Device for recovering glycerol from an epichlorohydrin by-product

Abstract

The utility model discloses a device for recovering glycerol from epichlorohydrin by-product belongs to resource cyclic utilization technical field. The outlet of ECH rectification residual liquid discharge pipe is connected with the feed inlet of flash tank, and the top gas phase outlet of flash tank is connected with the tube side inlet of flash condenser. The kettle bottom outlet of flash tank is connected with the tube side inlet of devolatilization preheater through flash kettle bottom delivery pump, and the tube side outlet of devolatilization preheater is connected with the material inlet of upper portion of devolatilization reactor, and the upper portion gas phase outlet of devolatilization reactor is connected with the tube side inlet of devolatilization condenser. The tube side outlet of flash condenser and devolatilization condenser is connected with the material inlet of glycerol temporary storage tank, and the bottom outlet of glycerol temporary storage tank is connected with glycerol delivery pump, and the outlet of glycerol delivery pump is connected with glycerol recovery pipe. The device can improve glycerol recovery rate, reduce energy consumption, greatly reduce hazardous waste emission, and can be long time stable operation.

Description

Technical Field

[0001] This utility model relates to the resource recovery of chemical by-products, and more particularly to an apparatus for recovering glycerol from epichlorohydrin by-products. It is applicable to the treatment of residual liquid containing glycerol, sodium salt and polymeric glycerol generated during the chlorohydrin ECH production process, and belongs to the field of resource recycling technology. Background Technology

[0002] Epichlorohydrin (ECH) is an important chemical intermediate widely used in epoxy resins, synthetic glycerol, and pharmaceuticals. During the chlorohydrin process for producing ECH, the cyclization reaction stage generates a large amount of byproduct—glycerol residue. This residue has a complex composition, typically containing 10%–20% glycerol, 15%–30% sodium salt, 30%–45% polymerized glycerol, and other impurities. This residue is highly viscous, has a high salt content, and is prone to polymerization. Traditional treatment methods, such as direct incineration or landfill, not only waste glycerol resources but also cause severe environmental pollution and high treatment costs.

[0003] In existing technologies, although attempts have been made to recover glycerol through distillation, extraction, and other methods, the presence of sodium salts and polymerized glycerol in the residual liquid easily leads to problems such as scaling, clogging, and reduced heat transfer efficiency in the equipment. This results in low recovery rates, high energy consumption, unstable operation, and difficulty in achieving continuous industrial operation.

[0004] For example, Chinese patent CN 107337308B discloses "an apparatus and process for extracting glycerol from high-salt wastewater concentrate from an epoxy resin plant," employing multi-stage thin-film evaporation concentration. This technical solution suffers from a fundamental thermodynamic flaw: it requires three-stage evaporation to operate at 160-200℃ and 10-25kPa. However, under this pressure, the boiling point of glycerol is above 213℃, and the boiling point of salt-containing glycerol solutions is even higher. The set temperature is far below the actual boiling point, making effective evaporation impossible. Forcibly increasing the temperature above the boiling point (>215℃) would lead to rapid polymerization and coking of the glycerol, causing equipment blockage and process failure. Therefore, the parameters of this solution are contradictory and lack engineering feasibility.

[0005] For example, Chinese patent CN 110229046B discloses "an apparatus and method for extracting glycerol and glycerol-like alcohols from the mother liquor of epoxy wastewater evaporation". Although this technical solution proposes a technical route combining distillation and molecular distillation, it still has the following significant problems and defects: 1. Complex process and high energy consumption: This process involves multiple unit operations such as preheating, distillation, three-stage segmented heat exchange, decolorization and deodorization, residual liquid centrifugation, and molecular distillation, resulting in a lengthy and complex system flow. Multiple heating, cooling, and vacuum operations lead to extremely high energy consumption, and require complex steam, heat transfer medium, vacuum, and cooling systems, resulting in huge investment and operating costs, raising questions about its economic viability for industrialization.

