Sorbitol membrane concentration device with high energy utilization rate

Abstract

The utility model relates to the technical field of material concentration, and particularly discloses a sorbitol membrane concentration device with a high energy utilization rate, which comprises a raw material tank, a booster pump, a heat exchanger in front of the raw material tank, a pretreatment micron filter and a high-pressure pump which are sequentially communicated, and an outlet of the high-pressure pump is sequentially connected with a first internal circulating pump and a first membrane concentration device; an outlet of the first membrane concentration device is sequentially connected with a second internal circulating pump and a second membrane concentration device, an outlet of the second membrane concentration device is sequentially connected with a third internal circulating pump and a third membrane concentration device, and an outlet of the third membrane concentration device is sequentially connected with a fourth internal circulating pump and a fourth membrane concentration device; and an outlet of the fourth membrane concentration device is sequentially connected with a fifth internal circulating pump and a fifth membrane concentration device. According to the utility model, the sorbitol byproduct can be concentrated, the steam consumption of the evaporator is reduced, the sorbitol production cost of an enterprise is reduced, and high-quality penetrating fluid can be obtained.

Description

Technical Field

[0001] The utility model relates to the technical field of material concentration, in particular to a sorbitol membrane concentration device with high energy utilization rate. Background Art

[0002] Sorbitol, also known as sorbitol, is a white hygroscopic powder or crystalline powder, flakes or granules. It is odorless, easily soluble in water, slightly soluble in ethanol and acetic acid, has a refreshing sweet taste, is about half as sweet as sucrose, and has a calorific value similar to sucrose.

[0003] Sorbitol is widely used in food, medicine, metallurgy, textile and other industries, and has rich application value. At present, the existing sorbitol production and processing enterprises in China mainly adopt the process of starch sugar fermentation-simulated moving bed-evaporation, and the evaporation cost of sorbitol production by this process is relatively high.

[0004] In view of this situation, it is an inevitable trend to increase the concentration of sorbitol byproducts and reduce the amount of steam used in the evaporator to maximize energy saving and consumption reduction. Therefore, by using the membrane concentration process between the simulated moving bed and the evaporation process, the liquid entering the evaporator is first concentrated by the membrane concentration device before entering the evaporator, which can help sorbitol manufacturers achieve a significant reduction in production costs. Utility Model Content

[0005] In order to solve the above-mentioned problems existing in the prior art, the utility model provides a sorbitol membrane concentration device with high energy utilization rate, which can concentrate sorbitol by-products, reduce evaporator steam consumption, reduce the cost of sorbitol production by enterprises, and obtain high-quality permeate, which can be used for cleaning the entire set of sorbitol production process equipment, thereby saving energy and reducing consumption while improving energy utilization rate.

[0006] The purpose of the utility model can be achieved through the following technical solutions:

[0007] A sorbitol membrane concentrator with high energy utilization efficiency, comprising a raw material tank, a booster pump, a heat exchanger before the raw material tank, a pretreatment micron filter, and a high-pressure pump connected in sequence, wherein the outlet of the high-pressure pump is connected in sequence to a first internal circulation pump and a first membrane concentrator, the outlet of the first membrane concentrator is connected in sequence to a second internal circulation pump and a second membrane concentrator, the outlet of the second membrane concentrator is connected in sequence to a third internal circulation pump and a third membrane concentrator, the outlet of the third membrane concentrator is connected in sequence to a fourth internal circulation pump and a fourth membrane concentrator, and the outlet of the fourth membrane concentrator is connected in sequence to a fifth internal circulation pump and a fifth membrane concentrator;

[0008] The outlet of the fifth membrane concentrating device is connected to the heat exchanger after the raw material tank and the concentrated liquid tank in sequence, the first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device are connected to the permeate tank, and the outlet of the concentrated liquid tank is connected to the raw material tank.

[0009] Furthermore, the high-pressure pump is provided with a variable frequency starter, the inlet and outlet of the high-pressure pump are provided with a pressure transmitter, and the outlet of the high-pressure pump is provided with an automatic valve.

[0010] Furthermore, the operating temperature of the first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device is 20°C to 30°C.

