CN115245687B - Five-effect evaporation system for sugar production and use method - Google Patents
Five-effect evaporation system for sugar production and use method Download PDFInfo
- Publication number
- CN115245687B CN115245687B CN202210776401.0A CN202210776401A CN115245687B CN 115245687 B CN115245687 B CN 115245687B CN 202210776401 A CN202210776401 A CN 202210776401A CN 115245687 B CN115245687 B CN 115245687B
- Authority
- CN
- China
- Prior art keywords
- juice
- effect evaporation
- heater
- effect
- stage
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000001704 evaporation Methods 0.000 title claims abstract description 270
- 230000008020 evaporation Effects 0.000 title claims abstract description 253
- 235000000346 sugar Nutrition 0.000 title claims abstract description 49
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims abstract description 22
- 235000011389 fruit/vegetable juice Nutrition 0.000 claims abstract description 234
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 107
- 230000000694 effects Effects 0.000 claims abstract description 75
- 238000009833 condensation Methods 0.000 claims abstract description 71
- 230000005494 condensation Effects 0.000 claims abstract description 71
- 239000006188 syrup Substances 0.000 claims abstract description 27
- 235000020357 syrup Nutrition 0.000 claims abstract description 26
- 238000002425 crystallisation Methods 0.000 claims description 11
- 230000008025 crystallization Effects 0.000 claims description 11
- 235000021552 granulated sugar Nutrition 0.000 claims description 6
- 238000001035 drying Methods 0.000 claims description 5
- 239000011552 falling film Substances 0.000 claims description 5
- 238000005406 washing Methods 0.000 claims description 4
- 230000008569 process Effects 0.000 abstract description 9
- 235000013311 vegetables Nutrition 0.000 abstract description 6
- 239000002918 waste heat Substances 0.000 abstract description 4
- 238000012546 transfer Methods 0.000 description 9
- 235000016068 Berberis vulgaris Nutrition 0.000 description 6
- 241000335053 Beta vulgaris Species 0.000 description 6
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 5
- 229930006000 Sucrose Natural products 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 241000196324 Embryophyta Species 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000007738 vacuum evaporation Methods 0.000 description 3
- 240000000111 Saccharum officinarum Species 0.000 description 2
- 235000007201 Saccharum officinarum Nutrition 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000003068 static effect Effects 0.000 description 2
- 241000219310 Beta vulgaris subsp. vulgaris Species 0.000 description 1
- CZMRCDWAGMRECN-UHFFFAOYSA-N Rohrzucker Natural products OCC1OC(CO)(OC2OC(CO)C(O)C(O)C2O)C(O)C1O CZMRCDWAGMRECN-UHFFFAOYSA-N 0.000 description 1
- 235000021536 Sugar beet Nutrition 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 235000021551 crystal sugar Nutrition 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 235000012907 honey Nutrition 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000010409 ironing Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
-
- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13B—PRODUCTION OF SUCROSE; APPARATUS SPECIALLY ADAPTED THEREFOR
- C13B25/00—Evaporators or boiling pans specially adapted for sugar juices; Evaporating or boiling sugar juices
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Biochemistry (AREA)
- Organic Chemistry (AREA)
- Non-Alcoholic Beverages (AREA)
Abstract
The invention provides a five-effect evaporation system for sugar production and a use method thereof, belonging to the technical field of sugar production, wherein the five-effect evaporation system for sugar production comprises a heater assembly, an evaporation tank assembly, a condensation water self-evaporation assembly and a syrup balance tank, wherein an inlet of a primary dilute juice heater in the heater assembly is connected with a juice inlet pipe; the juice inlet pipe of the fourth-effect evaporation tank in the evaporation tank assembly is connected with the outlet of the second-stage dilute juice heater, the juice outlet pipe is connected with the inlet of the third dilute juice heater through a sugar juice pump, the outlet of the fifth dilute juice heater is connected with the juice inlet pipe of the first-effect evaporation tank, the condensation water self-evaporation assembly is used for storing condensation water of the first-effect evaporation tank to the fifth-effect evaporation tank, the first-effect condensation water drum comprises three water drums connected in series, and through the arrangement of the system, the waste heat of each stage of reaction in the evaporation process can be effectively utilized, so that the total steam consumption of the sugar making evaporation process is reduced to 25.2% to the vegetable from more than 35% to the original vegetable, and the energy-saving effect is achieved.
Description
Technical Field
The invention relates to the technical field of sugar production, in particular to a five-effect evaporation system for sugar production and a use method thereof.
Background
Sugar production refers to production activities of refining and processing various refined sugar by taking sugarcane and beet as raw materials to produce finished sugar and taking raw sugar or granulated sugar as raw materials. Including raw sugar from sugarcane, such as white sugar, soft white sugar, brown sugar (brown sugar), yellow sugar, etc.; sugar beet product sugar such as white sugar and soft white sugar; processing sugar such as bonbon, crystal sugar, cube sugar, refined syrup, refined granulated sugar, etc.; sugar byproducts such as orange water.