[0006] 2. Bottlenecks exist in the core separation process: The core technology relies on distillation under a high vacuum of ≤5kPa to form an azeotrope between glycerol and water and then separate them. However, the mother liquor of epoxy wastewater has a complex composition (containing salts, amines, polyethers, etc.), and these impurities can severely interfere with the azeotropic composition and may lead to problems such as foaming and scaling in the tower. In actual operation, it is difficult to consistently obtain glycerol with a purity ≥95.5%. The glycerol sample data (97.5%) provided in the instruction manual lacks batch data supporting continuous and stable operation.

[0007] 3. High salt content leads to poor equipment reliability: This solution requires continuous separation and discharge of salt-containing slurry (NaCl≤5%) at the bottom of the distillation vessel. High concentrations of salt easily crystallize at high temperatures, causing severe scaling and blockage of the vessel bottom, pipes, valves, and centrifuges. This seriously affects the continuous operation cycle and stability of the equipment. The instruction manual's mention of needing to stop and clean the equipment after "5-8 days of continuous operation" proves the existence of this problem and makes it impossible to meet the requirements of continuous industrial production.

[0008] 4. Incomplete impurity removal poses a high risk to product quality: Although decolorization and deodorization are mentioned in the process, organic impurities such as N,N-dimethylformamide, amine catalysts, and polyethers present in the raw materials cannot be completely removed by distillation and simple layering alone. These impurities will affect the odor, color, and key indicators (such as saponification equivalent and reducing agents) of the glycerin product, posing a risk of substandard product quality and making it difficult to stably produce high-grade or first-grade industrial glycerin.

[0009] 5. Molecular distillation has harsh application conditions and low economic benefits: Relying on short-path molecular distillation to separate complex residual liquids (containing polyglycerol, PEG400, etc.) after desalination is expensive, difficult to operate, and has limited processing capacity. For materials with complex composition and extremely high viscosity, its separation efficiency, product yield, and economic benefits all face huge challenges, and its feasibility for industrial scale-up is low.

[0010] In summary, existing technologies are either impossible to implement due to thermodynamic design flaws or have complex process routes and high energy consumption. Furthermore, they lack effective solutions for engineering problems related to handling high-salt and high-impurity materials. Equipment scaling and clogging, as well as product quality control, are the main technical bottlenecks, making industrial application and promotion extremely difficult. Utility Model Content

[0011] The purpose of this section is to outline some aspects of embodiments of the present invention and to briefly describe some preferred embodiments. Simplifications or omissions may be made in this section, as well as in the abstract and title of this application, and such simplifications or omissions should not be construed as limiting the scope of the present invention.

[0012] In view of the problems existing in the prior art, this utility model is proposed.

[0013] The purpose of this invention is to overcome the problems existing in the prior art and provide a device for recovering glycerol from epichlorohydrin byproducts, which can improve the glycerol recovery rate, reduce energy consumption, significantly reduce hazardous waste emissions, and can operate stably for a long time.

[0014] To solve the above technical problems, this utility model provides an apparatus for recovering glycerol from epichlorohydrin byproducts, comprising a flash evaporator, an outlet of the ECH distillation residue discharge pipe connected to the feed inlet of the flash evaporator, a top vapor outlet of the flash evaporator connected to the tube-side inlet of the flash condenser; a bottom outlet of the flash evaporator connected to the tube-side inlet of a devolatilization preheater via a flash evaporator bottom transfer pump, a tube-side outlet of the devolatilization preheater connected to the material inlet at the top of the devolatilization reactor, and a top vapor outlet of the devolatilization reactor connected to the tube-side inlet of the devolatilization condenser; the tube-side outlets of both the flash condenser and the devolatilization condenser connected to the material inlet of a glycerol storage tank, a glycerol transfer pump connected to the bottom outlet of the glycerol storage tank, and a glycerol recovery pipe connected to the outlet of the glycerol transfer pump.

[0015] Furthermore, the bottom outlet of the devolatilization reactor is connected to the tube-side inlet of the devolatilization residue cooler via a bottom transfer pump, and the tube-side outlet of the residue cooler is connected to the feed inlet of the dilution vessel; the non-condensable gas outlets of the flash condenser and the devolatilization condenser are both connected to the inlet of the vacuum buffer tank, and the suction port of the vacuum buffer tank is connected to the vacuum port of the steam jet pump; the waste liquid outlet of the steam jet pump is connected to the wastewater storage tank, and the outlet of the wastewater storage tank is connected to the dilution water inlet of the dilution vessel via a wastewater transfer pump.

