CN219307956U - Waste heat utilization multistage evaporation system for fructose concentration - Google Patents
Waste heat utilization multistage evaporation system for fructose concentration Download PDFInfo
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- CN219307956U CN219307956U CN202320378016.0U CN202320378016U CN219307956U CN 219307956 U CN219307956 U CN 219307956U CN 202320378016 U CN202320378016 U CN 202320378016U CN 219307956 U CN219307956 U CN 219307956U
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Abstract
The utility model discloses a waste heat utilization multistage evaporation system for fructose concentration in the field of food processing equipment, which comprises a first-effect heat exchanger, a first-effect separator, a second-effect heat exchanger, a second-effect separator, a third-effect heat exchanger, a third-effect separator, a fourth-effect heat exchanger, a fourth-effect separator, a fifth-effect heat exchanger and a fifth-effect separator which are sequentially connected in series along the material flow direction, wherein steam inlets of the first-effect heat exchanger, the second-effect heat exchanger, the third-effect heat exchanger, the fourth-effect heat exchanger and the fifth-effect heat exchanger are respectively connected with steam outlets of a secondary injection liquid flash tank, a liquefied liquid buffer tank, a first-stage flash tank, a second-stage flash tank and a third-stage flash tank. The waste heat utilization multi-stage evaporation system for fructose concentration fully utilizes the steam generated in the processes of flash evaporation of secondary injection liquid and flash evaporation of liquefied liquid in the liquefaction and saccharification processes, is used as a heat source of the evaporation concentration system, greatly reduces the raw steam consumption of the evaporation concentration system, and achieves the purpose of energy conservation.
Description
Technical Field
The utility model relates to the field of food processing equipment, in particular to a waste heat utilization multistage evaporation system for fructose concentration.
Background
The production process flow of the fructose comprises the following steps: liquefying, saccharifying, isomerising, neutralizing, filtering, ion exchange, evaporating and filling.
The liquefying is to make starch obtain preliminary decomposition by using liquefying enzyme and high-temperature steam, starch molecular chain is preliminarily cut into small molecular dextrin and a small amount of sugar component, qualified substrate is provided for saccharification, and protein is denatured and coagulated by high-temperature action, so that the starch is filtered and separated. In this stage, it is necessary to perform the steps of liquefaction preparation, primary injection, primary flash evaporation, secondary injection (the temperature reaches about 138 °), secondary flash evaporation, and the like, and finally, the mixture enters a liquefaction column to perform a laminar flow reaction.
Saccharification is to flash-cool the liquefied liquid (with temperature of 95 deg.c) from the liquefied column for three times, cool the temperature to 60 deg.c, regulate the pH value of the liquefied liquid to 4.0-4.3 and add saccharifying enzyme. Then the mixture enters a saccharification tank for continuous reaction until the glucose value (DE value) in the saccharification tank is detected to reach more than 95 percent and is a qualified material.
A large amount of steam is generated in the processes of flash evaporation of the secondary injection liquid and flash evaporation of the liquefied liquid, and the steam is not effectively and reasonably utilized in the fructose production process in the prior art. In addition, in the fructose production process, a large amount of raw steam is consumed in the subsequent evaporation and concentration process, and with the continuous rising of steam prices in recent years, the energy consumption in the evaporation process enables the running cost burden of enterprises to be increased sharply, and meanwhile, the energy-saving, environment-friendly and emission-reducing work becomes a national major affair participated in by each enterprise. Therefore, the reasonable utilization of the high-temperature steam in the flash evaporation process and the reduction of the steam consumption in the fructose production process have great practical significance.
Disclosure of Invention
The utility model aims to provide a waste heat utilization multi-stage evaporation system for fructose concentration, so as to achieve the purposes of energy conservation and emission reduction.
The purpose of the utility model is realized in the following way: a waste heat utilization multistage evaporation system for fructose is concentrated, including the first effect heat exchanger, first effect separator, second effect heat exchanger, second effect separator, third effect heat exchanger, third effect separator, fourth effect heat exchanger, fourth effect separator, fifth effect heat exchanger, fifth effect separator of establishing ties in proper order along the material flow direction, the steam inlet of first effect heat exchanger, second effect heat exchanger, third effect heat exchanger, fourth effect heat exchanger, fifth effect heat exchanger is connected with the steam outlet of secondary injection flash tank, liquefaction buffer tank, first order flash tank, second order flash tank, tertiary flash tank respectively.
