Device for continuously hydrolyzing potassium phytate and recovering condensed water

Abstract

The utility model discloses a device for continuously hydrolyzing potassium phytate and recovering condensate water, which comprises a flash tank, a hydrolysis system and an evaporation device, a material inlet of the flash tank is communicated with the hydrolysis system, a gas phase outlet of the flash tank is communicated with a gas phase inlet of the evaporation device, and a material outlet of the flash tank is communicated with a material outlet of the evaporation device. A liquid phase outlet of the flash tank is communicated with a material inlet of an evaporation device, a condensate outlet of the evaporation device is communicated with a condensate recovery tank, and a liquid phase outlet of the evaporation device is communicated with a concentrated solution storage tank; the hydrolysis system comprises a plurality of hydrolysis tanks which are respectively communicated with the flash tank, and discharge regulating valves are arranged on connecting pipelines of the plurality of hydrolysis tanks and the flash tank; and feeding regulating valves are arranged on the feeding pipelines of the plurality of hydrolysis tanks. According to the device, the processes of hydrolysis, flash evaporation and evaporation can be circularly and continuously carried out, the production efficiency is improved, waste heat in the flash evaporation process and condensate in the evaporation process are recovered, and the energy consumption is reduced.

Description

Technical Field

[0001] The utility model relates to an inositol production device, in particular to a device for hydrolyzing potassium phytate and recovering condensed water. Background Art

[0002] Inositol, also known as cyclohexanol, is an isomer of glucose. It is a white crystalline powder, odorless, sweet, with a density of 1.752 and a melting point of 225-227°C. It is soluble in water but insoluble in anhydrous ethanol, ether, and chloroform. It is water-soluble or alkaline-neutral. Inositol is primarily used to treat conditions such as cirrhosis, hepatitis, fatty liver disease, and high blood cholesterol. Currently, inositol is mostly purified by hydrolysis of potassium phytate followed by flash distillation, evaporation, or concentration. The production of inositol from potassium phytate presents the following challenges: First, the flash distillation of the potassium phytate hydrolyzate generates a significant amount of heat. In the currently used batch production method, each subsequent discharge is directly discharged, wasting the heat generated during the hydrolysis process. This places significant strain on the environment and increases production costs. Second, the production of inositol from potassium phytate generates condensed water, which is directly discharged, resulting in a waste of resources. Utility Model Content

[0003] The technical problem to be solved by the utility model is: in view of the deficiencies in the existing technology, a device for continuously hydrolyzing potassium phytate and recovering condensed water is provided, wherein the device can realize the continuous cycle of hydrolysis, flash evaporation and evaporation processes, thereby improving production efficiency, and the waste heat in the flash evaporation process and the condensed liquid in the evaporation process are both recovered, thereby reducing energy consumption.

[0004] In order to solve the above technical problems, the technical solution of the utility model is:

[0005] A device for continuously hydrolyzing potassium phytate and recovering condensed water comprises a flash tank, a hydrolysis system and an evaporation device, wherein the material inlet of the flash tank is connected to the hydrolysis system, the gas phase outlet of the flash tank is connected to the gas phase inlet of the evaporation device, the liquid phase outlet of the flash tank is connected to the material inlet of the evaporation device, the condensate outlet of the evaporation device is connected to a condensate recovery tank, and the liquid phase outlet of the evaporation device is connected to a concentrated liquid storage tank;

[0006] The hydrolysis system comprises a plurality of hydrolysis tanks respectively connected to the flash tank, and the connecting pipes between the plurality of hydrolysis tanks and the flash tank are all provided with a discharge regulating valve; and the feed pipes of the plurality of hydrolysis tanks are all provided with a feed regulating valve.

[0007] Preferably, the liquid phase outlet of the flash tank is connected to the material inlet of the evaporation device through a flash buffer tank.

[0008] Preferably, the evaporation device includes a connected separation chamber and a heating chamber, the material inlet and the gas phase inlet of the heating chamber are respectively connected to the liquid phase outlet of the separation chamber and the gas phase outlet of the flash tank, the gas phase outlet of the heating chamber is connected to the separation chamber, the material outlets of the heating chamber and the separation chamber are connected to the concentrated liquid storage tank, and the material inlet of the separation chamber is connected to the flash buffer tank.

[0009] Preferably, feed pumps are provided on the connecting pipes between the separation chamber and the flash buffer tank, and between the flash tanks and the flash buffer tanks.