[0016] Furthermore, the bottom outlet of the dilution vessel is connected to the inlet of the diluent storage tank via a dilution vessel bottom transfer pump, the outlet of the diluent storage tank is connected to a diluent transfer pump, and the outlet of the diluent transfer pump is connected to a diluent transfer pipe.

[0017] Furthermore, the flash evaporator is a vertical structure with a stirring mechanism, and a spiral flow-guiding heating coil is installed inside it. The spiral flow-guiding heating coil is connected to the flash heat medium circulation pump to form a circulation loop.

[0018] Furthermore, the upper part of the devolatilization preheater is provided with a liquid distribution plate, and an external falling film tube is provided inside the devolatilization preheater. The upper end of the external falling film tube passes through the liquid distribution hole of the liquid distribution plate, and the inner cavity of the external falling film tube is connected to the devolatilization heat medium circulation pump to form a heat medium circulation loop.

[0019] Furthermore, the shell-side inlet of the devolatilization preheater is connected to a heat medium supply pipe, and its shell-side outlet is connected to a heat medium return pipe.

[0020] Furthermore, the shell-side inlets of the flash condenser, devolatilization condenser, and autoclave residue cooler are all connected to the cooling water supply pipe, and their shell-side outlets are all connected to the cooling water return pipe.

[0021] Furthermore, the outer wall of the glycerin storage tank is wrapped with a semi-tube heater, the inlet of which is connected to a hot water supply pipe and the outlet of which is connected to a hot water return pipe.

[0022] Furthermore, the outer wall of the dilution vessel is wrapped with a semi-tube cooler, the inlet of which is connected to a cooling water supply pipe and the outlet of which is connected to a cooling water return pipe.

[0023] Furthermore, the power steam inlet of the steam jet pump is connected to the outlet of the steam buffer tank, and the inlet of the steam buffer tank is connected to the power steam pipe.

[0024] Compared with the prior art, the advantages or beneficial effects of this utility model include at least the following: 1. High glycerol recovery rate: up to 87.6% or more, far exceeding that of traditional processes; 2. Low energy consumption: Thermal energy is utilized in stages, reducing overall energy consumption by more than 30%; 3. Significant environmental benefits: The residual liquid COD value is reduced by 66%, and hazardous waste emissions are reduced by 90%; 4. Stable equipment operation: anti-coking and anti-clogging, can run continuously for more than 72 hours; 5. High degree of automation: Reduces operator requirements by 50% and provides high control precision. Attached Figure Description

[0025] To more clearly illustrate the technical solutions of the embodiments of this utility model, the drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort. The drawings are provided for reference and illustration only and are not intended to limit this utility model. Wherein: Figure 1 The flowchart shows the apparatus for recovering glycerol from epichlorohydrin byproducts according to this invention. Figure reference numerals: R1. Flash evaporator; R2. Deviation reactor; R3. Dilution vessel; H1. Deviation preheater; H2. Kettle residue cooler; H3. Flash condenser; H4. Deviation condenser; T1. Glycerin temporary storage tank; T2. Diluent storage tank; T3. Vacuum buffer tank; T4. Wastewater storage tank; T5. Steam buffer tank; P1. Flash evaporation heat medium circulation pump; P2. Flash evaporation kettle bottom transfer pump; P3. Deviation heat medium circulation pump; P4. Deviation kettle bottom transfer pump; P5. Dilution kettle bottom transfer pump; P6. Glycerin transfer pump; P7. Wastewater transfer pump; P8. Diluent transfer pump; P9. Steam jet pump; G1. ECH distillation residue discharge pipe; G2. Power steam pipe; G3. Heat medium supply pipe; G4. Heat medium return pipe; G5. Cooling water supply pipe; G6. Cooling water return pipe; G7. Hot water supply pipe; G8. Hot water return pipe; G9. Glycerin recovery pipe; G10. Diluent delivery pipe. Detailed Implementation

[0026] To make the technical means, creative features, achieved objectives and effects of this utility model easier to understand, the present utility model will be further described below with reference to specific illustrations. Obviously, the described embodiments are only some embodiments of this utility model, and not all embodiments.

