Integrated device for desalting and concentrating glycerol residue

Abstract

This invention discloses an integrated treatment device for glycerol residue desalination and glycerol concentration, relating to the technical field of glycerol residue treatment equipment. It includes a centrifuge base and a centrifuge body fixed on the centrifuge base. The centrifuge body contains a centrifugal mechanism for desalting the glycerol residue. A concentration base is located on one side of the centrifuge base, and a concentration mechanism for concentrating glycerol is installed on the concentration base. During operation, this integrated treatment device achieves continuous solid-liquid separation through the centrifugal mechanism. The feeding, material separation, solid phase discharge, and liquid phase discharge processes run uninterruptedly, achieving stable and efficient separation results. It also possesses the technical advantages of large single-unit processing capacity and high degree of automation. Through the concentration mechanism, the material repeatedly completes film formation, evaporation, and downward movement processes, continuously achieving evaporation and concentration with sufficient heat exchange, significantly reducing production energy consumption.

Description

Technical Field

[0001] This invention relates to the technical field of glycerol residue treatment equipment, specifically an integrated treatment device for glycerol residue desalination and glycerol concentration. Background Technology

[0002] Glycerin residue is the residue after glycerin distillation in biodiesel or oleochemical production. It contains high concentrations of salt (mainly sodium chloride), glycerin, polyglycerol, and impurities. Its salt treatment is not only related to resource recovery, but also directly affects environmental protection costs.

[0003] With the development of the world economy and the continuous advancement of science and technology, the contradiction between rising production costs and shrinking resources has become increasingly prominent. How to effectively improve the high-value recycling of chemical solid waste is one of the common concerns of countries around the world and a key to achieving sustainable development. Improving the high-value recycling of industrial solid waste in the chemical industry is a way for enterprises to reduce costs and increase efficiency. It is also a way to recycle resources, reduce the generation of solid waste, lower treatment costs, and reduce the pollution of solid waste to the environment. Glycerin residue desalination and biogas production are important manifestations of enterprises enhancing their market competitiveness in environmental protection, cost control, and sustainable development.

[0004] For example, patent CN120662243A discloses a method for the combined treatment of glycerol salts obtained from crude glycerol refining and polyglycerol residue. This method first washes the glycerol salts with water to obtain washed salt and washed brine. The washed brine is mixed and dissolved with clean water to obtain causticized brine, which is then subjected to advanced oxidation technology to deeply oxidize the organic matter in the brine to the standard for chlor-alkali brine using an ion-exchange membrane, achieving resource recycling. The washed brine is mixed and dissolved with the polyglycerol residue, and under a strong acid environment, it reacts to generate water-insoluble fatty acids and NaCl salts that crystallize out due to supersaturation, resulting in a three-phase mixture. This mixture is then separated into solid NaCl salt, fatty acids, and a polyglycerol solution by a three-phase separator. The polyglycerol solution is subsequently neutralized, desalted by electrodialysis, concentrated by distillation, and decolorized to obtain a bright yellow or pale yellow polyglycerol product containing more than 90% glycerol and polyglycerol by weight.

[0005] For example, patent CN104230083A discloses a method for recovering and treating sodium chloride and glycerol from high-salt, high-concentration organic wastewater containing glycerol. The method includes complexation, nanofiltration desalination, evaporation concentration, crystallization, decomplexation, separation of glycerol from copper hydroxide or other metal hydroxides, nanofiltration separation of glycerol, reverse osmosis concentration of glycerol, distillation concentration of glycerol, and fractionation. Wastewater treated by this method has reduced salinity. After dilution, a biochemical treatment process is applied to ensure the effluent meets standards, while sodium chloride and glycerol are effectively recovered. The purity of the finished glycerol reaches 95%.

[0006] For example, the patent with announcement number CN205055535U discloses an alternating desalination device for glycerol distillation to remove salts. The first tank has a first feed pipe connected to its interior, with a first valve on the feed pipe. A first filter screen and the first tank form a first filter chamber. The first tank has at least one first drain pipe connected to the first filter chamber on its exterior, and a first compressed gas input pipe connected to the tank on its exterior. The second tank has a second feed pipe connected to its interior, with a second valve on the feed pipe. A second filter screen and the second tank form a second filter chamber. The second tank has at least one second drain pipe connected to the second filter chamber on its exterior, and a second compressed gas input pipe connected to the tank on its exterior. This device can separate the salts precipitated from crude glycerol after distillation.