[0011] Furthermore, the first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device are all provided with internal circulation.

[0012] Furthermore, the outlets of the first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device are all provided with pipelines and automatic valves for returning to the inlet of the internal circulation pump.

[0013] Furthermore, the first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device have the same number of membrane branches.

[0014] The beneficial effects of the utility model are:

[0015] (1) By setting a heat exchanger before the raw material tank, a pretreatment micron filter, a heat exchanger after the raw material tank and a permeate tank, the technical effect that can be achieved is that the sorbitol byproduct liquid can be concentrated through the treatment of the device, and a permeate with good quality can be separated. The permeate can be used for cleaning the whole set of equipment in the sorbitol production process, reducing the evaporation cost while improving the energy utilization rate. The cold source of the heat exchanger before the raw material tank for preliminary cooling of the raw material is the concentrated liquid generated by the system, which can obtain a certain amount of heat while cooling the raw material, reducing the heat loss of the system, and maximizing the energy utilization rate of the whole system.

[0016] (2) By setting up the first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device, the technical effect that can be achieved is that the number of membranes in the first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device is the same, and each membrane concentrating device can serve as a backup for each other to ensure the flexibility of the overall operation of the system. The use of internal circulation can ensure that each membrane concentrating device has a sufficient feed amount, thereby increasing the concentration multiple of the system. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] In order to facilitate understanding by those skilled in the art, the present invention is further described below in conjunction with the accompanying drawings.

[0018] Figure 1 It is a schematic diagram of the overall structure of the utility model;

[0019] Description of main component symbols:

[0020] In the figure: 1. Raw material tank; 2. Booster pump; 3. Heat exchanger before raw material tank; 4. Pretreatment micron filter; 5. High-pressure pump; 6. First internal circulation pump; 7. First membrane concentration device; 8. Second internal circulation pump; 9. Second membrane concentration device; 10. Third internal circulation pump; 11. Third membrane concentration device; 12. Fourth internal circulation pump; 13. Fourth membrane concentration device; 14. Fifth internal circulation pump; 15. Fifth membrane concentration device; 16. Heat exchanger after raw material tank; 17. Permeate tank; 18. Concentrate tank. DETAILED DESCRIPTION

[0021] The technical solutions in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application; obviously, the described embodiments are only part of the embodiments of the present application, rather than all the embodiments, and all other embodiments obtained by ordinary technicians in this field based on the embodiments in the present application without making creative work are within the scope of protection of the present application.

[0022] In the description of the present application, it should be noted that the terms "upper", "lower", "inner", "outer", "top / bottom" and the like indicate positions or positional relationships based on the positions or positional relationships shown in the drawings, and are only for the convenience of describing the present application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific position, be constructed and operated in a specific position, and therefore cannot be understood as limiting the present application. In addition, the terms "first" and "second" are used for descriptive purposes only, and cannot be understood as indicating or implying relative importance.

[0023] In the description of this application, it should be noted that, unless otherwise clearly specified and limited, the terms "installed", "provided with", "set / connected", "connected", etc. should be understood in a broad sense. For example, "connected" can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0024] Reference Figure 1 , which is a sorbitol membrane concentrator with high energy utilization rate disclosed in the utility model, comprising a raw material tank 1, a booster pump 2, a heat exchanger before the raw material tank 1, a pretreatment micron filter 4, and a high-pressure pump 5 connected in sequence, the outlet of the high-pressure pump 5 is connected in sequence with a first internal circulation pump 6 and a first membrane concentrator 7, the outlet of the first membrane concentrator 7 is connected in sequence with a second internal circulation pump 8 and a second membrane concentrator 9, the outlet of the second membrane concentrator 9 is connected in sequence with a third internal circulation pump 10 and a third membrane concentrator 11, the outlet of the third membrane concentrator 11 is connected in sequence with a fourth internal circulation pump 12 and a fourth membrane concentrator 13, and the outlet of the fourth membrane concentrator 13 is connected in sequence with a fifth internal circulation pump 14 and a fifth membrane concentrator 15.