[0027] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention pertains. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention.

[0028] like Figure 1 As shown, the apparatus for recovering glycerol from epichlorohydrin byproducts of this invention includes a flash evaporator R1, a devolatilization reactor R2, a dilution reactor R3, a devolatilization preheater H1, a reactor residue cooler H2, a flash condenser H3, a devolatilization condenser H4, a glycerol storage tank T1, a diluent storage tank T2, a vacuum buffer tank T3, a wastewater storage tank T4, and a steam buffer tank T5.

[0029] The outlet of the ECH distillation residue discharge pipe G1 is connected to the inlet of the flash evaporator R1. The flash evaporator R1 adopts a vertical structure with stirring, and has a built-in spiral flow heating coil and a double-blade agitator, which can effectively enhance the heat and mass transfer efficiency of high-viscosity materials and suppress mist entrainment. The upper outlet of the spiral flow heating coil is connected to the inlet of the flash heat medium circulation pump P1, and the outlet of the flash heat medium circulation pump P1 is connected to the lower inlet of the spiral flow heating coil.

[0030] The bottom outlet of the flash evaporator R1 is connected to the inlet of the flash evaporator bottom transfer pump P2 via a jacketed pipe. The outlet of the flash evaporator bottom transfer pump P2 is connected to the lower tube inlet of the devolatilization preheater H1 via a jacketed pipe. The lower shell inlet of the devolatilization preheater H1 is connected to the heat medium supply pipe G3, and the upper shell outlet of the devolatilization preheater H1 is connected to the heat medium return pipe G4. The upper tube outlet of the devolatilization preheater H1 is connected to the material inlet at the top of the devolatilization reactor R2 via a jacketed pipe. A liquid distribution plate is provided below the material inlet. The upper end of the outer falling film pipe passes through the liquid distribution hole of the liquid distribution plate. The liquid flows downward along the gap between the liquid distribution hole and the outer falling film pipe, forming a uniform outer falling film on the outer wall of the outer falling film pipe. The heat medium in the outer falling film pipe is circulated by the devolatilization heat medium circulation pump P3 to heat and devolatilize the outer falling film.

[0031] The bottom outlet of the devolatilization reactor R2 is connected to the lower inlet of the tube side of the devolatilization reactor H2 via the bottom transfer pump P4 and the jacketed pipe. The lower inlet of the shell side of the reactor H2 is connected to the cooling water supply pipe G5, and the upper outlet of the shell side of the reactor H2 is connected to the cooling water return pipe G6. The upper outlet of the tube side of the reactor H2 is connected to the feed port of the dilution reactor R3 via the jacketed pipe.

[0032] The top vapor outlet of the flash evaporator R1 is connected to the upper tube inlet of the flash condenser H3 via a jacketed pipe. The lower shell inlet of the flash condenser H3 is connected to the cooling water supply pipe G5. The upper shell outlet of the flash condenser H3 is connected to the cooling water return pipe G6. The lower tube outlet of the flash condenser H3 is connected to the material inlet of the glycerol storage tank T1.

[0033] The upper gas phase outlet of the devolatilization reactor R2 is connected to the upper tube inlet of the devolatilization condenser H4 via a jacketed pipe. The lower shell inlet of the devolatilization condenser H4 is connected to the cooling water supply pipe G5. The upper shell outlet of the devolatilization condenser H4 is connected to the cooling water return pipe G6. The lower tube outlet of the devolatilization condenser H4 is also connected to the material inlet of the glycerol storage tank T1.

[0034] The outer wall of the glycerol storage tank T1 is wrapped with a half-tube heater. The bottom inlet of the half-tube heater is connected to the hot water supply pipe G7, and the upper outlet of the half-tube heater is connected to the hot water return pipe G8. The bottom outlet of the glycerol storage tank T1 is connected to the inlet of the glycerol transfer pump P6, and the outlet of the glycerol transfer pump P6 is connected to the upper return port of the glycerol storage tank T1 and the glycerol recovery pipe G9. The outlet of the glycerol recovery pipe G9 is connected to the ECH distillation feed pipe of the upstream distillation vessel.