[0007] When using existing integrated desalting and concentration equipment for glycerol residue, traditional glycerol residue treatment processes suffer from low precision in manual control, poor separation of highly viscous and easily agglomerated materials, severe corrosion of equipment in high-salt media, disconnect between desalting and concentration processes, large transfer losses, and high energy consumption.

[0008] To address the aforementioned issues, there is an urgent need for innovative design based on the existing glycerol residue treatment equipment structure. Summary of the Invention

[0009] The purpose of this invention is to provide an integrated treatment device for glycerol residue desalination and glycerol concentration, in order to solve the problems of traditional glycerol residue treatment processes mentioned in the background art, such as low precision of manual control, poor separation effect of high viscosity and easily agglomerated materials, severe corrosion of equipment in high-salt media, disconnect between desalination and concentration processes, large transfer losses, and high energy consumption.

[0010] To achieve the above objectives, the present invention provides the following technical solution: an integrated treatment device for desalting and concentrating glycerol residue, comprising a centrifuge base and a centrifuge body fixed on the centrifuge base, wherein a centrifugation mechanism is provided inside the centrifuge body for desalting the glycerol residue; a concentration base is provided on one side of the centrifuge base, and a concentration mechanism for concentrating glycerol is provided on the concentration base.

[0011] Preferably, the centrifugation mechanism includes a geared motor disposed on one side of the centrifuge body, a drive pulley fixed at the output end of the geared motor, a driven pulley rotatably connected to the drive pulley via a synchronous belt, a differential gear is disposed at one end of the driven pulley, a protective box is installed between the centrifuge body and the geared motor, and the drive pulley, synchronous belt, driven pulley and differential gear are all disposed inside the protective box.

[0012] Preferably, one end of the differential is provided with a drum and a screw feeder. The screw feeder is located inside the drum, which is located inside the centrifuge body. The end of the drum near the differential is cone-shaped, and four sets of slag outlets are opened on the side wall of the cone end of the drum. An overflow port is opened on the end of the drum away from the differential. A screw ribbon is welded on the outer wall of the screw feeder, and a slag discharge port is opened on the outer wall of the screw feeder. The slag discharge port is located in the gap between the screw ribbons.

[0013] Preferably, the bottom of the centrifuge body is sealed with a slag guide hopper and a liquid guide hopper. The slag guide hopper is located directly below the slag outlet, and a slag collection box is installed at the bottom of the slag guide hopper. The liquid guide hopper is located directly below the overflow outlet, and a liquid collection box is installed at the bottom of the liquid guide hopper. The side wall of the liquid collection box is sealed with a first guide pipe.

[0014] Preferably, the centrifuge body is sealed with a glycerol residue main pipe on the side away from the geared motor, a dilution water pipe is sealed on the outer wall of the glycerol residue main pipe, and a Coriolis mass flow meter is installed on the glycerol residue main pipe, while an electromagnetic flow meter and an electric regulating valve are installed on the dilution water pipe.

[0015] Preferably, the end of the glycerol residue main pipe near the geared motor passes through the centrifuge body and is located inside the screw feeder. A screw distributor is provided at the port of the glycerol residue main pipe near the screw feeder, and an online viscometer is fixed on one side of the screw distributor.

[0016] Preferably, the concentration mechanism includes a feed pump disposed on one side of the concentration base. The input end of the feed pump is sealed with a first guide pipe, and the output end of the feed pump is sealed inside the evaporator body through a second guide pipe. The evaporator body is installed on the top of the concentration base, and an evaporation motor is fixed on the top of the evaporator body. A main shaft is fixed on the output end of the evaporation motor, and a distributor and a scraper are fixed on the outer side wall of the main shaft from top to bottom.

[0017] Preferably, the outer diameter of the distributor is smaller than the inner diameter of the evaporator body, the outer diameter of the scraper is the same as the inner diameter of the evaporator body, a wire mesh demister is provided above the distributor, the wire mesh demister is installed on the inner side wall of the evaporator body, and the end of the second guide pipe away from the feed pump is located between the distributor and the wire mesh demister.

[0018] Preferably, the inner wall of the evaporator body is provided with a heat conduction groove, a mist guide pipe is provided above the wire mesh demister, the mist guide pipe passes through and is fixed on the side wall of the evaporator body, the other end of the mist guide pipe is sealed on the input end of the condenser, the output end of the condenser is sealed with a concentration drain pipe, and the condenser is installed on the outer wall of the evaporator body. The inside of the concentration base is provided with a discharge hopper, and the bottom of the discharge hopper is sealed with a collection box.