[0025] The outlet of the fifth membrane concentrator 15 is connected to the heat exchanger after the raw material tank 1 and the concentrated liquid tank 18 in sequence, the first membrane concentrator 7, the second membrane concentrator 9, the third membrane concentrator 11, the fourth membrane concentrator 13 and the fifth membrane concentrator 15 are connected to the permeate tank 17, and the outlet of the concentrated liquid tank 18 is connected to the raw material tank 1.

[0026] The high-pressure pump 5 is provided with a variable frequency starter, the inlet and outlet of the high-pressure pump 5 is provided with a pressure transmitter, and the outlet of the high-pressure pump 5 is provided with an automatic valve.

[0027] The operating temperature of the first membrane concentrating device 7, the second membrane concentrating device 9, the third membrane concentrating device 11, the fourth membrane concentrating device 13 and the fifth membrane concentrating device 15 is 20°C to 30°C.

[0028] The first membrane concentrating device 7 , the second membrane concentrating device 9 , the third membrane concentrating device 11 , the fourth membrane concentrating device 13 and the fifth membrane concentrating device 15 are all provided with internal circulation.

[0029] The outlets of the first membrane concentrating device 7 , the second membrane concentrating device 9 , the third membrane concentrating device 11 , the fourth membrane concentrating device 13 and the fifth membrane concentrating device 15 are all provided with pipelines and automatic valves for returning to the inlet of the internal circulation pump.

[0030] The first membrane concentrating device 7, the second membrane concentrating device 9, the third membrane concentrating device 11, the fourth membrane concentrating device 13 and the fifth membrane concentrating device 15 have the same number of membranes, and each membrane concentrating device can serve as a backup for each other to ensure the flexibility of the overall operation of the system. The use of internal circulation can ensure that each membrane concentrating device has sufficient feed volume, thereby increasing the concentration multiple of the system.

[0031] Through the treatment of the device, the sorbitol byproduct liquid can be concentrated and a permeate with good quality can be separated. The permeate can be used for cleaning the whole set of equipment for sorbitol production process, reducing the evaporation cost and improving the energy utilization rate. The cold source of the heat exchanger before the raw material tank 1 for preliminary cooling of the raw material is the concentrated liquid produced by the system, which can obtain a certain amount of heat while cooling the raw material, reducing the heat loss of the system and maximizing the energy utilization rate of the whole system.

[0032] The working principle and use process of the utility model are as follows: when the temperature of the sorbitol byproduct raw material is 70°C to 80°C, it enters the heat exchanger in front of the raw material tank 1 through the feed pipeline, and the raw material is initially cooled when the concentrated liquid is at 20°C to 30°C. At the same time, the temperature of the concentrated liquid transported to the evaporation system is increased to reduce the evaporation cost. The initially heated raw material enters the raw material tank 1 through the pipeline from the raw material outlet of the heat exchanger in front of the raw material tank 1.

[0033] The initially heated raw materials enter the raw material tank 1 through the booster pump 2 and are cooled again by the heat exchanger. The raw material temperature is reduced to 20°C to 30°C. The design of the heat exchanger after the raw material tank 1 ensures that the raw material temperature can be effectively controlled at 20°C to 30°C.

[0034] The raw materials at 20°C to 30°C enter the pretreatment micron filter 4 from the raw material outlet of the heat exchanger after the raw material tank 1 through a pipeline to remove suspended impurities and fine particles in the raw materials.

[0035] The output of the pretreatment micron filter 4 enters the first membrane concentrating device 7 through the high-pressure pump 5 and the internal circulation pump of the first membrane concentrating device 7. The membrane concentrating devices are respectively five sequentially connected first membrane concentrating device 7, second membrane concentrating device 9, third membrane concentrating device 11, fourth membrane concentrating device 13, and fifth membrane concentrating device 15, that is, it is divided into five stages of concentration.