[0035] The non-condensable gas outlets of the lower heads of flash condenser H3 and devolatilization condenser H4 are connected to the inlet of vacuum buffer tank T3, respectively. The top suction port of vacuum buffer tank T3 is connected to the vacuum port of steam jet pump P9. The power steam inlet of steam jet pump P9 is connected to the top outlet of steam buffer tank T5, and the inlet of steam buffer tank T5 is connected to power steam pipe G2.

[0036] The waste liquid outlet of the steam jet pump P9 is connected to a vacuum drain pipe. The lower end of the vacuum drain pipe is inserted into the lower part of the wastewater storage tank T4. The bottom outlet of the wastewater storage tank T4 is connected to the inlet of the wastewater transfer pump P7. The outlet of the wastewater transfer pump P7 is connected to the upper reflux port of the wastewater storage tank T4 and the dilution water injection port of the dilution vessel R3.

[0037] The outer wall of the dilution vessel R3 is wrapped with a half-pipe cooler. The bottom inlet of the half-pipe cooler is connected to the cooling water supply pipe G5, and the upper outlet of the half-pipe cooler is connected to the cooling water return pipe G6. The bottom outlet of the dilution vessel R3 is connected to the inlet of the bottom transfer pump P5. The outlet of the bottom transfer pump P5 is connected to the upper inlet of the diluent storage tank T2. The bottom outlet of the diluent storage tank T2 is connected to the inlet of the diluent transfer pump P8. The outlet of the diluent transfer pump P8 is connected to the upper return port of the diluent storage tank T2 and the diluent transfer pipe G10.

[0038] The working process of this device is as follows: The ECH distillation residue from the upstream distillation vessel includes 10%–20% glycerol, 15%–30% sodium salt, and 30%–45% polyglycerol. It is continuously transported to the flash evaporator R1 via a bottom transfer pump and ECH distillation residue discharge pipe G1. The ECH distillation residue discharge pipe G1 is equipped with a level regulating valve that is interlocked with the level gauge of the flash evaporator R1 to precisely control the material residence time and avoid excessive thermal cracking or polymerization.

[0039] The flash evaporator R1 operates at a temperature controlled at 180–190°C by the flash heat medium circulation pump P1, while the pressure inside the evaporator is maintained at approximately 2 kPa (A) by the steam jet pump P9. The ECH distillation residue entering the flash evaporator R1 is heated by a built-in spiral flow heating coil and stirred by a dual-blade agitator. The pressure is controlled by a pressure regulating valve group installed on the vacuum pipeline. Simultaneously, based on the differences in boiling points and volatility of each component, the light component glycerol vapor is initially separated. The vaporized glycerol is discharged from the top vapor outlet of the flash evaporator R1 and enters the upper inlet of the tube side of the flash condenser H3 through a jacketed pipeline. Cooling water is introduced into the shell side of the flash condenser H3 to condense the vaporized glycerol, which then flows into the glycerol storage tank T1. The non-condensable vapor remaining in the flash condenser H3 is pumped through the vacuum buffer tank T3 and discharged by the steam jet pump P9.

[0040] The material at the bottom of the flash evaporator R1 after initial flash evaporation is sent out by the flash evaporator bottom transfer pump P2. It first flows through the tube side of the devolatilization preheater H1, where it is preheated by the shell-side heat medium, and then enters the devolatilization reactor R2. A temperature transmitter is installed at the tube-side outlet of the devolatilization preheater H1, which is interlocked with the temperature regulating valve on the heat medium return pipe G4 to raise the material temperature from about 190℃ to between 210-215℃.

