CN103007561A - Concentration production technology for glucose liquid - Google Patents
Concentration production technology for glucose liquid Download PDFInfo
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- CN103007561A CN103007561A CN2012105473695A CN201210547369A CN103007561A CN 103007561 A CN103007561 A CN 103007561A CN 2012105473695 A CN2012105473695 A CN 2012105473695A CN 201210547369 A CN201210547369 A CN 201210547369A CN 103007561 A CN103007561 A CN 103007561A
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- concentration
- glucose feed
- effect evaporator
- glucose
- mvr
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- 238000005516 engineering process Methods 0.000 title claims abstract description 22
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 18
- GZCGUPFRVQAUEE-SLPGGIOYSA-N aldehydo-D-glucose Chemical compound OC[C@@H](O)[C@@H](O)[C@H](O)[C@@H](O)C=O GZCGUPFRVQAUEE-SLPGGIOYSA-N 0.000 title abstract 4
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 claims abstract description 48
- 239000008103 glucose Substances 0.000 claims abstract description 45
- 238000001704 evaporation Methods 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims abstract description 36
- 230000008020 evaporation Effects 0.000 claims abstract description 33
- 238000000034 method Methods 0.000 claims abstract description 18
- 239000002912 waste gas Substances 0.000 claims abstract description 8
- 230000006835 compression Effects 0.000 claims abstract description 6
- 238000007906 compression Methods 0.000 claims abstract description 6
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- 230000000694 effects Effects 0.000 claims description 32
- 239000000463 material Substances 0.000 claims description 13
- 238000012545 processing Methods 0.000 claims description 6
- 238000007701 flash-distillation Methods 0.000 claims description 5
- 235000014666 liquid concentrate Nutrition 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- 238000004134 energy conservation Methods 0.000 abstract description 5
- 230000007613 environmental effect Effects 0.000 abstract description 5
- WHMDKBIGKVEYHS-IYEMJOQQSA-L Zinc gluconate Chemical compound [Zn+2].OC[C@@H](O)[C@@H](O)[C@H](O)[C@@H](O)C([O-])=O.OC[C@@H](O)[C@@H](O)[C@H](O)[C@@H](O)C([O-])=O WHMDKBIGKVEYHS-IYEMJOQQSA-L 0.000 abstract description 2
- 229960000306 zinc gluconate Drugs 0.000 abstract description 2
- 235000011478 zinc gluconate Nutrition 0.000 abstract description 2
- 239000011670 zinc gluconate Substances 0.000 abstract description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 239000011552 falling film Substances 0.000 description 2
- 230000009229 glucose formation Effects 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000008121 dextrose Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 150000002303 glucose derivatives Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007634 remodeling Methods 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
A concentration production technology for glucose liquid comprises the following steps: heating glucose liquid in a plate heat exchanger; evaporating the heated liquid in an MVR (mechanical vapor recompression) evaporating unit; and evaporating the liquid in a triple-effect evaporator to obtain 70-75 % of liquid. Heat required by the triple-effect evaporator used in the technology is compression heat of flash evaporation waste gas. According to the technology, one-step glucose liquid concentration treatment in the prior art is changed into staged evaporation treatment; the MVR evaporating unit and the triple-effect evaporator are respectively used in two stages of treatment; and the heat source of the triple-effect evaporator is flash evaporation waste gas produced in other procedures, so as to realize zero consumption of live steam in the stage. Through implementation of the technology, the quality of crystallized glucose products is improved, the technology has the advantages of high efficiency, low consumption, energy conservation and environmental friendliness, and a zinc gluconate product produced through the technology has high concentration and meets the current national requirements on energy conservation and environmental protection of enterprises.
Description
Technical field
The present invention relates to the glucose production technical field, especially relate to a kind of for realizing the production technology that the glucose feed liquid is concentrated by evaporimeter.
