinder (75) is a jacketed structure. The cylinder (75) comprises an inner cylinder (751) for mixing the rectification residue and the carbide slag and an outer cylinder (752) sleeved on the outside of the inner cylinder (751). The top edge of the outer tube (74) is connected to the bottom edge of the inner tube (751), a plurality of air holes (753) are formed on the side wall of the inner tube (751), a closed annular air chamber (754) is formed between the inner tube (751) and the outer tube (752), a hot air inlet connected to the hot air input pipeline (L10) is formed on the side wall of the outer tube (752), and a distillation residue inlet (71), an acid gas outlet (72) and a carbide slag inlet (73) are all arranged on the top wall of the inner tube (751).
4. The device for treating polyvinyl alcohol distillation residue according to claim 3, characterized in that: A fan (10) is provided on the hot air input pipeline (L10), an electric heating wire (9) is provided at the air outlet of the fan (10), the electric heating wire (9) is interlocked with a temperature control device, and a temperature measuring device is provided on the hot air input pipeline (L10) between the electric heating wire (9) and the hot air inlet of the outer cylinder of the material-slag mixer (7), and the temperature measuring device is interlocked with the temperature control device.
5. The device for treating polyvinyl alcohol distillation residue according to claim 1, characterized in that: The gas output pipeline of the first residue evaporator (4) is connected to the gas inlet of the residual liquid gas-liquid separator (3); the first residue evaporator (4) is provided with a heating medium inlet and a heating medium outlet; a heating pipe is connected between the heating medium inlet and the heating medium outlet and is wound from top to bottom in the first residue evaporator (4); the heating medium inlet of the first residue evaporator (4) is connected to the first heating medium input pipeline (L2); and the heating medium outlet of the first residue evaporator (4) is connected to the first heating medium output pipeline (L3).
6. The device for treating polyvinyl alcohol distillation residue according to claim 1, characterized in that: The gas output pipe (L8) of the second residue evaporator (5) is connected to the gas inlet of the residue condenser (6); the second residue evaporator (5) is provided with a heating medium inlet connected to the second heating medium input pipe (L4); the second heating medium input pipe (L4) is communicated with the internal space of the second residue evaporator (5); the second heating medium input pipe (L4) extends to the middle and lower part of the second residue evaporator (5); a stirring blade (14) is provided inside the second residue evaporator (5); the outer surface of the second residue evaporator (5) is provided with a jacket (15) wrapping the second residue evaporator (5); the jacket (15) is provided with a high-temperature medium inlet connected to the high-temperature medium input pipe (L5) and a low-temperature medium outlet connected to the low-temperature medium output pipe (L6); and the residue output pipe (L7) of the second residue evaporator (5) is connected to the bottom.
7. The device for treating polyvinyl alcohol distillation residue according to claim 6, characterized in that: The liquid output pipeline of the residue condenser (6) returns to the acetic acid residual liquid tank (1). The residue condenser (6) is provided with a cooling medium inlet and a cooling medium outlet. The cooling medium inlet is connected to the cooling medium input pipeline, and the cooling medium outlet is connected to the cooling medium output pipeline.
8. The device for treating polyvinyl alcohol distillation residue according to claim 5, characterized in that: The liquid outlet of the residual liquid gas-liquid separator (3) is connected to the acetic acid residual liquid tank (1) via a pipeline, and the gas output pipeline of the residual liquid gas-liquid separator (3) is connected to the distillation tower.
9. The device for treating polyvinyl alcohol distillation residue according to claim 1, characterized in that: An acetic acid residual liquid delivery pump (2) is provided on the acetic acid residual liquid output pipeline (L1) of the acetic acid residual liquid tank (1).
10. The device for treating polyvinyl alcohol distillation residue according to claim 3, characterized in that: A waste transfer vehicle (11) is provided below the discharge pipe (13) of the material-slag mixer (7), and the waste transfer vehicle (11) is provided with a bucket for receiving the mixed material-slag.