In the sugar production process using beet as raw material, the beet is pretreated, cut into vegetable shreds by a shredder, and the vegetable shreds are fed into a exuder to exude sugar juice. Removing slag, weighing, cleaning by using a bicarbonic acid method to obtain clear juice, and then carrying out the production processes of evaporation, sugar boiling, crystallization assistance, honey separation, drying and packaging.
The reason for the high vapor amount in the evaporation process is mainly as follows: 1. the juice steam is unreasonably distributed, a steam using unit of low-quality juice steam can be utilized, high-quality juice steam is used, and the total steam consumption is increased as a result; 2. the low-calorific-value heat source cannot be fully and reasonably utilized, for example, the waste heat of the condensed water is fully utilized, the juice steam of the final-effect evaporation tank and the juice steam of the crystallization tank are reasonably utilized, the self-evaporation steam of the condensed water is utilized, and the like; 3. the evaporation and heating equipment is behind, the heat transfer efficiency is low, the heat loss is large, the evaporation tank still uses the standard type, and the heater still uses the tubular type; 4. the content of calcium salt in the thin juice is high, and the evaporator and the heater are easy to scale, so that the heat transfer efficiency is reduced.
At present, most of beet sugar factories in China adopt a four-effect low-vacuum evaporation thermodynamic scheme, the total steam consumption of the scheme is generally more than 38% (for beet), only a few large sugar factories adopt a five-effect vacuum evaporation scheme, and the total steam consumption is also more than 35% (for beet). Although the traditional five-effect vacuum evaporation scheme has less steam consumption than the four-effect evaporation, the heat energy generated in the evaporation process cannot be reasonably utilized, so that the heat energy is greatly wasted.
Disclosure of Invention
The embodiment of the invention provides a five-effect evaporation system for sugar production, which aims to solve the problem that the existing five-effect evaporation system for sugar production cannot realize effective utilization of waste heat.
The embodiment of the invention provides a five-effect evaporation system for sugar production, which comprises a heater assembly, an evaporation tank assembly, a condensation water self-evaporation assembly and a syrup balance tank.
The heater assembly comprises a first-stage thin juice heater, a second-stage thin juice heater, a third-stage thin juice heater, a fourth-stage thin juice heater and a fifth-stage thin juice heater, wherein an inlet of the first-stage thin juice heater is connected with a sugar juice inlet pipe, an outlet of the first-stage thin juice heater is connected with an inlet of the second-stage thin juice heater, and the third-stage thin juice heater, the fourth-stage thin juice heater and the fifth-stage thin juice heater are sequentially connected.
The evaporation tank assembly comprises a first-effect evaporation tank, a second-effect evaporation tank, a third-effect evaporation tank, a fourth-effect evaporation tank, a fifth-effect evaporation tank and a juice pump, wherein a juice inlet pipe of the fourth-effect evaporation tank is connected with an outlet of the dilute juice secondary heater, a juice outlet pipe of the fourth-effect evaporation tank is connected with an inlet of the dilute juice tertiary heater through the juice pump, an outlet of the dilute juice fifth-stage heater is connected with a juice inlet pipe of the first-effect evaporation tank, and juice outlets of the first-effect evaporation tank, the second-effect evaporation tank, the third-effect evaporation tank and the fifth-effect evaporation tank are sequentially connected with the juice inlet pipe.
The steam inlet of the first effect evaporation tank is connected with a positive steam supply pipe, the juice steam outlet of the first effect evaporation tank is connected with the steam inlet of the second effect evaporation tank and the heat source of the thin juice five-stage heater, the juice steam outlet of the second effect evaporation tank is connected with the steam inlet of the third effect evaporation tank, the heat source of the thin juice four-stage heater, the crystallization washing tank heat source and the granulated sugar drying heat source, the juice steam outlet of the third effect evaporation tank is connected with the steam inlet of the fourth effect evaporation tank, the heat source of the thin juice three-stage heater and the heat source of the first clear juice two-stage heater, the heat source of the exudation juice two-stage heat ironing device, the heat source of the first clear juice one-stage heater, the heat source of the ash juice four-stage heater, the heat source of the exuder and the heat source of the crystallization tank, and the juice steam outlet of the fifth effect evaporation tank is connected with the ash juice two-stage heater and the condenser.
The condensation water self-evaporation assembly comprises a first-effect condensation water drum, a second-effect condensation water drum, a third-effect condensation water drum, a fourth-effect condensation water drum and a fifth-effect condensation water drum, wherein the first-effect condensation water drum, the second-effect condensation water drum, the third-effect condensation water drum and the fifth-effect condensation water drum are respectively used for storing condensation water of the first-effect evaporation tank, the second-effect evaporation tank, the third-effect evaporation tank, the fourth-effect evaporation tank and the fifth-effect evaporation tank, the first-effect condensation water drum comprises three serial water drums, condensation water discharged by the first-effect evaporation tank sequentially passes through the three serial water drums, the first-stage dilute juice heater and the third-stage ash juice heater, and finally the condensation water for a boiler of a power plant, and condensation water discharged by the second-effect evaporation tank sequentially passes through the second-effect condensation water drum, the third-effect condensation water drum, the fourth-effect condensation water drum, the fifth-effect condensation water drum, the exudation first-stage heat heater and the whole plant heater are finally stored in the hot water tank.