[0010] Preferably, the condensate outlet of the heating chamber is connected to a condensate recovery tank.

[0011] Preferably, the gas phase outlet of the separation chamber is communicated with the gas phase inlet of the heating chamber.

[0012] Preferably, the material outlets of the heating chamber and the separation chamber are connected to the liquid outlet pipes, the liquid outlet pipes are respectively connected to the discharge pipe and the circulation pipe, the discharge pipe is connected to the concentrated liquid storage tank, the circulation pipe is connected to the material inlet of the heating chamber, a density meter is provided on the liquid outlet pipe, a discharge valve and a discharge pump are provided on the discharge pipe, a circulation valve and a circulation pump are provided on the circulation pipe, and the density meter is interlocked with the discharge valve, discharge pump, circulation valve and circulation pump respectively.

[0013] Due to the adoption of the above technical solution, the beneficial effects of the utility model are:

[0014] The utility model provides a device for continuously hydrolyzing potassium phytate and recovering condensed water, comprising a flash tank, a hydrolysis system and an evaporation device, wherein the material inlet of the flash tank is connected to the hydrolysis system, the gas phase outlet of the flash tank is connected to the gas phase inlet of the evaporation device, the liquid phase outlet of the flash tank is connected to the material inlet of the evaporation device, the condensate outlet of the evaporation device is connected to a condensate recovery tank, and the liquid phase outlet of the evaporation device is connected to a concentrated liquid storage tank; the hydrolysis system comprises a plurality of hydrolysis tanks respectively connected to the flash tank, and the connecting pipes of the plurality of hydrolysis tanks and the flash tank are all provided with a discharge regulating valve; the feed pipes of the plurality of hydrolysis tanks are all provided with a feed regulating valve. The device adopts a plurality of hydrolysis tanks respectively connected to the flash tank, and by effectively adjusting the feed time, hydrolysis time, discharge time of each hydrolysis tank and the feed interval time of adjacent hydrolysis tanks, a continuous cycle of hydrolysis, flash evaporation and evaporation is achieved, and the waste heat in the flash evaporation process is reused in the evaporation process, thereby ensuring the recycling of waste heat, and the condensed water in the evaporation process is also recycled, thereby reducing energy consumption. Furthermore, continuous discharge from the flash tank ensures that the gaseous waste heat in the evaporation unit remains heated, improving evaporation efficiency. The multiple hydrolysis tanks in this unit operate independently, ensuring high stability. Discharging from a single tank in the hydrolysis system allows for continuous production and waste heat generation, fully utilizing the thermal energy.

[0015] In this device, the liquid phase outlet of the flash tank is connected to the material inlet of the evaporation unit through a flash buffer tank. The flash buffer tank not only serves as a temporary storage and transfer tank to achieve continuous production, but also acts as a buffer, thereby maintaining a relatively stable pressure in the evaporation unit.

[0016] In this device, the gas phase outlet of the separation chamber is connected to the gas phase inlet of the heating chamber, and the gas phase generated during the separation process re-enters the heating chamber as a heating medium, so that the waste heat is further utilized.

[0017] In this device, the material outlets of the heating chamber and the separation chamber are connected to the liquid outlet pipe, which is then connected to the discharge pipe and the circulation pipe, respectively. The discharge pipe is connected to the concentrated liquid storage tank, and the circulation pipe is connected to the material inlet of the heating chamber. A density meter is installed on the liquid outlet pipe, a discharge valve and a discharge pump are installed on the discharge pipe, and a circulation valve and a circulation pump are installed on the circulation pipe. The density meter is interlocked with the discharge valve, discharge pump, circulation valve, and circulation pump. The density meter can effectively monitor the solid content of the evaporated liquid. If the solid content meets the standard, it will be directly transferred to the concentrated liquid storage tank. If the solid content is too low, it will be re-entered into the heating chamber for further evaporation, thereby improving the concentration efficiency. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0019] Figure 1 It is a structural schematic diagram of an embodiment of the utility model;

[0020] In the figure, 1. Flash tank; 2. Evaporation device; 3. Condensate recovery tank; 4. Concentrate storage tank; 5. Hydrolysis tank; 6. Discharge regulating valve; 7. Feed regulating valve; 8. Flash buffer tank; 9. Separation chamber; 10. Heating chamber; 11. Feed pump; 12. Liquid outlet pipe; 13. Discharge pipe; 14. Circulation pipe; 15. Density meter; 16. Discharge valve; 17. Discharge pump; 18. Circulation valve; 19. Circulation pump. DETAILED DESCRIPTION

[0021] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the embodiments described are only part of the embodiments of the present invention, not all of them. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of the present invention.