The waste heat utilization multi-stage evaporation system for fructose concentration fully utilizes the steam generated in the processes of flash evaporation of secondary injection liquid and flash evaporation of liquefied liquid in the liquefaction and saccharification processes, is used as a heat source of the evaporation concentration system, greatly reduces the raw steam consumption of the evaporation concentration system, and achieves the purpose of energy conservation.
As a further improvement of the utility model, the steam outlets of the first-effect separator, the second-effect separator, the third-effect separator and the fourth-effect separator are respectively connected with the steam inlets of the second-effect heat exchanger, the third-effect heat exchanger, the fourth-effect heat exchanger and the fifth-effect heat exchanger, so that the secondary steam discharged by the separators is fully utilized, and the raw steam consumption is reduced.
As a further improvement of the utility model, a primary preheater, a four-effect preheater, a three-effect preheater, a two-effect preheater and a one-effect preheater are sequentially connected in series on a feed pipe of the one-effect heat exchanger, a discharge port of the one-effect preheater is connected with a feed inlet of the one-effect heat exchanger, and steam inlet pipelines of the one-effect preheater, the two-effect preheater, the three-effect preheater and the four-effect preheater are respectively connected with steam inlet pipelines of the one-effect heat exchanger, the two-effect heat exchanger, the three-effect heat exchanger and the four-effect heat exchanger in parallel. That is, the flash steam generated by the flash vaporization system and the secondary steam discharged from the separator are used as heat sources of the heater and the preheater at the same time, so that the raw steam consumption of the whole system is further reduced.
The utility model further improves, still include one effect condensate water tank, two effect condensate water tank, three effect condensate water tank, four effect condensate water tank, five effect condensate water tank, one effect heat exchanger, two effect heat exchanger, three effect heat exchanger, four effect heat exchanger, five effect heat exchanger's liquid outlet is connected with the inlet of one effect condensate water tank, two effect condensate water tank, three effect condensate water tank, four effect condensate water tank, five effect condensate water tank respectively, the outlet of one effect preheater, two effect preheater, three effect preheater, four effect preheater is connected with the inlet of one effect condensate water tank, two effect condensate water tank, three effect condensate water tank, four effect condensate water tank respectively, the outlet of four effect condensate water tank is connected with the inlet of primary preheater, make full use of comdenstion water residual temperature as primary preheater heat source, the energy consumption is saved.
As a further improvement of the utility model, the evaporator further comprises a condenser and a final condensing water tank, wherein the steam outlet of the five-effect separator is connected with the heat medium inlet of the condenser, the heat medium outlet of the condenser is connected with the liquid inlet of the final condensing water tank, the liquid outlet of the five-effect condensing water tank is connected with the liquid inlet of the final condensing water tank, the gas-liquid separation is realized, and the final exhaust temperature of the evaporation concentration system is reduced.
As a further improvement of the utility model, the non-condensable gas outlet at the top of the first-effect condensation water tank, the second-effect condensation water tank, the third-effect condensation water tank, the fourth-effect condensation water tank and the fifth-effect condensation water tank is connected with the heat medium inlet of the condenser, so as to reduce the exhaust temperature.
As a further improvement of the utility model, the first-effect heat exchanger, the second-effect heat exchanger, the third-effect heat exchanger, the fourth-effect heat exchanger, the fifth-effect heat exchanger and the condenser all adopt plate heat exchangers, and the structure is compact and the heat transfer efficiency is high.
Drawings
Fig. 1 is a schematic diagram of a waste heat utilization multistage evaporation system for fructose concentration of the present utility model.
The device comprises a first-effect heat exchanger 1, a first-effect separator 2, a second-effect heat exchanger 3, a second-effect separator 4, a third-effect heat exchanger 5, a third-effect separator 6, a fourth-effect heat exchanger 7, a fourth-effect separator 8, a fifth-effect heat exchanger 9, a fifth-effect separator 10, a flash tank for 11 secondary injection liquid, a buffer tank for 12 liquefied liquid, a first-stage flash tank 13, a second-stage flash tank 14, a third-stage flash tank 15, a first-stage preheater 16, a fourth-effect preheater 17, a third-effect preheater 18, a second-effect preheater 19, a first-effect preheater 20, a first-effect condensate tank 21, a second-effect condensate tank 22, a third-effect condensate tank 23, a fourth-effect condensate tank 24, a fifth-effect condensate tank 25, a condenser 26 and a final condensate tank 27.
Description of the embodiments
The waste heat utilization multistage evaporation system for fructose concentration shown in fig. 1 comprises a first-effect heat exchanger 1, a first-effect separator 2, a second-effect heat exchanger 3, a second-effect separator 4, a third-effect heat exchanger 5, a third-effect separator 6, a fourth-effect heat exchanger 7, a fourth-effect separator 8, a fifth-effect heat exchanger 9 and a fifth-effect separator 10 which are sequentially connected in series along the material flow direction.