The syrup balance tank is used for storing syrup flowing out from the juice outlet of the fifth-effect evaporation tank.
In this embodiment, the inlet of the dilute juice primary heater in the heater assembly is connected to the juice inlet tube; the juice inlet pipe of the fourth-effect evaporation tank in the evaporation tank assembly is connected with the outlet of the second-stage dilute juice heater, the juice outlet pipe is connected with the inlet of the third dilute juice heater through a sugar juice pump, the outlet of the fifth dilute juice heater is connected with the juice inlet pipe of the first-effect evaporation tank, the condensation water self-evaporation assembly is used for storing condensation water of the first-effect evaporation tank to the fifth-effect evaporation tank, the first-effect condensation water bag comprises three water bags connected in series, and all-stage reaction waste heat in the evaporation process can be effectively utilized through the arrangement of the system, so that the energy-saving effect is achieved.
In one embodiment of the invention, the first effect evaporation tank, the second effect evaporation tank, the third effect evaporation tank, the fourth effect evaporation tank and the fifth effect evaporation tank all use falling film evaporation tanks.
In this embodiment, the use of a falling film evaporator results in a high heat transfer coefficient for the evaporator, slow fouling generation, no static pressure differential loss, and operation at lower temperatures.
In one embodiment of the invention, a primary dilute juice heater, a secondary dilute juice heater, a tertiary dilute juice heater, a quaternary dilute juice heater and a five-stage dilute juice heater all use plate heat exchangers.
In this embodiment, the use of the plate heat exchanger makes the heat transfer efficiency of each heater 2 to 4 times higher than that of the shell-and-tube heater, so that the heat transfer efficiency can be greatly improved.
The embodiment of the invention also provides a use method of the five-effect evaporation system for sugar production, which utilizes the five-effect evaporation system for sugar production of the above embodiments, and comprises the following steps:
S1, setting the temperature: setting the temperature of the positive steam and the outlet temperatures of the juice steam of the first effect evaporation tank, the second effect evaporation tank, the third effect evaporation tank, the fourth effect evaporation tank and the fifth effect evaporation tank to be 132.9 ℃, 126.7 ℃, 120.2 ℃, 113.0 ℃ and 105.0 ℃ respectively;
s2, starting all parts of the system, and introducing the syrup to be evaporated and concentrated into a syrup primary heater to enable the flowing sequence of the syrup to be as follows: the device comprises a first-stage dilute juice heater, a second-stage dilute juice heater, a fourth-effect evaporation tank, a sugar pump, a third-stage dilute juice heater, a fourth-stage dilute juice heater, a fifth-stage dilute juice heater, a first-effect evaporation tank, a second-effect evaporation tank, a third-effect evaporation tank and a fifth-effect evaporation tank;
and S3, finally, collecting the syrup obtained by the fifth-effect evaporation tank in a syrup balance tank.
By adopting the use method of the five-effect evaporation system for sugar production, which is mentioned in the embodiment, sugar juice is changed from a traditional advanced one-effect evaporation tank to an advanced four-effect evaporation tank. The feeding mode has the advantages that the supply quantity of the four-effect juice steam is ensured, and the prior steam using unit using the three-effect juice steam is changed into the four-effect juice steam. Meanwhile, because the sugar juice directly enters the five-effect tank from the three-effect tank, the evaporation capacity of the sugar juice in the five-effect tank is increased relative to the conventional feeding mode because the three-effect juice outlet temperature is higher than the five-effect boiling point, the method is favorable for improving the syrup brix, and can meet the requirement of using a large amount of five-effect low-quality juice steam, so that the total steam consumption in the sugar production evaporation process is reduced from 35% to 25.2% for vegetables, and the purpose of saving energy is achieved.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments will be briefly described below, it being understood that the following drawings only illustrate some examples of the present invention and therefore should not be considered as limiting the scope, and other related drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic diagram of the operation of a five-effect evaporation system for sugar production according to an embodiment of the present invention.
Icon: 10-a five-effect evaporation system for sugar production; a 100-heater assembly; 110-a first stage dilute juice heater; 120-a second-stage dilute juice heater; 130-a thin juice three-stage heater; 140-a thin juice four-stage heater; 150-a thin juice five-stage heater; 300-an evaporation tank assembly; 310-a first-effect evaporation tank; 320-a second-effect evaporation tank; 330-a third effect evaporation tank; 340-a fourth effect evaporation tank; 350-a fifth effect evaporation tank; 360-sugar juice pump; 500-a condensate self-evaporating assembly; 510-a first-effect condensation water bag; 511-series water bags; 520-double effect condensation water bag; 530-triple effect condensation water drum; 540-four-effect condensation water bag; 550-five-effect condensation water bag; 700-syrup balancing tank.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments. All other embodiments, based on the embodiments of the invention, which are apparent to those of ordinary skill in the art without inventive faculty, are intended to be within the scope of the invention.
Thus, the following detailed description of the embodiments of the invention, as presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, based on the embodiments of the invention, which are apparent to those of ordinary skill in the art without inventive faculty, are intended to be within the scope of the invention.