[0019] Compared with the prior art, the beneficial effects of the present invention are as follows: The integrated treatment device for glycerol residue desalination and glycerol concentration, through the main pipeline of glycerol residue and in conjunction with the DCS distributed control system, uses the residue flow data collected by the flow meter as the calculation basis, and combines the preset target dilution ratio to output the theoretically required flow rate of dilution water in real time as a feedforward control signal to quickly drive the electric regulating valve to adjust the opening, thus constructing a dynamic adaptive closed-loop optimization adjustment system. Through the centrifugal mechanism, continuous solid-liquid separation can be achieved, and the processes of feeding, material separation, solid phase discharge, and liquid phase discharge can be run uninterrupted, achieving a stable and efficient separation effect. At the same time, it has the technical advantages of large single-unit processing capacity and high degree of automation control. Through the concentration mechanism, the material repeatedly completes the processes of film formation, evaporation, and downward movement, continuously achieving evaporation and concentration, with sufficient heat exchange, which can significantly reduce production energy consumption.

[0020] 1. A main pipeline for glycerol residue is installed. Glycerol residue in this system is transported from storage tanks to the main pipeline. All storage tanks, pipelines, and centrifuge casings are equipped with hot water heating jackets or electric heating components to maintain a stable material temperature of 65–75℃, adjusting the material's dynamic viscosity to a range suitable for efficient centrifugal separation. Under heating conditions, the glycerol residue temperature is controlled at 60–70℃. Dynamic dilution water is dynamically mixed into the feed pipe to reduce the viscosity of the residue medium, breaking down the adhesive agglomerates between salt components and organic matter, providing excellent operating conditions for the centrifugal separation process. The dilution ratio employs a fully automatic and precise control mechanism: a Coriolis mass flow meter is installed on the main glycerol residue pipeline to collect real-time instantaneous mass flow rate and medium density parameters; the DCS distributed control system uses the residue flow rate data collected by the flow meter as a calculation basis, combined with the preset target dilution ratio, to output the dilution water ratio in real time. Based on the required flow rate, the electric regulating valve is quickly driven to adjust its opening as a feedforward control signal. The system is equipped with a feedback fine-tuning loop, which collects the online viscometer readings from the pipeline after mixing and the operating current of the centrifuge geared motor as the basis for feedback adjustment. When the measured viscosity is higher than the set threshold or the motor operating current is too high, the control system automatically increases the dilution water addition ratio, and vice versa, thus constructing a dynamic adaptive closed-loop optimization adjustment system. A dedicated spiral diversion device is provided at the discharge end of the glycerol residue main pipeline. This diversion device includes a guide cone equipped with spiral blades. After the material flows into the internal cavity of the centrifuge drum, it is smoothly and evenly accelerated circumferentially by the spiral blades and evenly spread on the liquid surface of the liquid pool inside the spiral pusher. This effectively avoids the turbulence and local material accumulation caused by the high-speed jet of material impacting the liquid pool, and significantly improves the utilization efficiency of the effective settling area inside the drum.

[0021] 2. Equipped with a centrifuge body, during the solid-liquid separation of glycerol residue, the geared motor outputs power to drive the drive pulley to rotate. The drive pulley, through a synchronous belt drive pair, drives the driven pulley to rotate, thereby driving the differential to operate. The differential drives the drum and the screw conveyor to rotate synchronously at high speed. The glycerol residue material is fed into the internal chamber of the screw conveyor through the main glycerol residue pipe. Under the action of centrifugal force, high-density solid particles such as yellow salt are thrown to the outer periphery of the screw conveyor and conveyed along the spiral blades towards the conical end. The solid particles fall through the slag discharge port to the inner wall of the drum to form a slag layer. The less dense yellow glycerol mother liquor liquid phase passes through the filter holes opened in the screw conveyor and accumulates on the side of the drum near the axis to form a liquid ring layer. There is a gap between the screw conveyor and the drum. The minute speed difference continuously pushes the solid sludge adhering to the inner wall of the drum towards the conical end of the drum. The sludge is eventually discharged from the sludge outlet and transported to the sludge collection box via the sludge guide hopper for centralized collection and subsequent outsourced disposal, achieving the goal of solid waste reduction. The overflow port located at the cylindrical end of the drum discharges the inner layer of clear yellow glycerol mother liquor, which flows into the collection box via the liquid guide hopper and is transported to the subsequent glycerol concentration process. This device can achieve continuous solid-liquid separation, with uninterrupted operation of the feeding, material separation, solid phase discharge, and liquid phase discharge processes. By adjusting operating parameters such as the drum speed and the differential speed of the screw feeder, it can adapt to feed materials with different physicochemical properties to achieve stable and efficient separation results. It also has the technical advantages of large single-unit processing capacity and high degree of automation control.

