Psicose crystal separating and drying device
By designing a paclitaxel crystal separation and drying device that integrates the negative pressure separation process and separation and drying, the paclitaxel crystallization problem in the prior art is solved, and the separation and drying cycle and production cost are shortened.
Patent Information
- Application Number
- CN202420723366.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-04-09
- Publication Date
- 2025-03-25
- Estimated Expiration
- 2034-04-09
AI Technical Summary
The existing paclitaxel-water system crystallization process has problems such as difficult crystallization, large equipment area, high maintenance cost, high energy consumption and high noise, and the paclitaxel-ethanol system crystallization process requires the redesign and manufacture of new process equipment.
A paclitaxel crystal separation and drying device is designed, including a reactor equipped with a jacket. The reactor is divided into a separation chamber and a filtrate chamber through a sintered net. The negative pressure separation process is used to design it in one piece, which shortens the separation and drying cycle.
It effectively shortens the separation and drying cycle, reduces production floor area, reduces noise, energy consumption and maintenance costs, and avoids material pollution and losses.
Smart Images
Figure CN222658642U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of starch sugar processing, and specifically relates to a device for separating and drying allulose crystals. Background Art
[0002] The production of allulose is usually based on fructose as a substrate and is generated under the catalysis of D-psicose 3-epimerase. The solubility of allulose in water and in ethanol systems is different, so there are water crystallization processes and ethanol crystallization processes. The current traditional crystallization process adopts the allulose-water system crystallization process. Because allulose has a large solubility in aqueous solution and is difficult to crystallize, the back-end process of the traditional allulose-water system crystallization process often uses a high-speed centrifuge to separate the crystals from the mother liquor, and then further uses a fluidized bed to dry the crystals. The high-speed centrifuge and fluidized bed used in the current process occupy a large space and have problems such as high maintenance cost, high energy consumption, and high noise. If the allulose-ethanol system crystallization process is used for production, due to the low viscosity of the sugar paste obtained in the allulose-ethanol crystallization system and the small crystal particles, the traditional crystal separation and drying equipment is not suitable for this crystallization system, and new process equipment needs to be redesigned and manufactured. Summary of the invention
[0003] The technical problem to be solved by the utility model is to provide a D-psicose crystal separation and drying device, which is suitable for the D-psicose-ethanol crystallization process, and the separation and drying cycle is effectively shortened. At the same time, the defects of the existing process equipment, such as long production cycle, large floor space, high maintenance cost, high energy consumption and high noise, are overcome.
[0004] In order to solve the above technical problems, the technical solution of the utility model is:
[0005] A device for separating and drying allulose crystals comprises a reactor provided with a jacket, wherein a pressure gauge, a vacuum port, a pressure balance port and a feed port are provided on the top of the reactor, and a stirring device and a washing device are provided which penetrate from the top of the reactor into the inner cavity of the reactor; a filtrate outlet is provided at the bottom of the reactor, and the filtrate outlet is externally connected to a first ethanol recovery tank; the inner cavity of the reactor is divided into a separation cavity and a filtrate cavity by a sintered mesh arranged at the bottom of the inner cavity, a crystal outlet is provided on a side wall of the reactor on one side of the upper part of the sintered mesh, and the crystal outlet is connected to a screw feeder and a vibrating screen in sequence through a stop valve and a pipeline; the vibrating screen is provided with a finished product discharge port and a coarse material discharge port, the finished product discharge port is connected to a weighing and packaging device, and the coarse material discharge port is connected to a pulverizer and a cyclone separator in sequence through a pipeline; the discharge port of the cyclone separator is connected to the vibrating screen, and the air outlet of the cyclone separator is connected to a dust removal device.
[0006] Preferably, the jacket is a water circulation jacket, with a circulating water inlet at the bottom and a circulating water outlet at the top. The circulating water inlet and the circulating water outlet are connected to the circulating water supply device and the circulating water recovery device through pipelines and valves respectively. The circulating water temperature is set to 40°C to 80°C.
[0007] Preferably, the vacuum port is connected to the first vacuum valve, the second vacuum valve and the first ethanol recovery tank through pipelines respectively, the first vacuum valve is also connected to the steam-water separator through a pipeline, and the steam-water separator is connected to the vacuum pump and the second ethanol recovery tank respectively.
[0008] Preferably, the stirring paddle of the stirring device is a double-layer anchor-type stirring paddle.
[0009] Furthermore, the distance between the end of the stirring paddle of the stirring device and the side wall of the inner cavity of the reactor is 30 mm to 300 mm, and the distance between the bottom of the stirring paddle and the upper part of the sintering net is 30 mm to 300 mm.
[0010] Preferably, the washing device comprises a circular pipe arranged at the upper part of the inner cavity of the reactor and surrounding the stirring shaft of the stirring device, and a plurality of vertically downward atomizing nozzles are evenly arranged on the circular pipe, and the feed end of the circular pipe passes through the top of the reactor and is respectively connected to the compressed air input device and the ethanol input device.