[0022] Example

[0023] like Figure 1 As shown, a device for continuously hydrolyzing potassium phytate and recovering condensed water comprises a flash tank 1, a hydrolysis system and an evaporation device 2, wherein the material inlet of the flash tank 1 is connected to the hydrolysis system, the gas phase outlet of the flash tank 1 is connected to the gas phase inlet of the evaporation device 2, the liquid phase outlet of the flash tank 1 is connected to the material inlet of the evaporation device 2, the condensate outlet of the evaporation device 2 is connected to a condensate recovery tank 3, and the liquid phase outlet of the evaporation device 2 is connected to a concentrated liquid storage tank 4;

[0024] The hydrolysis system includes multiple hydrolysis tanks 5 respectively connected to the flash tank 1, and the connecting pipes between the multiple hydrolysis tanks 5 and the flash tank 1 are each provided with a discharge regulating valve 6; the feed pipes of the multiple hydrolysis tanks 5 are each provided with a feed regulating valve 7.

[0025] In the above scheme, the flash tank 1 is respectively connected to multiple hydrolysis tanks 5, and the multiple hydrolysis tanks 5 are used independently. The feed flow rate and the discharge flow rate are effectively controlled by the feed regulating valve 7 and the discharge regulating valve 6, thereby adjusting the feed time and the discharge time. By reasonably adjusting the feed interval time and the hydrolysis time of the adjacent hydrolysis tanks 5, the hydrolysis tank 5 at the head end starts to discharge after the hydrolysis is completed, and the hydrolysis tank 5 at the adjacent rear end starts to discharge just after the hydrolysis is completed. This cycle is repeated. The arrangement of multiple hydrolysis tanks 5 can ensure that the cycle of hydrolysis, flash evaporation and evaporation processes continues.

[0026] The waste heat in the flash evaporation process is used in the evaporation process, so that the waste heat is fully utilized and energy consumption is reduced. The condensed water in the evaporation process is also recycled, further saving energy and reducing consumption.

[0027] In this embodiment, the liquid phase outlet of the flash tank 1 is connected to the material inlet of the evaporation device 2 through the flash buffer tank 8. The flash buffer tank 8 not only serves as a temporary storage and transfer tank to achieve continuous production, but also plays a buffering role, thereby maintaining a relatively stable pressure in the evaporation device 2.

[0028] In this embodiment, the evaporation device 2 includes a connected separation chamber 9 and a heating chamber 10. The material inlet and gas inlet of the heating chamber 10 are respectively connected to the liquid phase outlet of the separation chamber 9 and the gas phase outlet of the flash tank 1. The gas outlet of the heating chamber 10 is connected to the separation chamber 9. The material outlets of the heating chamber 10 and the separation chamber 9 are connected to the concentrated liquid storage tank 4. The condensate outlet of the heating chamber 10 is connected to the condensate recovery tank 3. The material inlet of the separation chamber 9 is connected to the flash buffer tank 8. The separation chamber 9 performs preliminary gas-liquid separation on the flashed material. The separated liquid phase enters the heating chamber 10 for heating and concentration. The gas generated during the evaporation process enters the separation chamber 9 for further gas-liquid separation. The separated liquid phase enters the concentrated liquid storage tank 4. The condensate in the jacket of the heating chamber 10 enters the condensate recovery tank 3 for treatment. This operation not only recovers condensed water but also reuses waste heat from the flash evaporation process, saving energy and reducing consumption.

[0029] In this embodiment, feed pumps 11 are provided on the connecting pipes between the separation chamber 9 and the flash buffer tank 8 , and between the flash tank 1 and the flash buffer tank 8 .

[0030] In this embodiment, the gas phase outlet of the separation chamber 9 is connected to the gas phase inlet of the heating chamber 10. The gas phase separated during the separation process enters the heating chamber 10 again for reuse, further reducing energy consumption.