In order to fully utilize steam generated in the processes of flash evaporation of secondary injection liquid and flash evaporation of liquefied liquid in the processes of liquefying and saccharifying in the fructose production process, steam inlets of the first-effect heat exchanger 1, the second-effect heat exchanger 3, the third-effect heat exchanger 5, the fourth-effect heat exchanger 7 and the fifth-effect heat exchanger 9 are respectively connected with steam outlets of the secondary injection liquid flash evaporation tank 11, the liquefied liquid buffer tank 12, the first-stage flash evaporation tank 13, the second-stage flash evaporation tank 14 and the third-stage flash evaporation tank 15, namely, the steam generated in the processes of liquefying and saccharifying is used as a heat source of a heat exchanger in an evaporation concentration system. The steam inlet of the first-effect heat exchanger 1 is also connected with an external low-pressure steam delivery pipeline, so that part of generated steam can be conveniently supplemented according to the needs of the evaporation system in real time.
As shown in the figure, the steam outlets of the first-effect separator 2, the second-effect separator 4, the third-effect separator 6 and the fourth-effect separator 8 are respectively connected with the steam inlets of the second-effect heat exchanger 3, the third-effect heat exchanger 5, the fourth-effect heat exchanger 7 and the fifth-effect heat exchanger 9, so that the secondary steam discharged by the separators is fully utilized, and the raw steam consumption is reduced.
The feeding pipe of the first-effect heat exchanger 1 is sequentially connected with a primary preheater 16, a four-effect preheater 17, a three-effect preheater 18, a two-effect preheater 19 and a first-effect preheater 20 in series. The discharge port of the primary preheater 20 is connected with the feed port of the primary heat exchanger 1. The steam inlet pipelines of the first-effect preheater 20, the second-effect preheater 19, the third-effect preheater 18 and the fourth-effect preheater 17 are respectively connected with the steam inlet pipelines of the first-effect heat exchanger 1, the second-effect heat exchanger 3, the third-effect heat exchanger 5 and the fourth-effect heat exchanger 7 in parallel. That is, the flash steam generated by the flash vaporization system and the secondary steam discharged from the separator are used as heat sources of the heater and the preheater at the same time, so that the raw steam consumption of the whole system is further reduced.
The waste heat utilization multistage evaporation system for fructose concentration of the present embodiment further includes a first-effect condensate water tank 21, a second-effect condensate water tank 22, a third-effect condensate water tank 23, a fourth-effect condensate water tank 24, a fifth-effect condensate water tank 25, a condenser 26, and a final condensate water tank 27. The liquid outlets of the first-effect heat exchanger 1, the second-effect heat exchanger 3, the third-effect heat exchanger 5, the fourth-effect heat exchanger 7 and the fifth-effect heat exchanger 9 are respectively connected with the liquid inlets of the first-effect condensation water tank 21, the second-effect condensation water tank 22, the third-effect condensation water tank 23, the fourth-effect condensation water tank 24 and the fifth-effect condensation water tank 25, the liquid outlets of the first-effect preheater 20, the second-effect preheater 19, the third-effect preheater 18 and the fourth-effect preheater 17 are respectively connected with the liquid inlets of the first-effect condensation water tank 21, the second-effect condensation water tank 22, the third-effect condensation water tank 23 and the fourth-effect condensation water tank 24, the liquid outlet of the fourth-effect condensation water tank 24 is connected with the liquid inlet of the primary preheater 16, and the residual temperature of condensate water is fully utilized as the heat source of the primary preheater 16, so that the energy consumption is saved. The steam outlet of the five-effect separator 10 is connected with the heat medium inlet of the condenser 26, the heat medium outlet of the condenser 26 is connected with the liquid inlet of the final condensation water tank 27, the liquid outlet of the five-effect condensation water tank 25 is connected with the liquid inlet of the final condensation water tank 27, the gas-liquid separation is realized, and the final exhaust temperature of the evaporation concentration system is reduced. The non-condensable gas outlets at the tops of the first-effect condensation water tank 21, the second-effect condensation water tank 22, the third-effect condensation water tank 23, the fourth-effect condensation water tank 24 and the fifth-effect condensation water tank 25 are connected with the heat medium inlet of the condenser 26, so that the exhaust temperature is reduced. The first-effect heat exchanger 1, the second-effect heat exchanger 3, the third-effect heat exchanger 5, the fourth-effect heat exchanger 7, the fifth-effect heat exchanger 9 and the condenser 26 are all plate heat exchangers, and the heat exchanger has compact structure and high heat transfer efficiency.