[0022] 3. An evaporator body is installed. The preheated mother liquor is transported to the evaporator body. The evaporation motor outputs power to drive the main shaft to rotate, and the main shaft drives the distributor and scraper to rotate synchronously. After the mother liquor falls onto the surface of the distributor, it is evenly spread on the inner wall of the evaporator under the action of centrifugal force and flows downward along the cylinder wall by its own weight. The scraper adheres tightly to the inner wall of the cylinder under the centrifugal force, scraping the material to be evaporated along the wall into an ultra-thin liquid film of uniform thickness. The heat-conducting cavity of the evaporator jacket is filled with heat-conducting oil or high-pressure steam is introduced. The temperature of the heating medium is controlled at 140-170℃. The heat is transferred to the inner wall evaporation heat exchange surface through the metal wall of the cylinder. This process promotes the rapid vaporization of glycerol and moisture within the material. The rising steam generated by vaporization flows through a wire mesh demister at the top of the equipment to remove entrained liquid droplets, and is then transported outwards via a mist guide pipe. The scraper is designed with an inclined spiral structure and has a built-in spiral pushing function: it can scrape the continuously flowing material from above to vaporize it on the evaporation surface, and simultaneously transport the material downwards. The material repeatedly completes the film formation, evaporation, and downward movement processes, continuously achieving evaporation and concentration. The concentrated material flows into the collection box through the discharge hopper, where it can be directly stored or transported to the front-end circulating filtration process. This structure provides ample heat exchange and can significantly reduce production energy consumption. Attached Figure Description

[0023] Figure 1 This is a three-dimensional structural diagram of the present invention;

[0024] Figure 2 This is a side view of the three-dimensional structure of the present invention;

[0025] Figure 3 This is a schematic diagram of the three-dimensional structure of the centrifuge base of the present invention;

[0026] Figure 4 This is a schematic diagram of the three-dimensional structure of the centrifuge base of the present invention in half section.

[0027] Figure 5 This is a schematic diagram of the three-dimensional structure of a half-section of the centrifuge body of the present invention;

[0028] Figure 6 This is a schematic diagram of the three-dimensional structure of the drum of the present invention;

[0029] Figure 7 This is a three-dimensional structural diagram of the spiral feeder of the present invention;

[0030] Figure 8 This is a three-dimensional structural diagram of the slag discharge port of the present invention;

[0031] Figure 9 This is a schematic diagram of the three-dimensional structure of the drum in this invention (half-section).

[0032] Figure 10 This is a three-dimensional structural diagram of the main pipeline for glycerol residue according to the present invention;

[0033] Figure 11 This is a schematic diagram of the three-dimensional structure of the evaporator body of the present invention;

[0034] Figure 12 This is a schematic diagram of the three-dimensional structure of a half-section of the evaporator body of the present invention;

[0035] Figure 13 This is a three-dimensional structural diagram of the wire mesh demister of the present invention;

[0036] Figure 14 This is a schematic diagram of the three-dimensional structure of the condensation base of the present invention.

[0037] In the diagram: 1. Centrifuge base; 2. Centrifuge body; 3. Concentrator base; 4. Gear motor; 5. Drive pulley; 6. Synchronous belt; 7. Driven pulley; 8. Differential; 9. Protective box; 10. Drum; 11. Screw feeder; 12. Slag outlet; 13. Overflow outlet; 14. Screw ribbon; 15. Slag discharge port; 16. Slag guide hopper; 17. Liquid guide hopper; 18. Slag collection box; 19. Liquid collection box; 20. First guide pipe; 21. Glycerin residue main pipe; 22. Dilute 23. Water release pipeline; 24. Coriolis mass flow meter; 25. Electromagnetic flow meter; 26. Electric regulating valve; 27. Spiral distributor; 28. Online viscometer; 29. ​​Feed pump; 30. Second guide pipe; 31. Evaporator body; 32. Evaporation motor; 33. Main shaft; 34. Distributor; 35. Scraper; 36. Wire mesh demister; 37. Heat transfer groove; 38. Mist guide pipe; 39. Condenser; 40. Concentrated drain pipe; 51. Discharge hopper; 62. Collection box. Detailed Implementation