It should be noted that: like reference numerals and letters denote like items in the following figures, and thus once an item is defined in one figure, no further definition or explanation thereof is necessary in the following figures.
In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the apparatus or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, the meaning of "a plurality" is two or more, unless explicitly defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "above" or "below" a second feature may include both the first and second features being in direct contact, as well as the first and second features not being in direct contact but being in contact with each other through additional features therebetween. Moreover, a first feature being "above," "over" and "on" a second feature includes the first feature being directly above and obliquely above the second feature, or simply indicating that the first feature is higher in level than the second feature. The first feature being "under", "below" and "beneath" the second feature includes the first feature being directly under and obliquely below the second feature, or simply means that the first feature is less level than the second feature.
Examples
Referring to fig. 1, the present invention provides a five-effect evaporation system 10 for sugar production, comprising a heater assembly 100, an evaporation tank assembly 300, a condensate self-evaporation assembly 500, and a syrup balance tank 700.
Referring to fig. 1 again, the heater assembly 100 includes a first stage juice heater 110, a second stage juice heater 120, a third stage juice heater 130, a fourth stage juice heater 140, and a fifth stage juice heater 150, wherein an inlet of the first stage juice heater 110 is connected to a juice inlet pipe, that is, a juice inlet in the drawing, an outlet of the first stage juice heater 110 is connected to an inlet of the second stage juice heater 120, and it can be understood that juice first enters the first stage juice heater 110, and is then introduced into the second stage juice heater 120 for second stage heating after first stage heating. Meanwhile, the third stage heater 130 for the weak juice, the fourth stage heater 140 for the weak juice, and the fifth stage heater 150 for the weak juice are sequentially connected.
With continued reference to fig. 1, the evaporator assembly 300 includes a first effect evaporator 310, a second effect evaporator 320, a third effect evaporator 330, a fourth effect evaporator 340, a fifth effect evaporator 350 and a juice pump 360, in which, in particular, a juice inlet pipe of the fourth effect evaporator 340 is connected to an outlet of the second-stage juice heater 120, that is, juice is heated by two poles of the first-stage juice heater 110 and the second-stage juice heater 120 and then introduced into the fourth effect evaporator 340, and a juice outlet pipe of the fourth effect evaporator 340 is connected to an inlet of the third-stage juice heater 130 through the juice pump 360, when juice enters the third-stage juice heater 130, the juice can be sequentially heated by the third-stage juice heater 130, the fourth-stage juice heater 140 and the fifth-stage juice heater 150 due to the sequential connection of the third-stage juice heater 130, the fourth-stage juice heater 140 and the fifth-stage juice heater 150. The outlet of the fifth-stage heater 150 for the thin juice is connected with the juice inlet pipe of the first-effect evaporation tank 310, and the juice outlets of the first-effect evaporation tank 310, the second-effect evaporation tank 320, the third-effect evaporation tank 330 and the fifth-effect evaporation tank 350 are sequentially connected with the juice inlet pipe, that is, after being heated by the fifth-stage heater 150 for the thin juice, the sugar juice can sequentially enter the first-effect evaporation tank 310, the second-effect evaporation tank 320, the third-effect evaporation tank 330 and the fifth-effect evaporation tank 350.
Specifically, the steam inlet of the first-effect evaporation tank 310 is connected to the positive steam supply pipe, the juice steam outlet of the first-effect evaporation tank 310 is connected to the steam inlet of the second-effect evaporation tank 320 and the heat source of the fifth-stage heater 150 for thin juice, and it can be understood that the juice steam of the first-effect evaporation tank 310 can be used as the steam source of the second-effect evaporation tank 320 and the heat source of the fifth-stage heater 150 for thin juice; the juice vapor outlet of the second-effect evaporation tank 320 is connected with the vapor inlet of the third-effect evaporation tank 330, the heat source of the thin juice four-stage heater 140, the crystallization washing tank heat source and the granulated sugar drying heat source, and similarly, the juice vapor of the second-effect evaporation tank 320 can be used as the vapor source of the third-effect evaporation tank 330, the heat source of the thin juice four-stage heater 140, the crystallization washing tank heat source and the granulated sugar drying heat source; the juice vapor outlet of the third effect evaporation tank 330 is connected with the vapor inlet of the fourth effect evaporation tank 340, the heat source of the third-stage thin juice heater 130 and the heat source of the second-stage clear juice heater, that is, the juice vapor of the third effect evaporation tank 330 can be used as the vapor source of the fourth effect evaporation tank 340, the heat source of the third-stage thin juice heater 130 and the heat source of the second-stage clear juice heater; the juice vapor outlet of the fourth effect evaporation tank 340 is connected with the vapor inlet of the fifth effect evaporation tank 350, the heat source of the second-stage thin juice heater 120, the heat source of the second-stage exuded juice heater, the heat source of the first-stage clear juice heater, the heat source of the fourth-stage ash juice heater, the heat source of the exuder and the heat source of the crystallization tank, and likewise, the juice vapor of the fourth effect evaporation tank 340 can be used for the vapor source of the fifth effect evaporation tank 350, the heat source of the second-stage thin juice heater 120, the heat source of the second-stage exuded juice heater, the heat source of the first-stage clear juice heater, the heat source of the fourth-stage ash juice heater, the heat source of the exuder and the heat source of the crystallization tank; the juice vapor outlet of the fifth effect evaporation tank 350 is connected with the ash juice secondary heater heat source and the condenser, that is, the juice vapor of the fifth effect evaporation tank 350 can be supplied to the ash juice secondary heater heat source and the condenser for use.