Background technology
In engineering of producing crystalline dextrose, need to be that to be evaporated to concentration be to carry out crystallization with evaporimeter again behind the 70%-75% for the liquid glucose of 30-35% with concentration, in production process in the past, generally use general evaporimeter it is carried out evaporation and concentration, one ton of water of the every evaporation of this kind technology need consume the steam of 0.25-0.35 ton, and the waste gas that produces directly is cooled to the solidifying water of vapour, can not reasonably utilize its waste heat, when having increased single ton of sugared production cost, also cause resource waste extremely, do not met very much current national to the requirement of industry energy conservation environmental protection.
Summary of the invention
The object of the invention is to overcome the defective that exists in the prior art, provide a kind of glucose feed liquid to concentrate production technology, this production technology by evaporation mode stage by stage with the thermal balance of the whole production line of rational allocation, realized that zero gives birth to steam consumption, reached energy-saving and cost-reducing purpose, the technical scheme that adopts is: a kind of glucose feed liquid concentrates production technology, and it is characterized in that: described production technology may further comprise the steps:
1) when reaching 50%, the liquid level of glucose feed liquid in the storage tank before the evaporation opens feed pump, by feed pump the glucose feed pump being delivered to plate type heat exchanger heats, the glucose feed pump is delivered in the material balance tank after the heating, and the plate type heat exchanger drop temperature is 75 ℃;
2) open feed pump when above when material in the material balance tank reaches 30%, glucose feed pump in the material balance tank is delivered to the vaporization chamber of MVR evaporation unit and started simultaneously MVR evaporation unit carry out evaporation process;
3) the glucose feed liquid after MVR evaporation unit is processed enters into MVR and processes rear storage tank, open feed pump when storage tank reaches 50% after MVR processes, the glucose feed liquid is pumped into triple effect evaporator, open simultaneously the feed back valve, close discharge valve, make the rear glucose feed liquid of processing at first be back to MVR and process rear storage tank;
4) observe the growth of triple effect evaporator DC density, slowly adjust triple effect evaporator FC output concentration, after exporting concentration and reaching requirement concentration, discharge valve is opened simultaneously closing volume valve, make the glucose feed liquid after the processing enter next workshop section;
5) be in stable state and output concentration when having reached requirement concentration when the glucose feed liquid, each triple effect evaporation circulating pump FC series connection of triple effect evaporator PC, it is auto state that triple effect evaporator DC is set.
Technical scheme of the present invention also has: the flash distillation waste gas compression that the liquefaction operation produces in will producing heats up, and regenerates thermal source, and this thermal source is passed in the triple effect evaporator.
Technical scheme of the present invention also has: the concentration of glucose feed liquid is 30-35% in the front storage tank of the described evaporation of step 1), and the glucose feed concentration after the described MVR evaporation of step 3) unit is processed is 55-60%, and the concentration of output described in the step 5) is 70-75%.
Beneficial effect of the present invention is: this process modification the concentrated production technology of grape sugar feed liquid, one step completed glucose feed liquid concentration in the prior art has been become stage by stage evaporation treatment process, MVR evaporation unit and triple effect evaporator have been used respectively in two phase process, and the thermal source that uses in triple effect evaporator derives from the flash distillation waste gas that produces in other operation, thereby has realized and should the stage zero give birth to steam consumption.The enforcement of this technique has not only improved the quality of crystallization glucose product, and has the advantage of efficient, low consumption, energy-conservation and environmental protection, and the zinc gluconate product design by this explained hereafter is high and meet the current requirement to the industry energy conservation environmental protection of country.
Description of drawings
Accompanying drawing 1 is process chart of the present invention.