[0038] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0039] Example 1: Please refer to Figures 1-3 Existing integrated desalination and concentration treatment devices for glycerol residue suffer from several drawbacks in traditional glycerol residue processing. These include low precision in manual control, poor separation of highly viscous and easily agglomerated materials, severe corrosion of equipment in high-salt media, disconnect between desalination and concentration processes, high transfer losses, and high energy consumption. To address these technical problems, this embodiment discloses the following technical content: an integrated desalination and concentration treatment device for glycerol residue, comprising a centrifuge base 1 and a centrifuge body 2 fixed on the centrifuge base 1. The centrifuge body 2 is internally equipped with a centrifugal mechanism for desalting the glycerol residue. A concentration base 3 is located on one side of the centrifuge base 1, and a concentration mechanism for concentrating glycerol is installed on the concentration base 3.

[0040] Please see Figures 2-10The centrifugal mechanism includes a geared motor 4 mounted on one side of the centrifuge body 2. A drive pulley 5 is fixed to the output end of the geared motor 4. The drive pulley 5 is rotatably connected to a driven pulley 7 via a synchronous belt 6. A differential 8 is mounted at one end of the driven pulley 7. A protective box 9 is installed between the centrifuge body 2 and the geared motor 4. The drive pulley 5, synchronous belt 6, driven pulley 7, and differential 8 are all housed inside the protective box 9. A drum 10 and a spiral are mounted at one end of the differential 8. The screw feeder 11 is located inside the rotating drum 10, which is located inside the centrifuge body 2. The end of the rotating drum 10 closest to the differential 8 is conical, and four sets of slag discharge ports 12 are opened on the side wall of the conical end of the rotating drum 10. An overflow port 13 is opened on the end of the rotating drum 10 furthest from the differential 8. A screw ribbon 14 is welded to the outer wall of the screw feeder 11, and a slag discharge port 15 is opened on the outer wall of the screw feeder 11. The slag discharge port 15 is located in the gap between the screw ribbons 14. The centrifuge body 2 has a sealed bottom with a slag guide hopper 16 and a liquid guide hopper 17. The slag guide hopper 16 is located directly below the slag outlet 12, and a slag collection box 18 is installed at the bottom of the slag guide hopper 16. The liquid guide hopper 17 is located directly below the overflow outlet 13, and a liquid collection box 19 is installed at the bottom of the liquid guide hopper 17. A first guide pipe 20 is sealed on the side wall of the liquid collection box 19. A glycerol residue main pipe 21 is sealed on the side of the centrifuge body 2 away from the geared motor 4. The outer wall of the glycerol residue main pipe 21 is sealed. There is a dilution water pipeline 22, and a Coriolis mass flow meter 23 is installed on the glycerol residue main pipeline 21. An electromagnetic flow meter 24 and an electric regulating valve 2401 are installed on the dilution water pipeline 22. The end of the glycerol residue main pipeline 21 near the geared motor 4 passes through the centrifuge body 2 and is installed inside the screw feeder 11. A screw distributor 25 is installed at the port of the glycerol residue main pipeline 21 near the screw feeder 11. An online viscometer 26 is fixed on one side of the screw distributor 25.