Referring to fig. 1, the condensation self-evaporation assembly 500 includes a first-effect condensation water drum 510, a second-effect condensation water drum 520, a third-effect condensation water drum 530, a fourth-effect condensation water drum 540 and a fifth-effect condensation water drum 550, wherein the first-effect condensation water drum 510, the second-effect condensation water drum 520, the third-effect condensation water drum 530, the fourth-effect condensation water drum 540 and the fifth-effect condensation water drum 550 are respectively used for storing condensation water of the first-effect evaporation tank 310, the second-effect evaporation tank 320, the third-effect evaporation tank 330, the fourth-effect evaporation tank 340 and the fifth-effect evaporation tank 350. Meanwhile, the first-effect condensation water drum 510 comprises three serial water drums 511, so that condensation water discharged from the first-effect evaporation tank 310 can sequentially pass through the three serial water drums 511 and release heat step by step, then pass through the dilute juice primary heater 110 and the ash juice tertiary heater, when the temperature is reduced to about 80 ℃, and finally be introduced into a power plant as boiler water.
Specifically, the self-evaporation steam of the first series water drum 511 can be introduced into the first-effect evaporation tank 310 again to be used as evaporation steam, the self-evaporation steam of the second series water drum 511 can be introduced into the second-effect evaporation tank 320 to be used as evaporation steam, and the self-evaporation steam of the third series water drum 511 can be introduced into the third-effect evaporation tank 330 to be used as evaporation steam.
The condensed water discharged from the second effect evaporation tank 320 sequentially passes through the second effect condensation water drum 520, the third effect condensation water drum 530, the fourth effect condensation water drum 540, the fifth effect condensation water drum 550, the exudation juice primary blancher and the whole plant heater, and finally is stored in the hot water tank, it can be understood that the condensed water of the second effect evaporation tank 320, the third effect evaporation tank 330, the fourth effect evaporation tank 340 and the fifth effect evaporation tank 350 can be used for the exudation juice primary blancher heat source, and then is introduced into the whole plant heater to be used as a heating heat source, and finally when the water temperature is reduced to about 60 ℃, the condensed water is stored in the hot water tank to be used for supplying daily hot water.
Meanwhile, the self-evaporation steam of the two-effect condensation water drum 520, the three-effect condensation water drum 530, the four-effect condensation water drum 540 and the five-effect condensation water drum 550 can be returned to the second-effect evaporation tank 320, the third-effect evaporation tank 330, the fourth-effect evaporation tank 340 and the fifth-effect evaporation tank 350 as evaporation steam, respectively.
Referring to fig. 1, the syrup balance tank 700 is connected to the juice outlet of the fifth effect evaporation tank 350, and can be used for storing syrup flowing out of the juice outlet after evaporation treatment of the fifth effect evaporation tank 350, and the obtained syrup can be subjected to a next sugar boiling operation.
In a specific embodiment, the first effect evaporation tank 310, the second effect evaporation tank 320, the third effect evaporation tank 330, the fourth effect evaporation tank 340 and the fifth effect evaporation tank 350 all use falling film evaporation tanks, and the use of falling film evaporation tanks can make the heat transfer coefficient of the evaporation tanks high, the scale formation slow, no static pressure temperature difference loss exists, and can operate at a lower temperature.
In another specific embodiment, the first stage dilute juice heater 110, the second stage dilute juice heater 120, the third stage dilute juice heater 130, the fourth stage dilute juice heater 140 and the fifth stage dilute juice heater 150 all use plate heat exchangers, so that the heat transfer efficiency of each heater is 2-4 times higher than that of the shell-and-tube heater, and therefore, the heat transfer efficiency can be greatly improved.
The invention also provides a method for using the five-effect evaporation system 10 for sugar production, in particular to the five-effect evaporation system for sugar production, which can utilize the above embodiments, and the following steps:
S1, setting the temperature: setting the temperature of the positive steam and the outlet temperatures of the juice steam of the first effect evaporation tank 310, the second effect evaporation tank 320, the third effect evaporation tank 330, the fourth effect evaporation tank 340 and the fifth effect evaporation tank 350 to be 132.9 ℃, 126.7 ℃, 120.2 ℃, 113.0 ℃ and 105.0 ℃ respectively;
S2, starting all components of the system, and introducing the syrup to be evaporated and concentrated into the first-stage dilute juice heater 110, so that the flowing sequence of the syrup is as follows: a first-stage dilute juice heater 110, a second-stage dilute juice heater 120, a fourth-effect evaporation tank 340, a sugar pump 360, a third-stage dilute juice heater 130, a fourth-stage dilute juice heater 140, a fifth-stage dilute juice heater 150, a first-effect evaporation tank 310, a second-effect evaporation tank 320, a third-effect evaporation tank 330 and a fifth-effect evaporation tank 350;
And S3, finally, collecting the syrup obtained by the fifth-effect evaporation tank 350 in a syrup balance tank 700.