[0031] In this embodiment, the material outlets of the separation chamber 9 and the heating chamber are connected to the liquid outlet pipe 12, and the liquid outlet pipe 12 is respectively connected to the discharge pipe 13 and the circulation pipe 14, the discharge pipe 13 is connected to the concentrated liquid storage tank 4, and the circulation pipe 14 is connected to the material inlet of the heating chamber 10, and the liquid outlet pipe 12 is provided with a density meter 15, the discharge pipe 13 is provided with a discharge valve 16 and a discharge pump 17, and the circulation pipe 14 is provided with a circulation valve 18 and a circulation pump 19, and the density meter 15 is interlocked with the discharge valve 16, the discharge pump 17, the circulation valve 18 and the circulation pump 19, respectively.

[0032] Based on the above technical solution, the density meter 15 on the liquid outlet pipe 12 can detect the density of the liquid discharged from the separation chamber 9, thereby detecting the solid content of the liquid. If the solid content reaches the set value, the density meter 15 transmits the signal to the external control system (not shown in the figure), and the external control system automatically opens the discharge valve 16 and the discharge pump 17 on the discharge pipe 13, and the material enters the concentrated liquid storage tank 4. If the solid content is lower than the set value, the external control system automatically opens the circulation valve 18 and the circulation pump 19 on the circulation pipe 14, and the material re-enters the heating chamber 10 for re-concentration processing, thereby achieving precise control and efficiency of evaporation and concentration.

[0033] The above description of the disclosed embodiments will enable one skilled in the art to implement or use the present invention. Various modifications to these embodiments will be readily apparent to one skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the present invention. Therefore, the present invention is not limited to the embodiments shown herein but is intended to conform to the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A device for continuous hydrolysis of potassium phytate and recovery of condensed water, characterized by: It includes a flash tank, a hydrolysis system and an evaporation device, wherein the material inlet of the flash tank is connected to the hydrolysis system, the gas phase outlet of the flash tank is connected to the gas phase inlet of the evaporation device, the liquid phase outlet of the flash tank is connected to the material inlet of the evaporation device, the condensate outlet of the evaporation device is connected to a condensate recovery tank, and the liquid phase outlet of the evaporation device is connected to a concentrated liquid storage tank; The hydrolysis system comprises a plurality of hydrolysis tanks respectively connected to the flash tank, and the connecting pipes between the plurality of hydrolysis tanks and the flash tank are all provided with a discharge regulating valve; and the feed pipes of the plurality of hydrolysis tanks are all provided with a feed regulating valve.

2. The device for continuous hydrolysis of potassium phytate and recovery of condensed water according to claim 1, characterized in that: The liquid phase outlet of the flash tank is communicated with the material inlet of the evaporation device through the flash buffer tank.

3. The device for continuous hydrolysis of potassium phytate and recovery of condensed water according to claim 2, characterized in that: The evaporation device includes a separation chamber and a heating chamber that are connected. The material inlet and the gas phase inlet of the heating chamber are respectively connected to the liquid phase outlet of the separation chamber and the gas phase outlet of the flash tank. The gas outlet of the heating chamber is connected to the separation chamber. The material inlet of the separation chamber is connected to the flash buffer tank. The material outlet of the separation chamber and the material outlet of the heating chamber are both connected to the concentrated liquid storage tank.

4. The device for continuous hydrolysis of potassium phytate and recovery of condensed water according to claim 3, characterized in that: Feed pumps are provided on the connecting pipes between the separation chamber and the flash buffer tank, and between the flash tank and the flash buffer tank.

5. The device for continuous hydrolysis of potassium phytate and recovery of condensed water according to claim 3, characterized in that: The condensate outlet of the heating chamber is communicated with a condensate recovery tank.

6. The device for continuous hydrolysis of potassium phytate and recovery of condensed water according to claim 3, characterized in that: The gas phase outlet of the separation chamber is communicated with the gas phase inlet of the heating chamber.

7. The device for continuous hydrolysis of potassium phytate and recovery of condensed water according to claim 3, characterized in that: The material outlets of the separation chamber and the heating chamber are connected to the liquid outlet pipes, and the liquid outlet pipes are respectively connected to the discharge pipe and the circulation pipe. The discharge pipe is connected to the concentrated liquid storage tank, and the circulation pipe is connected to the material inlet of the heating chamber. A density meter is provided on the liquid outlet pipe, a discharge valve and a discharge pump are provided on the discharge pipe, and a circulation valve and a circulation pump are provided on the circulation pipe. The density meter is interlocked with the discharge valve, the discharge pump, the circulation valve and the circulation pump respectively.

Images