[0041] During operation, glycerol residue is transported from the storage tank to the main glycerol residue pipeline 21. All storage tanks, pipelines, and centrifuge casings are equipped with hot water tracing jackets or electric heating to maintain the material temperature at 65-75℃, keeping the dynamic viscosity within a range suitable for efficient separation. At this temperature, the glycerol residue is heated to 60-70℃, and dilution water is dynamically injected into the feed pipeline to reduce the residue viscosity and break down the adhesive structure of salt and organic matter, creating conditions for centrifugal separation. The dilution ratio is precisely adjusted by the automatic control system. A Coriolis mass flow meter 23 is installed on the main glycerol residue pipeline 21 to measure the instantaneous mass flow rate and density of the residue in real time. The DCS system multiplies the residue flow rate measured by the Coriolis mass flow meter 23 by the set target dilution ratio (e.g., residue:water = 1:0.3~1:). 0.6), calculate the theoretical required flow rate of dilution water in real time, and use it as a feedforward signal to quickly adjust the opening of the electric regulating valve 2401; use the online viscometer 26 or the host current signal of the geared motor 4 on the pipeline after mixing for feedback fine adjustment. If the viscosity is higher than the set value or the host current is too high, the dilution water ratio will be automatically increased, and vice versa, forming a dynamic optimization closed loop; at the outlet of the glycerol residue main pipeline 21, a special spiral distributor 25 is designed, which is composed of a guide cone with spiral blades. After the material enters the inner cavity of the drum 10, it is accelerated smoothly and evenly along the circumferential direction by the spiral blades and distributed to the surface of the liquid pool inside the spiral pusher 11, which completely avoids the high-speed jet rushing into the liquid pool and causing turbulence and local accumulation, and significantly improves the utilization rate of the effective settling area.

[0042] When preparing for solid-liquid separation, the geared motor 4 drives the drive pulley 5 to rotate. The drive pulley 5 drives the driven pulley 7 to rotate via the synchronous belt 6, which in turn causes the differential 8 to rotate. The differential 8 drives the drum 10 and the screw conveyor 11 to rotate at high speed together. Glycerin residue enters the interior of the screw conveyor 11 through the glycerin residue main pipe 21. Under the action of strong centrifugal force, the heavy solid particles such as yellow salt are thrown to the outermost ring of the screw conveyor 11 and move towards the conical end of the screw conveyor 11. The solid particles such as yellow salt are discharged into the interior of the drum 10 through the slag discharge port 15 to form a slag layer, while the less dense liquid such as yellow glycerin mother liquor is thrown to the center of the drum 10 through the filter holes on the screw conveyor 11. A liquid ring is formed, and the spiral distributor 25 maintains a slight speed difference with the drum 10, continuously pushing the sludge on the inner wall towards the conical end of the drum 10, and finally discharging it through the sludge outlet 12. The sludge falls into the sludge collection box 18 through the sludge guide hopper 16 for collection and outsourced disposal, thus reducing solid waste. The clarified liquid, such as the inner layer yellow glycerin mother liquor, flows out along the overflow port 13 at the cylindrical end of the drum 10 and flows into the interior of the collection box 19 through the liquid guide hopper 17, facilitating subsequent glycerin concentration. This completes the solid-liquid separation. The entire process involves continuous feeding, and the separation, sludge discharge, and liquid discharge do not need to be interrupted. By adjusting parameters such as the rotation speed of the drum 10 and the differential speed of the spiral pusher 11, it can be adapted to different material characteristics to achieve efficient and stable separation, with the advantages of large processing capacity and high degree of automation.

[0043] For the harsh corrosive environment of high concentration sodium chloride and high temperature (60~75℃), duplex stainless steel (2205, S32205) resistant to pitting corrosion and chloride ion stress corrosion is used throughout. All core components of the centrifuge body 2, including the drum 10, screw feeder 11, casing, and glycerol residue main pipeline 21, which come into contact with materials, are made of 2205 duplex stainless steel through casting or welding. For piping and instrument contact parts: pipelines use 2205 seamless pipes, and valves use 2205 ball valves or diaphragm valves. The Coriolis mass flow meter 23 uses Hastelloy C-22 for its measuring tube, offering better compatibility, but all flange adapters are made of 2205.

[0044] The system integrates DCS control functions, enabling one-button start / stop and sequential control: the system follows a logical sequence of "lubrication station start → main unit start → differential speed start → feed pump start → dilution water start," in conjunction with a flushing procedure, to prevent clumping and blockage during start-up and shutdown; safety interlocks: real-time monitoring of main unit bearing temperature, vibration values, and differential torque; when torque exceeds limits or differential speed suddenly drops, an alarm is automatically triggered, and the feed rate is sequentially reduced, the dilution water is increased, or even an emergency shutdown is initiated to protect the equipment; data management: the DCS records and displays key parameters such as instantaneous processing capacity, cumulative processing capacity, dilution ratio, main unit current, differential speed, and running time, generating operation reports for energy efficiency analysis and fault tracing.