[0011] Furthermore, the aperture of the atomizing nozzle is 0.3 mm to 0.6 mm, and the interval is 300 mm to 600 mm.
[0012] Preferably, the sintered mesh is a stainless steel sintered mesh with a mesh size of 200 to 1000 meshes.
[0013] Preferably, the vacuum pump is a SKA (2BV)-2071 vacuum pump produced by Shanghai Sunshine Pump Industry; the screw feeder is a LS400 screw feeder of Xinxiang Hongyun Mining Machinery; the steam-water separation device is a vertical T-type steam-water separator produced by Xinxiang Matt Filtration Equipment Co., Ltd.; the vibrating screen is a GFBD-A swing screen produced by Xinxiang Gaofu Machinery Co., Ltd.; the grinder is a GFJ300 high-efficiency grinder produced by Kunshan Qiangwei Powder Equipment Co., Ltd.; and the cyclone separator is a XZZ model cyclone separator produced by Huaning Environmental Protection Technology Co., Ltd.
[0014] Due to the adoption of the above technical solution, the beneficial effects of the utility model are:
[0015] 1. The utility model sets the separation and drying processes in one reactor, which shortens the production cycle and reduces the production area;
[0016] 2. The process of separating crystals and mother liquor in the utility model is different from that of the traditional centrifuge, and the noise, energy consumption and maintenance cost are all improved;
[0017] 3. After the separation operation is completed in the utility model, the material does not need to be transferred and can be dried directly in the reactor, thus avoiding the problems of material contamination and loss between the separation process and the drying process in the traditional process.
[0018] In summary, the utility model is suitable for the allulose-ethanol crystallization process. The negative pressure separation process and separation and drying are integrated into one design of the equipment, so that the separation and drying cycle is effectively shortened. At the same time, it also overcomes the defects of the equipment used in the prior art, such as long production cycle, large footprint, high maintenance cost, high energy consumption, and high noise. BRIEF DESCRIPTION OF THE DRAWINGS
[0019] Figure 1 This is a schematic diagram of the structure of the first embodiment of the utility model;
[0020] In the figure, 1, jacket; 2, reactor; 3, stirring device; 4, washing device; 5, first vacuum valve; 6, second vacuum valve; 7, first ethanol recovery tank; 8, gas-water separator; 9, vacuum pump; 10, second ethanol recovery tank; 11, sintering net; 12, screw feeder; 13, vibrating screen; 14, weighing and packaging device; 15, crusher; 16, cyclone separator; 17, dust removal device. DETAILED DESCRIPTION
[0021] The present invention is further described below in conjunction with the accompanying drawings and embodiments.
[0022] Embodiment 1:
[0023] like Figure 1As shown, a device for separating and drying allulose crystals comprises a reactor 2 provided with a jacket 1, a pressure gauge (not marked), a vacuum port (not marked), a pressure balance port (not marked) and a feed port (not marked) being provided on the top of the reactor 2, and a stirring device 3 and a washing device 4 penetrating from the top of the reactor 2 into the inner cavity of the reactor are also provided; the vacuum port is connected to a first vacuum valve 5, a second vacuum valve 6 and a first ethanol recovery tank 7 respectively through a pipeline (not marked), the first vacuum valve 5 is further connected to a steam-water separator 8 through a pipeline, and the steam-water separator 8 is respectively connected to a vacuum pump 9 and a second ethanol recovery tank 10; a filtrate outlet (not marked) is provided at the bottom of the reactor 2, and the filtrate outlet is externally connected to the first ethanol recovery tank 7. Alcohol recovery tank 7; the inner cavity of the reactor 2 is divided into a separation cavity (not marked) and a filtrate cavity (not marked) by a sintered mesh 11 arranged at the bottom of the inner cavity, and a crystal outlet (not marked) is provided on the side wall of the reactor 2 on the upper side of the sintered mesh 11, and the crystal outlet is connected to the screw feeder 12 and the vibrating screen 13 in sequence through a stop valve (not marked) and a pipeline; the vibrating screen 13 is provided with a finished product discharge port (not marked) and a coarse material discharge port (not marked), the finished product discharge port is connected to the weighing and packaging device 14, and the coarse material discharge port is connected to the crusher 15 and the cyclone separator 16 in sequence through a pipeline; the discharge port of the cyclone separator is connected to the vibrating screen 13, and the air outlet of the cyclone separator 16 is connected to the dust removal device 17.
[0024] The washing device 4 includes a circular pipe (not marked) arranged in the upper part of the inner cavity of the reactor 2 and surrounding the stirring shaft of the stirring device 3. A plurality of vertically downward atomizing nozzles (not marked) are evenly arranged on the circular pipe. The feed end of the circular pipe passes through the top of the reactor and is respectively connected to a compressed air input device (not marked) and an ethanol input device (not marked).