[0036] The concentrated liquid of the first membrane concentrating device 7 is connected to the inlet of the internal circulation pump of the second membrane concentrating device 9 through a pipeline, and enters the second section through the circulation pump for further concentration. The concentrated liquid of the second membrane concentrating device 9 is connected to the inlet of the internal circulation pump of the third membrane concentrating device 11 through a pipeline, and enters the third section through the circulation pump for further concentration. The concentrated liquid of the third membrane concentrating device 11 is connected to the inlet of the internal circulation pump of the fourth membrane concentrating device 13 through a pipeline, and enters the fourth section through the circulation pump for further concentration. The concentrated liquid of the fourth membrane concentrating device 13 is connected to the inlet of the internal circulation pump of the fifth membrane concentrating device 15 through a pipeline, and enters the fifth section through the circulation pump for further concentration and separation, wherein the permeate of the first section, the second section, the third section, the fourth section and the fifth section are respectively collected in the permeate tank.

[0037] The five membrane concentration devices concentrate and separate the sorbitol byproduct delivered by the high-pressure pump 5. The design of the internal circulation pump can ensure that each membrane concentration device has a sufficient feed volume, thereby increasing the concentration multiple of the system.

[0038] When one of the backup membrane concentrators is undergoing chemical cleaning, the remaining four membrane concentrators can operate normally; when the first membrane concentrator 7 is undergoing cleaning, the second membrane concentrator 9 is used as the first membrane concentrator 7, the third membrane concentrator 11 is used as the second membrane concentrator 9, the fourth membrane concentrator 13 is used as the third membrane concentrator 11, the fifth membrane concentrator 15 is used as the fourth membrane concentrator 13, and the same applies to the other membrane concentrators during cleaning, thereby ensuring that the system can operate continuously and stably for 24 hours.

[0039] The above description is only a preferred embodiment of the present invention and does not constitute any form of limitation to the present invention. Although the present invention has been disclosed as a preferred embodiment as above, it is not intended to limit the present invention. Any technical personnel in this field can make some changes or modify the technical contents disclosed above into equivalent embodiments without departing from the scope of the technical solution of the present invention. However, any brief modifications, equivalent changes and modifications made to the above embodiments based on the technical essence of the present invention without departing from the content of the technical solution of the present invention still fall within the scope of the technical solution of the present invention.

Claims

1. A sorbitol membrane concentration device with high energy utilization efficiency, characterized in that: It comprises a raw material tank, a booster pump, a heat exchanger before the raw material tank, a pretreatment micron filter, and a high-pressure pump which are connected in sequence, wherein the outlet of the high-pressure pump is connected in sequence to a first internal circulation pump and a first membrane concentrating device, the outlet of the first membrane concentrating device is connected in sequence to a second internal circulation pump and a second membrane concentrating device, the outlet of the second membrane concentrating device is connected in sequence to a third internal circulation pump and a third membrane concentrating device, the outlet of the third membrane concentrating device is connected in sequence to a fourth internal circulation pump and a fourth membrane concentrating device, and the outlet of the fourth membrane concentrating device is connected in sequence to a fifth internal circulation pump and a fifth membrane concentrating device; The outlet of the fifth membrane concentrating device is connected to the heat exchanger after the raw material tank and the concentrated liquid tank in sequence, the first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device are connected to the permeate tank, and the outlet of the concentrated liquid tank is connected to the raw material tank.

2. The sorbitol membrane concentration device with high energy utilization rate according to claim 1, characterized in that: The high-pressure pump is provided with a variable frequency starter, the inlet and outlet of the high-pressure pump are provided with a pressure transmitter, and the outlet of the high-pressure pump is provided with an automatic valve.

3. The sorbitol membrane concentration device with high energy utilization rate according to claim 1, characterized in that: The operating temperature of the first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device is 20°C to 30°C.

4. The sorbitol membrane concentration device with high energy utilization rate according to claim 1, characterized in that: The first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device are all provided with internal circulation.

5. The sorbitol membrane concentration device with high energy utilization rate according to claim 1, characterized in that: The outlets of the first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device are all provided with pipelines and automatic valves for returning to the inlet of the internal circulation pump.

6. The sorbitol membrane concentration device with high energy utilization efficiency according to claim 1, characterized in that: The first membrane concentrating device, the second membrane concentrating device, the third membrane concentrating device, the fourth membrane concentrating device and the fifth membrane concentrating device have the same number of membrane branches.

Images