In a specific embodiment, according to the existing equipment and the temperature setting, the thermodynamic consumption of each stage is different in the actual evaporation process, and specific data are as follows.
The following is a five-effect evaporation system thermodynamic distribution profile for sugar manufacturing as referred to in the examples of the present invention:
Based on the data in the thermodynamic distribution profile, let the juice vapor amount be E, it is known that the juice vapor amount e1=0.88 (t) of the first effective evaporation tank 310; juice vapor quantity e2=2.83 (t) of the second-effect evaporation tank 320; the juice vapor amount e3=5.56 (t) of the third-effect evaporation tank 330; juice vapor quantity e4=16.42 (t) of the fourth-effect evaporation tank 340; the juice vapor quantity e5=2.51 (t) of the fifth effect evaporation tank 350.
The material balance can be known as follows:
Total evaporation water m=evaporation syrup amount-evaporation solid loss = 114.49-24.66-0.18= 89.65 (t);
Total consumption m' =5e 5+4E4+3E3+2E2+E1 = 101.45 (t) of juice and steam at each stage;
because the total consumption of the juice steam exceeds the allowable total evaporation water quantity, the steam extraction scheme needs to be readjusted, and the extraction quantity of the four-effect juice steam can be reduced by assuming that the positive steam is used for one sand crystallization, and the supplementing quantity is X: e 4 =16.42-X
Namely: m' =5×2.51+4× (16.42-X) +3×5.56+2×2.83+0.88
＝101.45-4X
Because the process requirement needs to meet m' =m, that is 101.45-4x=89.65, x=2.95
Then: after adjustment, the amount of the four-effect juice vapor is 16.42-2.95=13.47 (t)
Thus, the fifth effect evaporation tank 350 evaporates the water amount m5=2.51 (t);
The fourth-effect evaporation tank 340 evaporates the water amount m4=m5+e4=2.51+13.47=15.98 (t);
the third-effect evaporation tank 330 evaporates the water amount m3=m4+e3=15.98+5.56= 21.54 (t);
the second-effect evaporation tank 320 evaporates the water amount m2=m3+e2=21.54+2.83=24.37 (t);
The first-effect evaporation tank 310 evaporates the water amount m1=m2+e1=24.37+0.88=25.25 (t).
Therefore, the evaporation section consumes positive steam d=m1+x=25.25+2.95=28.2 (t)
And through actual measurement and calculation, the condensation water of each stage can be self-evaporated to save 2.0t, the sugar juice can be self-evaporated to save 2.2t, and the theoretical positive steam consumption is 28.2-2.0-2.2=24 (t).
Therefore, the actual steam consumption is: theoretical air loss x heat loss = 24 x 1.05 = 25.2 (t)
According to the scheme of the invention and the empirical data of heat transfer of each heat equipment in actual production, the scheme can be calculated to reduce the total steam consumption of the sugar-making evaporation process from 35% to 25.2% for vegetables (empirical data), namely 25.2 tons for beet per hundred tons, so that the consumption of heat is greatly reduced, and the energy-saving effect is achieved.
The above is only a preferred embodiment of the present invention, and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (3)
1. The application method of the five-effect evaporation system for sugar production is characterized by adopting the five-effect evaporation system, wherein the five-effect evaporation system comprises
The device comprises a heater assembly, a juice inlet pipe and a juice outlet pipe, wherein the heater assembly comprises a first-stage juice heater, a second-stage juice heater, a third-stage juice heater, a fourth-stage juice heater and a fifth-stage juice heater, the inlet of the first-stage juice heater is connected with the juice inlet pipe, the outlet of the first-stage juice heater is connected with the inlet of the second-stage juice heater, and the third-stage juice heater, the fourth-stage juice heater and the fifth-stage juice heater are sequentially connected;
The evaporation tank assembly comprises a first-effect evaporation tank, a second-effect evaporation tank, a third-effect evaporation tank, a fourth-effect evaporation tank, a fifth-effect evaporation tank and a juice pump, wherein a juice inlet pipe of the fourth-effect evaporation tank is connected with an outlet of the dilute juice secondary heater, a juice outlet pipe of the fourth-effect evaporation tank is connected with an inlet of the dilute juice tertiary heater through the juice pump, an outlet of the dilute juice fifth-stage heater is connected with a juice inlet pipe of the first-effect evaporation tank, juice outlets of the first-effect evaporation tank, the second-effect evaporation tank, the third-effect evaporation tank and the fifth-effect evaporation tank are sequentially connected with the juice inlet pipe, a steam inlet of the first-effect evaporation tank is connected with a positive steam supply