[0025] In actual production, the stop valve at the crystal outlet of the reactor 2 is closed, and the crystallized sugar paste obtained in the previous process is transported from the feed port of the reactor 2 to the separation chamber inside the reactor 2. After the feeding is completed, the feed port and the first vacuum valve 5 are closed in sequence, the pressure balance port, the second vacuum valve 6, and the filtrate outlet are opened, and the vacuum pump 9 is turned on to intercept the crystals in the sugar paste through the sintered mesh 11. The mother liquor enters the filtrate chamber through the sintered mesh 11 under the action of negative pressure and is transported to the first ethanol recovery tank 7 through the filtrate outlet for temporary storage. The volatilized ethanol is further recovered into the second ethanol recovery tank 10 through the steam-water separator 8. During the separation period, the ethanol transported by the ethanol input device is mixed with the compressed air and sprayed onto the crystal surface for washing through the atomizing nozzle of the washing device 4. After the separation is completed, the pressure balance port, the second vacuum valve 6, and the filtrate outlet are closed, and then the first vacuum valve is opened. 5. Open the circulating water of the jacket 1 for heating and drying. The residual ethanol in the crystals is volatilized and then recovered to the second ethanol recovery tank 10 through the steam-water separator 8. After drying, close the vacuum pump 9, the first vacuum valve 5, the circulating water inlet and the circulating water outlet of the jacket 1, open the pressure balance port and the stop valve, and drive the stirring device 3 to scrape the dried materials on the stainless steel sintered mesh 11 and the inner wall of the reactor 2 and send them to the screw feeder 12 through the stop valve, and then the screw feeder 12 is transported to the vibrating screen 13 for screening, and the finished products are transported to the weighing and packaging device 14 for packaging, and the coarse products are transported to the pulverizer 15 for further pulverization, and then transported to the cyclone separator 16 for separation, and the separated particles are returned to the vibrating screen 13 for further screening; the gas in the cyclone separator 16 is dedusted by the dust removal device 17 and then discharged.
[0026] It should be understood that these embodiments are only used to illustrate the present invention and are not used to limit the scope of the present invention. In addition, it should be understood that after reading the content taught by the present invention, those skilled in the art can make various changes or modifications to the present invention, and these equivalent forms also fall within the scope defined by the claims attached to this application.
Claims
1. A device for separating and drying psicose crystals, characterized in that: It comprises a reactor provided with a jacket, a stirring device and a washing device, wherein a pressure gauge, a vacuum port, a pressure balance port and a feed port are provided on the top of the reactor; a filtrate outlet is provided at the bottom of the reactor, and the filtrate outlet is externally connected to a first ethanol recovery tank; the inner cavity of the reactor is divided into a separation cavity and a filtrate cavity by a sintered mesh arranged at the bottom of the inner cavity, a crystal outlet is provided on the side wall of the reactor on the upper side of the sintered mesh, and the crystal outlet is connected to a screw feeder and a vibrating screen in sequence through a stop valve and a pipeline; the vibrating screen is provided with a finished product discharge port and a coarse material discharge port, the finished product discharge port is connected to a weighing and packaging device, and the coarse material discharge port is connected to a crusher and a cyclone separator in sequence through a pipeline; the discharge port of the cyclone separator is connected to the vibrating screen, and the air outlet of the cyclone separator is connected to a dust removal device.
2. The device for separating and drying psicose crystals according to claim 1, wherein: The jacket is a water circulation jacket, with a circulating water inlet at the bottom and a circulating water outlet at the top.
3. The device for separating and drying psicose crystals according to claim 1, wherein: The vacuum port is connected to the first vacuum valve, the second vacuum valve and the first ethanol recovery tank through pipelines respectively. The first vacuum valve is also connected to the steam-water separator through a pipeline. The steam-water separator is connected to a vacuum pump and the second ethanol recovery tank respectively.
4. The device for separating and drying psicose crystals according to claim 1, wherein: The stirring paddle of the stirring device is a double-layer anchor-type stirring paddle.
5. The device for separating and drying psicose crystals according to claim 4, wherein: The distance between the end of the stirring paddle and the side wall of the inner cavity of the reactor is 30 mm to 300 mm, and the distance between the bottom of the stirring paddle and the upper part of the sintering net is 30 mm to 300 mm.
6. The device for separating and drying psicose crystals according to claim 1, wherein: The washing device comprises a circular pipe arranged at the upper part of the inner cavity of the reactor and surrounding the stirring shaft of the stirring device. A plurality of vertically downward atomizing nozzles are evenly arranged on the circular pipe. The feed end of the circular pipe passes through the top of the reactor and is respectively connected to the compressed air input device and the ethanol input device.
7. The device for separating and drying psicose crystals according to claim 6, wherein: The aperture of the atomizing nozzle is 0.3 mm to 0.6 mm, and the interval is 300 mm to 600 mm.
8. The device for separating and drying psicose crystals according to claim 1, wherein: The mesh size of the sintered mesh is 200-1000 meshes.