The specific embodiment
Below in conjunction with accompanying drawing, the present invention is specifically described.The invention discloses the concentrated production technology of a kind of glucose feed liquid, this production technology may further comprise the steps:
1) when reaching 50%, the liquid level of glucose feed liquid in the storage tank before the evaporation opens feed pump, the concentration of glucose feed liquid is 30-35% in the front storage tank of evaporation, by feed pump the glucose feed pump being delivered to plate type heat exchanger heats, the glucose feed pump is delivered in the material balance tank after the heating, and the plate type heat exchanger drop temperature is 75 ℃;
2) when reaching 30%, material in the material balance tank opens feed pump when above, glucose feed pump in the material balance tank delivered to the vaporization chamber of MVR evaporation unit and start simultaneously MVR evaporation unit carry out evaporation process, the glucose feed concentration after MVR evaporation unit is processed is 55-60%;
3) the glucose feed liquid after MVR evaporation unit is processed enters into MVR and processes rear storage tank, open feed pump when storage tank reaches 50% after MVR processes, the glucose feed liquid is pumped into triple effect evaporator, open simultaneously the feed back valve, close discharge valve, make the rear glucose feed liquid of processing at first be back to MVR and process rear storage tank;
4) growth of observation triple effect evaporator DC density, slowly adjust triple effect evaporator FC output concentration, after exporting concentration and reaching requirement concentration, discharge valve is opened simultaneously closing volume valve, make the glucose feed liquid after the processing enter next workshop section, this glucose feed liquid output concentration is 70-75%;
5) be in stable state and output concentration when having reached requirement concentration when the glucose feed liquid, each triple effect evaporation circulating pump FC series connection of triple effect evaporator PC, it is auto state that triple effect evaporator DC is set.
Wherein, the MVR evaporimeter is different from common single-action falling liquid film or multiple-effect falling film evaporimeter, MVR is the monomer evaporimeter, integrate the multiple-effect falling film evaporimeter, take the segmented evaporation according to required product concentration difference, when to be product can not reach desired concn after for the first time through the effect body, product vavuum pump by effect body bottom after leaving the effect body was extracted into effect body top again by the effect body with product by effect external body pipeline, then by this repeatedly by the effect body to reach desired concn.
In the MVR evaporator system, under certain pressure, utilize fixed gas (during the beginning preheating) and water vapour (during start vaporizer) in the vapour compression machine heat exchanger to compress, thereby produce steam, discharge simultaneously heat energy.The indirect steam that produces is after mechanical type heat energy compressor (being similar to air blast) effect, and in evaporator system the heat of the indirect steam that produces of recycling repeatedly, make 5～20 ℃ of intrasystem temperature increase, heat can continuous several times be utilized, live steam only is used for the supplemental heat loss and replenishes the input and output material heat content, significantly lowers evaporimeter to the consumption of external live steam.Improve the thermal efficiency, reduced energy consumption, avoided using external steam (main operating expenses of this steam recompression formula energy-saving evaporator only is the electric energy of drive compression machine).Because electric energy is clean energy resource, therefore, the MVR evaporimeter has really reached the discharging of " zero " pollution, has not namely had the requirement of CO2 emission fully.
Required thermal source comes from the flash distillation waste gas that the liquefaction operation produces in the glucose production in the triple effect evaporator, will change the compression of flash distillation waste gas and heat up, and regenerates thermal source, and this thermal source is passed in the triple effect evaporator.
Certainly, above-mentioned explanation is not limitation of the present invention, and the present invention also is not limited only to above-mentioned giving an example, and the variation that those skilled in the art make in essential scope of the present invention, remodeling, interpolation or replacement also belong to protection scope of the present invention.
Claims (3)
1. a glucose feed liquid concentrates production technology, and it is characterized in that: described production technology may further comprise the steps:
1) when reaching 50%, the liquid level of glucose feed liquid in the storage tank before the evaporation opens feed pump, by feed pump the glucose feed pump being delivered to plate type heat exchanger heats, the glucose feed pump is delivered in the material balance tank after the heating, and the plate type heat exchanger drop temperature is 75 ℃;
2) open feed pump when above when material in the material balance tank reaches 30%, glucose feed pump in the material balance tank is delivered to the vaporization chamber of MVR evaporation unit and started simultaneously MVR evaporation unit carry out evaporation process;
3) the glucose feed liquid after MVR evaporation unit is processed enters into MVR and processes rear storage tank, open feed pump when storage tank reaches 50% after MVR processes, the glucose feed liquid is pumped into triple effect evaporator, open simultaneously the feed back valve, close discharge valve, make the rear glucose feed liquid of processing at first be back to MVR and process rear storage tank;
4) observe the growth of triple effect evaporator DC density, slowly adjust triple effect evaporator FC output concentration, after exporting concentration and reaching requirement concentration, discharge valve is opened simultaneously closing volume valve, make the glucose feed liquid after the processing enter next workshop section;
5) be in stable state and output concentration when having reached requirement concentration when the glucose feed liquid, each triple effect evaporation circulating pump FC series connection of triple effect evaporator PC, it is auto state that triple effect evaporator DC is set.