The utility model is not limited to the above embodiments, and based on the technical solution disclosed in the utility model, a person skilled in the art may make some substitutions and modifications to some technical features thereof without creative effort according to the technical content disclosed, and all the substitutions and modifications are within the protection scope of the utility model.
Claims (7)
1. A waste heat utilization multistage vaporization system for fructose is concentrated, includes one effect heat exchanger, one effect separator, two effect heat exchangers, two effect separators, three effect heat exchangers, three effect separators, four effect heat exchangers, four effect separators, five effect heat exchangers, five effect separators that establish ties in proper order along material flow direction, its characterized in that: and steam inlets of the first-effect heat exchanger, the second-effect heat exchanger, the third-effect heat exchanger, the fourth-effect heat exchanger and the fifth-effect heat exchanger are respectively connected with steam outlets of the secondary injection liquid flash tank, the liquefied liquid buffer tank, the primary flash tank, the secondary flash tank and the tertiary flash tank.
2. The waste heat utilization multistage evaporation system for fructose concentration according to claim 1, wherein: and steam outlets of the first-effect separator, the second-effect separator, the third-effect separator and the fourth-effect separator are respectively connected with steam inlets of the second-effect heat exchanger, the third-effect heat exchanger, the fourth-effect heat exchanger and the fifth-effect heat exchanger.
3. The waste heat utilization multistage evaporation system for fructose concentration according to claim 2, wherein: the feeding pipe of the first-effect heat exchanger is sequentially connected with the first-effect preheater, the fourth-effect preheater, the third-effect preheater, the second-effect preheater and the first-effect preheater in series, the discharge port of the first-effect preheater is connected with the feeding port of the first-effect heat exchanger, and the steam inlet pipelines of the first-effect preheater, the second-effect preheater, the third-effect preheater and the fourth-effect preheater are respectively connected with the steam inlet pipelines of the first-effect heat exchanger, the second-effect heat exchanger, the third-effect heat exchanger and the fourth-effect heat exchanger in parallel.
4. A waste heat utilization multistage evaporation system for fructose concentration according to claim 3, wherein: the liquid outlet of the first-effect heat exchanger, the second-effect heat exchanger, the third-effect heat exchanger, the fourth-effect heat exchanger and the fifth-effect heat exchanger is respectively connected with the liquid inlets of the first-effect condensate water tank, the second-effect condensate water tank, the third-effect condensate water tank, the fourth-effect condensate water tank and the fifth-effect condensate water tank, and the liquid outlets of the first-effect preheater, the second-effect preheater, the third-effect preheater and the fourth-effect preheater are respectively connected with the liquid inlets of the first-effect condensate water tank, the second-effect condensate water tank, the third-effect condensate water tank and the fourth-effect condensate water tank, and the liquid outlet of the fourth-effect condensate water tank is connected with the liquid inlet of the primary preheater.
5. The waste heat utilization multistage evaporation system for fructose concentration according to claim 4, wherein: the device comprises a condenser, a final condensing water tank, a steam outlet of a five-effect separator is connected with a heat medium inlet of the condenser, a heat medium outlet of the condenser is connected with a liquid inlet of the final condensing water tank, and a liquid outlet of the five-effect condensing water tank is connected with a liquid inlet of the final condensing water tank.
6. The waste heat utilization multistage evaporation system for fructose concentration of claim 5, wherein: the non-condensable gas outlet at the top of the first-effect condensation water tank, the second-effect condensation water tank, the third-effect condensation water tank, the fourth-effect condensation water tank and the fifth-effect condensation water tank is connected with the heat medium inlet of the condenser.
7. The waste heat utilization multistage evaporation system for fructose concentration according to any one of claims 5 to 6, wherein: the first-effect heat exchanger, the second-effect heat exchanger, the third-effect heat exchanger, the fourth-effect heat exchanger, the fifth-effect heat exchanger and the condenser are all plate heat exchangers.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320378016.0U CN219307956U (en) | 2023-03-03 | 2023-03-03 | Waste heat utilization multistage evaporation system for fructose concentration |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320378016.0U CN219307956U (en) | 2023-03-03 | 2023-03-03 | Waste heat utilization multistage evaporation system for fructose concentration |
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| CN219307956U true CN219307956U (en) | 2023-07-07 |
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| CN202320378016.0U Active CN219307956U (en) | 2023-03-03 | 2023-03-03 | Waste heat utilization multistage evaporation system for fructose concentration |
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