pipe, a juice steam outlet of the first-effect evaporation tank is connected with a steam inlet of the second-effect evaporation tank and a heat source of the dilute juice fifth-stage heater, the juice steam outlet of the second-effect evaporation tank is connected with the steam inlet of the third-effect evaporation tank, the heat source of the dilute juice four-stage heater, the crystallization washing tank heat source and the granulated sugar drying heat source, the juice steam outlet of the third-effect evaporation tank is connected with the steam inlet of the fourth-effect evaporation tank, the heat source of the dilute juice three-stage heater and the heat source of a clear juice two-stage heater, the juice steam outlet of the fourth-effect evaporation tank is connected with the steam inlet of the fifth-effect evaporation tank, the heat source of the dilute juice two-stage heater, the heat source of a exuded juice two-stage heater, the heat source of a clear juice one-stage heater, the heat source of an ash juice four-stage heater, the heat source of the exuder and the heat source of the crystallization tank, and the juice steam outlet of the fifth-effect evaporation tank is connected with the heat source of the ash juice two-stage heater and the condenser;
The condensation water self-evaporation assembly comprises a first-effect condensation water drum, a second-effect condensation water drum, a third-effect condensation water drum, a fourth-effect condensation water drum and a fifth-effect condensation water drum, wherein the first-effect condensation water drum, the second-effect condensation water drum and the third-effect condensation water drum are respectively used for storing condensation water of the first-effect evaporation drum, the second-effect evaporation drum, the third-effect evaporation drum, the fourth-effect evaporation drum and the fifth-effect evaporation drum, the first-effect condensation water drum comprises three serial connection water drums, the condensation water discharged by the first-effect evaporation drum can sequentially pass through three serial connection water drums, a dilute juice primary heater and an ash juice tertiary heater, and finally the condensation water for a power plant boiler, self-evaporation steam of the first serial connection water drum can be introduced into the first-effect evaporation drum again to serve as evaporation steam, self-evaporation of the second-effect evaporation drum can be introduced into the second-effect evaporation drum, the second-effect evaporation drum can be introduced into the second-effect evaporation drum, the third-effect evaporation drum, the fifth-effect evaporation drum can be introduced into the third-effect evaporation drum, the third-effect evaporation drum and the fifth-effect evaporation drum can be introduced into the third-effect evaporation drum, the third-effect evaporation drum and the fifth-effect evaporation drum can be sequentially used as evaporation water drum, the condensation water drum, the third-effect evaporation water drum can be sequentially discharged by the first-effect evaporation drum, the third-effect evaporation drum can be introduced into the third-effect evaporation drum, the third-effect evaporation drum can be condensed by the third effect evaporation drum, and the condensation water can be subjected to the condensation water can be used by the evaporation water can be sequentially and the evaporation water can be used as the evaporation water through the evaporation drum;
The syrup balance tank is used for storing syrup flowing out from the juice outlet of the fifth-effect evaporation tank;
The method comprises the following steps:
S1, setting the temperature: setting the temperature of the positive steam, the first effect evaporation tank, the second effect evaporation tank, the third effect evaporation tank, the fourth effect evaporation tank and the fifth effect evaporation tank to be 132.9 ℃, 126.7 ℃, 120.2 ℃, 113.0 ℃, 105.0 ℃ and 93.0 ℃ respectively;
S2, starting all parts of the system, and introducing the syrup to be evaporated and concentrated into the first-stage dilute juice heater, so that the flowing sequence of the syrup is as follows: the first-stage dilute juice heater, the second-stage dilute juice heater, the fourth-effect evaporation tank, the sugar juice pump, the third-stage dilute juice heater, the fourth-stage dilute juice heater, the fifth-stage dilute juice heater, the first-effect evaporation tank, the second-effect evaporation tank, the third-effect evaporation tank and the fifth-effect evaporation tank;
and S3, finally, collecting the syrup obtained by the fifth-effect evaporation tank in the syrup balance tank.
2. The method of claim 1, wherein the first, second, third, fourth and fifth effect evaporators each use a falling film evaporator.