[0045] Example 2: Please refer to Figure 1 , Figure 2 and Figure 11 Based on Embodiment 1, a concentration mechanism is also disclosed, the specific structure of which is as follows: The concentration mechanism includes a feed pump 27 disposed on one side of the concentration base 3. The input end of the feed pump 27 is sealed with a first guide pipe 20, and the output end of the feed pump 27 is sealed inside the evaporator body 29 through a second guide pipe 28. The evaporator body 29 is installed on the top of the concentration base 3, and an evaporation motor 30 is fixed on the top of the evaporator body 29. A main shaft 31 is fixed on the output end of the evaporation motor 30. A distributor 32 and a scraper 33 are fixed on the outer side wall of the main shaft 31 from top to bottom.

[0046] Please see Figures 11-14The outer diameter of the distributor 32 is smaller than the inner diameter of the evaporator body 29. The outer diameter of the scraper 33 is the same as the inner diameter of the evaporator body 29. A wire mesh demister 34 is installed above the distributor 32 and is mounted on the inner side wall of the evaporator body 29. The end of the second guide pipe 28 away from the feed pump 27 is located between the distributor 32 and the wire mesh demister 34. A heat conduction groove 35 is opened on the inner wall of the evaporator body 29. A mist guide pipe 36 is installed above the wire mesh demister 34. The mist guide pipe 36 passes through and is fixed on the side wall of the evaporator body 29. The other end of the mist guide pipe 36 is sealed on the input end of the condenser 37. A concentration drain pipe 38 is sealed at the output end of the condenser 37. The condenser 37 is mounted on the outer side wall of the evaporator body 29. A discharge hopper 39 is opened inside the concentration base 3. A collection box 40 is sealed at the bottom of the discharge hopper 39.

[0047] The desalted glycerol mother liquor is fed into a spiral plate or tubular preheater via feed pump 27. The waste heat of the secondary steam condensate from the evaporator is used to preheat it to near the boiling point (about 60-80℃), saving energy and reducing consumption.

[0048] The preheated mother liquor enters the evaporator body 29. The evaporation motor 30 operates, driving the distributor 32 and scraper 33 to rotate via the main shaft 31. The mother liquor first falls onto the surface of the distributor 32, and under the centrifugal force of the distributor 32, it is evenly distributed on the inner wall of the evaporator body 29 and flows downward under gravity. Under the centrifugal force, the scraper 33 adheres tightly to the cylinder wall, scraping the evenly retained liquid to be evaporated into an extremely thin, uniform film on the evaporation surface of the inner cylinder wall. The heat transfer tank 35 in the jacket contains heat transfer oil or high-pressure steam, which heats the liquid to 140~170℃. Heat is transferred to the evaporation surface of the inner cylinder wall through the inner cylinder, where glycerin and water evaporate rapidly. The rising steam removes droplets through the top wire mesh demister 34 and is then discharged through the mist guide pipe 36. Because the scraper 33 is set in a spiral shape with a certain angle, it has a spiral propulsion effect, pushing the liquid downwards while scraping the liquid coming from above into a thin film for evaporation on the evaporation surface. This process of continuous evaporation, pushing downwards, film formation, and evaporation completes the evaporation and concentration process. Unnecessary liquid flows into the collection box 40 through the discharge hopper 39 for storage or recycling filtration, which greatly saves energy.

[0049] The evaporator body 29 controls the inlet flow rate and the temperature of the jacket steam according to different needs, and obtains the required concentrated liquid from the outlet; the evaporated glycerol-water mixed vapor is discharged to the interior of the condenser 37 through the mist guide pipe 36, and the mixed vapor is condensed into liquid by the circulating cooling water, thus obtaining yellow glycerol.

[0050] The contents not described in detail in this specification are existing technologies known to those skilled in the art.

[0051] Although embodiments of the invention have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the appended claims and their equivalents.

Claims

1. An integrated treatment device for glycerol residue desalination and glycerol concentration, comprising a centrifuge base (1) and a centrifuge body (2) fixed on the centrifuge base (1), characterized in that: The centrifuge body (2) is equipped with a centrifugal mechanism inside, which is used to desalinate glycerol residue; A concentration base (3) is provided on one side of the centrifuge base (1), and a concentration mechanism for concentrating glycerol is provided on the concentration base (3).