[0041] After preheating, the material enters the devolatilization reactor R2, forming a uniform liquid film on the surface of the outer falling film tubes. The devolatilization reaction temperature is controlled at approximately 220℃ by the devolatilization heat medium circulation pump P3, and the devolatilization reaction pressure is controlled at an ultimate vacuum of approximately 500Pa by the steam jet pump P9. Under high temperature and high vacuum reaction conditions, residual glycerol is further removed. The vaporized glycerol obtained from devolatilization enters the tube side of the devolatilization condenser H4 through a jacketed pipe. Cooling water is introduced into the shell side of the devolatilization condenser H4 to condense the vaporized glycerol into the glycerol storage tank T1. The non-condensable vapors remaining in the devolatilization condenser H4 are pumped to the steam jet pump P9 through the vacuum buffer tank T3 for discharge. The outer wall of the falling film tubes in the devolatilization reactor R2 is coated with an Al2O3-TiO2 nanocomposite coating by plasma spraying, which can reduce the coking rate by 72%. At the same time, the equipment body is equipped with multiple sets of sight glasses and electric scraper devices to monitor the film status and cleanliness in real time.

[0042] The high-viscosity polymer after the devolatilization reaction in devolatilization reactor R2 enters the bottom transfer pump P4 from the bottom outlet. It is then pumped by P4 to the tube side of the residue cooler H2 for cooling before entering the dilution vessel R3. Cooling water is introduced into the shell side of the residue cooler H2. A temperature transmitter at the tube side outlet of the residue cooler H2 is interlocked with the temperature regulating valve on the cooling water return pipe G6 to reduce the material temperature from approximately 180℃ to below 100℃.

[0043] The cooled material enters the dilution vessel R3, which adopts a vertical high-shear stirring structure with an external half-pipe cooling system. Cooling water enters from the lower point of the half-pipe and flows out from the higher point. Simultaneously, steam from the power steam pipe G2 enters the steam buffer tank T5 to power the steam jet pump P9. Wastewater generated during vacuuming is discharged into the wastewater storage tank T4. Diluent water is then injected into the dilution vessel R3 via the wastewater transfer pump P7 at a ratio of 20%–40% of the residual liquid feed. The injection volume is precisely controlled by the flow meter and flow regulating valve group on the outlet pipeline of the wastewater transfer pump P7. The operating temperature of the dilution vessel R3 is maintained at 70-90℃. Under the stirring action, the residual liquid and aqueous solution are uniformly mixed, and the COD value of the diluted solution is significantly reduced. The entire system can achieve long-term stable operation. The diluted solution is then sent to the diluent storage tank T2 via the dilution vessel bottom transfer pump P5. The solution temporarily stored in the diluent storage tank T2 is then sent out by the diluent transfer pump P8 and outsourced for further processing via the diluent transfer pipe G10.

[0044] The glycerol recovery rate of this device can reach over 87%. The glycerol solution recovered into the glycerol storage tank T1 is sent out by the glycerol transfer pump P6 and connected to the ECH distillation feed pipe via the glycerol recovery pipe G9, serving as the feed material for ECH distillation in the system reaction. The glycerol storage tank T1 is externally heated by a half-pipe, with hot water entering from the bottom and flowing out from the top, controlling the glycerol temperature inside T1 at 80~90℃, ensuring good fluidity for easy transport.

[0045] The above description is merely a preferred embodiment of the present utility model, showing and describing the basic principles, main features, and advantages of the present utility model. It is not intended to limit the scope of patent protection of the present utility model. Those skilled in the art should understand that the present utility model is not limited to the above embodiments. In addition to the above embodiments, the present utility model may have other implementations without departing from the spirit and scope of the present utility model. Various changes and improvements to the present utility model are also possible. All technical solutions formed by equivalent substitutions or equivalent transformations fall within the scope of protection claimed by the present utility model. The scope of protection claimed by the present utility model is defined by the appended claims and their equivalents. Technical features not described in the present utility model can be implemented by or using existing technology, and will not be elaborated here.