2. according to the concentrated production technology of glucose feed liquid claimed in claim 1, it is characterized in that: the flash distillation waste gas compression that the liquefaction operation produces in will producing heats up, and regenerates thermal source, and this thermal source is passed in the triple effect evaporator.
3. according to claim 1 or the concentrated production technology of 2 described glucose feed liquids, it is characterized in that: the concentration of glucose feed liquid is 30-35% in the front storage tank of the described evaporation of step 1), glucose feed concentration after the described MVR evaporation of step 3) unit is processed is 55-60%, and the concentration of output described in the step 5) is 70-75%.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210547369.5A CN103007561B (en) | 2012-12-17 | 2012-12-17 | Concentration production technology for glucose liquid |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210547369.5A CN103007561B (en) | 2012-12-17 | 2012-12-17 | Concentration production technology for glucose liquid |
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| CN103007561A true CN103007561A (en) | 2013-04-03 |
| CN103007561B CN103007561B (en) | 2014-09-17 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103537104A (en) * | 2013-10-25 | 2014-01-29 | 昆山市盛兴设备安装有限公司 | Fructose-glucose syrup evaporating system |
| CN109022625A (en) * | 2018-09-18 | 2018-12-18 | 上海立足生物科技有限公司 | A method of producing the D-Psicose of concentration |
| CN112843761A (en) * | 2021-03-10 | 2021-05-28 | 郑州博大浓缩干燥设备有限公司 | Lees protein production fodder is with lees filter liquor evaporation concentration system |
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| DE10358015A1 (en) * | 2003-12-11 | 2005-07-14 | Gea Wiegand Gmbh | evaporation |
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2012
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|---|---|---|---|---|
| CN103537104A (en) * | 2013-10-25 | 2014-01-29 | 昆山市盛兴设备安装有限公司 | Fructose-glucose syrup evaporating system |
| CN109022625A (en) * | 2018-09-18 | 2018-12-18 | 上海立足生物科技有限公司 | A method of producing the D-Psicose of concentration |
| CN112843761A (en) * | 2021-03-10 | 2021-05-28 | 郑州博大浓缩干燥设备有限公司 | Lees protein production fodder is with lees filter liquor evaporation concentration system |
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| CN103007561B (en) | 2014-09-17 |
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Inventor after: Wang Dai Inventor after: Zhang Xiaojie Inventor after: Yang Rongyu Inventor after: Wang Yi Inventor after: Wang Yan Inventor after: Wang Qian Inventor after: Xie Dengyu Inventor after: Han Cuiping Inventor after: Sun Ying Inventor after: Sun Chao Inventor before: Wang Dai Inventor before: Zhang Jian Inventor before: Li Wei Inventor before: Wang Yan Inventor before: Tang Haijing Inventor before: Zhang Quangang Inventor before: Yang Ruyu Inventor before: Ma Sen Inventor before: Wang Qian |
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Denomination of invention: A concentration production process of grape sugar liquid Effective date of registration: 20211224 Granted publication date: 20140917 Pledgee: Agricultural Development Bank of China Zouping sub branch Pledgor: XIWANG PHARMACEUTICAL Co.,Ltd. Registration number: Y2021980016207 |
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Date of cancellation: 20221025 Granted publication date: 20140917 Pledgee: Agricultural Development Bank of China Zouping sub branch Pledgor: XIWANG PHARMACEUTICAL Co.,Ltd. Registration number: Y2021980016207 |
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Denomination of invention: A process for concentrating glucose feed solution Effective date of registration: 20221027 Granted publication date: 20140917 Pledgee: Agricultural Development Bank of China Zouping sub branch Pledgor: XIWANG PHARMACEUTICAL Co.,Ltd. Registration number: Y2022980019930 |