2. The integrated treatment device for glycerol residue desalting and glycerol concentration according to claim 1, characterized in that: The centrifugation mechanism includes a geared motor (4) located on one side of the centrifuge body (2). The output end of the geared motor (4) is fixed with a drive pulley (5). The drive pulley (5) is rotatably connected to a driven pulley (7) via a synchronous belt (6). A differential (8) is provided at one end of the driven pulley (7). A protective box (9) is installed between the centrifuge body (2) and the geared motor (4). The drive pulley (5), synchronous belt (6), driven pulley (7) and differential (8) are all located inside the protective box (9).

3. The integrated treatment device for glycerol residue desalting and glycerol concentration according to claim 2, characterized in that: One end of the differential (8) is provided with a drum (10) and a screw feeder (11). The screw feeder (11) is located inside the drum (10). The drum (10) is located inside the centrifuge body (2). The end of the drum (10) near the differential (8) is cone-shaped, and four sets of slag outlets (12) are opened on the cone end sidewall of the drum (10). An overflow outlet (13) is opened on the end of the drum (10) away from the differential (8). A screw ribbon (14) is welded on the outer sidewall of the screw feeder (11). A slag discharge port (15) is opened on the outer sidewall of the screw feeder (11). The slag discharge port (15) is located in the gap between the screw ribbons (14).

4. The integrated treatment device for glycerol residue desalting and glycerol concentration according to claim 3, characterized in that: The centrifuge body (2) is sealed with a slag guide hopper (16) and a liquid guide hopper (17) at the bottom. The slag guide hopper (16) is located directly below the slag outlet (12), and a slag collection box (18) is installed at the bottom of the slag guide hopper (16). The liquid guide hopper (17) is located directly below the overflow outlet (13), and a liquid collection box (19) is installed at the bottom of the liquid guide hopper (17). The side wall of the liquid collection box (19) is sealed with a first guide pipe (20).

5. The integrated treatment device for glycerol residue desalting and glycerol concentration according to claim 4, characterized in that: The centrifuge body (2) is sealed with a glycerol residue main pipe (21) on the side away from the geared motor (4). A dilution water pipe (22) is sealed on the outer wall of the glycerol residue main pipe (21). A Coriolis mass flow meter (23) is installed on the glycerol residue main pipe (21). An electromagnetic flow meter (24) and an electric regulating valve (2401) are installed on the dilution water pipe (22).

6. The integrated treatment device for glycerol residue desalting and glycerol concentration according to claim 5, characterized in that: The end of the glycerol residue main pipe (21) near the geared motor (4) passes through the centrifuge body (2) and is located inside the screw feeder (11). A screw distributor (25) is provided at the port of the glycerol residue main pipe (21) near the screw feeder (11). An online viscometer (26) is fixed on one side of the screw distributor (25).

7. The integrated treatment device for glycerol residue desalting and glycerol concentration according to claim 6, characterized in that: The concentration mechanism includes a feed pump (27) disposed on one side of the concentration base (3). The input end of the feed pump (27) is sealed with a first guide pipe (20), and the output end of the feed pump (27) is sealed inside the evaporator body (29) through a second guide pipe (28). The evaporator body (29) is installed on the top of the concentration base (3), and an evaporation motor (30) is fixed on the top of the evaporator body (29). The output end of the evaporation motor (30) is fixed with a main shaft (31). A distributor (32) and a scraper (33) are fixed on the outer side wall of the main shaft (31) from top to bottom.

8. The integrated treatment device for glycerol residue desalting and glycerol concentration according to claim 7, characterized in that: The outer diameter of the distributor (32) is smaller than the inner diameter of the evaporator body (29), the outer diameter of the scraper (33) is the same as the inner diameter of the evaporator body (29), a wire mesh demister (34) is provided above the distributor (32), the wire mesh demister (34) is installed on the inner side wall of the evaporator body (29), and the end of the second guide pipe (28) away from the feed pump (27) is located between the distributor (32) and the wire mesh demister (34).

9. The integrated treatment device for glycerol residue desalting and glycerol concentration according to claim 8, characterized in that: The inner wall of the evaporator body (29) is provided with a heat conduction groove (35). A mist guide pipe (36) is provided above the wire mesh demister (34). The mist guide pipe (36) passes through and is fixed on the side wall of the evaporator body (29). The other end of the mist guide pipe (36) is sealed on the input end of the condenser (37). The output end of the condenser (37) is sealed with a concentration drain pipe (38). The condenser (37) is installed on the outer wall of the evaporator body (29). A discharge hopper (39) is provided inside the concentration base (3). A collection box (40) is sealed at the bottom of the discharge hopper (39).

Images