Claims

1. An apparatus for recovering glycerol from epichlorohydrin byproducts, comprising a flash evaporator (R1), characterized in that: The outlet of the ECH distillation residue discharge pipe (G1) is connected to the feed inlet of the flash evaporator (R1), and the top vapor outlet of the flash evaporator (R1) is connected to the tube-side inlet of the flash condenser (H3). The bottom outlet of the flash evaporator (R1) is connected to the tube-side inlet of the devolatilization preheater (H1) via the flash evaporator bottom transfer pump (P2). The tube-side outlet of the devolatilization preheater (H1) is connected to the material inlet at the top of the devolatilization reactor (R2). The upper gas phase outlet of the devolatilization reactor (R2) is connected to the tube-side inlet of the devolatilization condenser (H4). The tube-side outlets of the flash condenser (H3) and devolatilization condenser (H4) are both connected to the material inlet of the glycerol storage tank (T1). The bottom outlet of the glycerol storage tank (T1) is connected to a glycerol transfer pump (P6), and the outlet of the glycerol transfer pump (P6) is connected to a glycerol recovery pipe (G9).

2. The apparatus for recovering glycerol from epichlorohydrin byproducts according to claim 1, characterized in that: The bottom outlet of the devolatilization reactor (R2) is connected to the tube-side inlet of the devolatilization reactor bottom transfer pump (P4), and the tube-side outlet of the reactor residue cooler (H2) is connected to the feed inlet of the dilution vessel (R3). The non-condensable gas outlets of the flash condenser (H3) and the devolatilization condenser (H4) are both connected to the inlet of the vacuum buffer tank (T3). The suction port of the vacuum buffer tank (T3) is connected to the vacuum port of the steam jet pump (P9). The waste liquid outlet of the steam jet pump (P9) is connected to the wastewater storage tank (T4). The outlet of the wastewater storage tank (T4) is connected to the dilution water inlet of the dilution vessel (R3) through the wastewater transfer pump (P7).

3. The apparatus for recovering glycerol from epichlorohydrin byproducts according to claim 2, characterized in that: The bottom outlet of the dilution vessel (R3) is connected to the inlet of the diluent storage tank (T2) via the bottom transfer pump (P5). The outlet of the diluent storage tank (T2) is connected to the diluent transfer pump (P8), and the outlet of the diluent transfer pump (P8) is connected to the diluent transfer pipe (G10).

4. The apparatus for recovering glycerol from epichlorohydrin byproducts according to claim 1, characterized in that, The flash evaporator (R1) is a vertical structure with a stirring mechanism. It is equipped with a spiral flow-guiding heating coil, which is connected to the flash heat medium circulation pump (P1) to form a circulation loop.

5. The apparatus for recovering glycerol from epichlorohydrin byproducts according to claim 1, characterized in that, The upper part of the devolatilization preheater (H1) is provided with a liquid distribution plate, and an external falling film tube is provided inside the devolatilization preheater (H1). The upper end of the external falling film tube passes through the liquid distribution hole of the liquid distribution plate, and the inner cavity of the external falling film tube is connected to the devolatilization heat medium circulation pump (P3) to form a heat medium circulation loop.

6. The apparatus for recovering glycerol from epichlorohydrin byproducts according to claim 1, characterized in that, The shell-side inlet of the devolatilizer (H1) is connected to a heat medium supply pipe (G3), and its shell-side outlet is connected to a heat medium return pipe (G4).

7. The apparatus for recovering glycerol from epichlorohydrin byproducts according to claim 2, characterized in that, The shell-side inlets of the flash condenser (H3), devolatilization condenser (H4), and autoclave residue cooler (H2) are all connected to the cooling water supply pipe (G5), and their shell-side outlets are all connected to the cooling water return pipe (G6).

8. The apparatus for recovering glycerol from epichlorohydrin byproducts according to claim 1, characterized in that, The outer wall of the glycerin storage tank (T1) is wrapped with a half-tube heater. The inlet of the half-tube heater is connected to the hot water supply pipe (G7), and the outlet is connected to the hot water return pipe (G8).

9. The apparatus for recovering glycerol from epichlorohydrin byproducts according to claim 2, characterized in that, The outer wall of the dilution vessel (R3) is wrapped with a half-tube cooler. The inlet of the half-tube cooler is connected to the cooling water supply pipe (G5), and the outlet is connected to the cooling water return pipe (G6).

10. The apparatus for recovering glycerol from epichlorohydrin byproducts according to claim 2, characterized in that, The power steam inlet of the steam jet pump (P9) is connected to the outlet of the steam buffer tank (T5), and the inlet of the steam buffer tank (T5) is connected to the power steam pipe (G2).

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