3. The method of claim 1, wherein the first-stage, second-stage, third-stage, fourth-stage, and fifth-stage dilute juice heaters are plate heat exchangers.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210776401.0A CN115245687B (en) | 2022-06-30 | 2022-06-30 | Five-effect evaporation system for sugar production and use method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210776401.0A CN115245687B (en) | 2022-06-30 | 2022-06-30 | Five-effect evaporation system for sugar production and use method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115245687A CN115245687A (en) | 2022-10-28 |
| CN115245687B true CN115245687B (en) | 2024-05-14 |
Family
ID=83700237
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210776401.0A Active CN115245687B (en) | 2022-06-30 | 2022-06-30 | Five-effect evaporation system for sugar production and use method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115245687B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117732095B (en) * | 2024-02-21 | 2024-05-03 | 珙县华洁危险废物治理有限责任公司成都分公司 | Method for treating sodium azide by adopting triple-effect evaporation system |
Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2065191U (en) * | 1990-01-25 | 1990-11-07 | 常熟市医疗制药机械厂 | Efficient high-purity distilled water machine |
| CN103060480A (en) * | 2011-10-18 | 2013-04-24 | 中国轻工业南宁设计工程有限公司 | Plate-type evaporator and application thereof to evaporation system in refined sugar factory |
| CN106512458A (en) * | 2016-12-09 | 2017-03-22 | 南宁市黑晶信息技术有限公司 | Distillation system for sugar industry factory |
| CN106540471A (en) * | 2016-10-28 | 2017-03-29 | 广西大学 | A kind of employing triple effect evaporation technique concentrates the method and device of biogas slurry |
| WO2017124215A1 (en) * | 2016-01-18 | 2017-07-27 | 江门市佰川环境科技有限公司 | Double-effect cross-flow mvr evaporation concentration system |
| CN207286714U (en) * | 2017-07-21 | 2018-05-01 | 江苏瑞达环保科技有限公司 | A kind of TVR evaporation concentration devices of NMMO ionic liquids |
| CN212651369U (en) * | 2020-02-28 | 2021-03-05 | 西昌市正中食品有限公司 | Multiple-effect enrichment facility is used in bitter buckwheat processing |
| CN113307433A (en) * | 2021-04-30 | 2021-08-27 | 江苏瑞升华能源科技有限公司 | Four-effect cross-flow pharmaceutical wastewater evaporative crystallization system with external heat exchanger |
| CN216092275U (en) * | 2021-10-11 | 2022-03-22 | 呼伦贝尔晟通糖业科技有限公司 | A five-effect evaporation concentration system for sugaring production |
-
2022
- 2022-06-30 CN CN202210776401.0A patent/CN115245687B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2065191U (en) * | 1990-01-25 | 1990-11-07 | 常熟市医疗制药机械厂 | Efficient high-purity distilled water machine |
| CN103060480A (en) * | 2011-10-18 | 2013-04-24 | 中国轻工业南宁设计工程有限公司 | Plate-type evaporator and application thereof to evaporation system in refined sugar factory |
| WO2017124215A1 (en) * | 2016-01-18 | 2017-07-27 | 江门市佰川环境科技有限公司 | Double-effect cross-flow mvr evaporation concentration system |
| CN106540471A (en) * | 2016-10-28 | 2017-03-29 | 广西大学 | A kind of employing triple effect evaporation technique concentrates the method and device of biogas slurry |
| CN106512458A (en) * | 2016-12-09 | 2017-03-22 | 南宁市黑晶信息技术有限公司 | Distillation system for sugar industry factory |
| CN207286714U (en) * | 2017-07-21 | 2018-05-01 | 江苏瑞达环保科技有限公司 | A kind of TVR evaporation concentration devices of NMMO ionic liquids |
| CN212651369U (en) * | 2020-02-28 | 2021-03-05 | 西昌市正中食品有限公司 | Multiple-effect enrichment facility is used in bitter buckwheat processing |
| CN113307433A (en) * | 2021-04-30 | 2021-08-27 | 江苏瑞升华能源科技有限公司 | Four-effect cross-flow pharmaceutical wastewater evaporative crystallization system with external heat exchanger |
| CN216092275U (en) * | 2021-10-11 | 2022-03-22 | 呼伦贝尔晟通糖业科技有限公司 | A five-effect evaporation concentration system for sugaring production |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115245687A (en) | 2022-10-28 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN115245687B (en) | Five-effect evaporation system for sugar production and use method | |
| CN105056565B (en) | Device and method for evaporation and crystallization of sodium gluconate solution | |
| CN104628208B (en) | A kind of method of contains sodium sulfate high-salinity wastewater zero-emission and recycling | |
| CN110282676B (en) | Hydrazine hydrate wastewater evaporation crystallization equipment and evaporation crystallization process thereof | |
| CN104692415A (en) | Evaporative crystallization method of ammonium chloride in potassium nitrate production | |
| CN108862325A (en) | The recovery and treatment method and equipment of sodium chloride-containing and potassium chloride high-salt wastewater | |
| CN103508877A (en) | Energy-saving method and device for four-effect concentration and crystallization of itaconic acid | |
| CN106629938A (en) | Four-effect vacuum energy-saving evaporative crystallization system for high-concentration saline wastewater | |
| CN101274784B (en) | Steam-water four-stage separating five-effect water distillator | |
| CN108651932A (en) | A kind of honey process units and its application method | |
| CN205662335U (en) | Two -stage forced circulation evaporation crystal system among MVR | |
| US4441958A (en) | Forced-circulation evaporator plant | |
| CN218130003U (en) | Evaporation crystallization device for producing borax from salt lake lithium extraction discharge liquid | |
| CN114949893B (en) | Evaporation crystallization process and device for producing lithium chloride from salt lake brine | |
| CN217297316U (en) | Industrial potassium chloride purification system | |
| CN213221027U (en) | Ammonium magnesium sulfate evaporation crystallization equipment | |
| CN112755560A (en) | Device for improving energy utilization rate by liquid glucose sterilization and use method | |
| CN213466794U (en) | Amino acid concentration system | |
| CN102336419A (en) | Equipment special for producing bulk wet salt by using sodium sulfate type brine | |
| CN103467401B (en) | Production method and device for ametryn | |
| CN112657219A (en) | Evaporation concentration system and evaporation concentration method | |
| CN210813967U (en) | Crystallization evaporation system | |
| CN220478170U (en) | Erythritol cold and hot co-crystallization system | |
| CN214232802U (en) | Evaporation concentration system | |
| CN100348285C (en) | Energy-saving three-stage vacuum evaporation concentrate crystallization method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |