Recycling device for stevioside mother liquor

Abstract

The utility model discloses a recycling device of stevioside mother liquor, and relates to the field of stevioside production, an outlet of a crude product powder tank is communicated with a dissolving tank, an outlet of the dissolving tank is communicated with a first crystallizing tank, an outlet of the first crystallizing tank is communicated with a first separator, and the first separator is communicated with a first crystal tank and a first crystallizing mother liquor tank; an outlet of the first crystallization mother liquor tank is communicated with a second crystallization tank through a pipeline, an inlet of the second crystallization tank is communicated to the crude product powder tank, an outlet of the second crystallization tank is communicated with a second separator through a pipeline, a solid phase outlet of the second separator is communicated with a second dryer, and an outlet of the second dryer is communicated with a second crystal tank; and a liquid phase outlet of the second separator is communicated with a second crystallization mother liquor tank. The primary crystallization mother liquor is used as a solvent to dissolve a new material and then is subjected to secondary crystallization, so that the solvent and solvent recovery energy consumption are saved, meanwhile, the product yield is improved, the additional value of mother liquor sugar is increased, the cost is low, and the method is suitable for industrial production.

Description

TECHNICAL FIELD

[0001] The utility model relates to the reclamation and utilization device of rebaudioside mother liquor in the rebaudioside production field. BACKGROUND

[0002] At present, most of the rebaudioside production process is generally through the crystallization to take out rebaudioside A from rebaudioside total glycoside. After the first crystallization of rebaudioside A, other components in the total rebaudioside glycoside are usually recovered by secondary crystallization. A large amount of crystallization mother liquor sugar (mother liquor separated by crystallization filtration, obtained by drying) will inevitably be produced after twice crystallization. The composition of this part of mother liquor sugar is more, but the total glycoside content and the content of each component are not high, and it is difficult to obtain total glycoside sugar or each single component by crystallization. The overall recovery rate of glycoside recovered from mother liquor sugar by crystallization method is not high, the input cost is relatively high, and it is not conducive to industrial production. SUMMARY

[0003] The technical problem to be solved by the utility model is: in view of the deficiencies existing in the prior art, a reclamation and utilization device of rebaudioside mother liquor is provided, which has high recovery rate, low cost and is suitable for industrial production.

[0004] To solve the above technical problems, the technical scheme of the utility model is:

[0005] The reclamation and utilization device of rebaudioside mother liquor, including the extraction tank, the outlet of the extraction tank is connected with the flocculation tank through the pipeline, the outlet of the flocculation tank is connected with the decolorization tank through the pipeline, the outlet of the decolorization tank is connected with the resolution tank through the pipeline, the outlet of the resolution tank is connected with the crude product powder tank through the pipeline, the outlet of the crude product powder tank is connected with the dissolution tank through the pipeline, the inlet of the first dissolution tank is connected with the first solvent tank through the pipeline, the outlet of the dissolution tank is connected with the first crystallization tank through the pipeline, the outlet of the first crystallization tank is connected with the first separator through the pipeline, the solid phase outlet of the first separator is connected with the first dryer, the outlet of the first dryer is connected with the first crystal tank, and the liquid phase outlet of the first separator is connected with the first crystallization mother liquor tank through the pipeline.

[0006] The outlet of the first crystallization mother liquor tank is connected with the second crystallization tank through the pipeline, the inlet of the second crystallization tank is connected with the crude product powder tank through the pipeline, the outlet of the second crystallization tank is connected with the second separator through the pipeline, the solid phase outlet of the second separator is connected with the second dryer, the outlet of the second dryer is connected with the second crystal tank, and the liquid phase outlet of the second separator is connected with the second crystallization mother liquor tank through the pipeline.

[0007] As an improved technical scheme, the outlet of the second crystallization mother liquor tank is connected with the first dealcoholization tank through the pipeline, and the upper outlet of the first dealcoholization tank is connected with the first recovery tank through the pipeline.

[0008] As the improved technical scheme, the lower outlet of the first dealcoholization tank is communicated with a third dryer through a pipeline, and the outlet of the third dryer is communicated with a powder tank.

[0009] As the improved technical scheme, the outlet of the powder tank is communicated with a third crystallization tank through a pipeline, the inlet of the third crystallization tank is communicated with a second solvent tank through a pipeline, the outlet of the third crystallization tank is communicated with a third separator through a pipeline, the solid phase outlet of the third separator is communicated with a fourth dryer, the outlet of the fourth dryer is communicated with a third crystal tank, and the liquid phase outlet of the third separator is communicated with a third crystallization mother liquor tank through a pipeline.

[0010] As the improved technical scheme, the outlet of the third crystallization mother liquor tank is communicated with a fourth crystallization tank through a pipeline, the inlet of the fourth crystallization tank is communicated with the powder tank through a pipeline, the outlet of the fourth crystallization tank is communicated with a fourth separator through a pipeline, the solid phase outlet of the fourth separator is communicated with a fifth dryer, the outlet of the fifth dryer is communicated with a fourth crystal tank, and the liquid phase outlet of the fourth separator is communicated with a fourth crystallization mother liquor tank through a pipeline.

[0011] As the improved technical scheme, the outlet of the fourth crystallization mother liquor tank is communicated with a second dealcoholization tank through a pipeline, and the upper outlet of the second dealcoholization tank is communicated with a second recovery tank through a pipeline.

[0012] As the preferred technical scheme, the lower outlet of the second dealcoholization tank is communicated with a sixth dryer through a pipeline, and the outlet of the sixth dryer is communicated with a glycoside recovery tank.

[0013] Due to the adoption of the above technical scheme, the beneficial effects of the present application are as follows:

[0014] The utility model discloses a kind of steviol glycoside mother liquor recycling devices, including extraction tank, the outlet of the extraction tank is communicated with flocculation tank by pipeline, the outlet of the flocculation tank is communicated with decoloring tank by pipeline, the outlet of the decoloring tank is communicated with analytical tank by pipeline, the outlet of the analytical tank is communicated with crude product powder tank by pipeline, the outlet of the crude product powder tank is communicated with dissolving tank by pipeline, the inlet of the dissolving tank is communicated with first solvent tank by pipeline, the outlet of the dissolving tank is communicated with first crystallization tank by pipeline, the outlet of the first crystallization tank is communicated with first separator by pipeline, the solid phase outlet of the first separator is communicated with first dryer, the outlet of the first dryer is communicated with first crystal tank, and the liquid phase outlet of the first separator is communicated with first crystallization mother liquor tank by pipeline;The outlet of the first crystallization mother liquor tank is communicated with second crystallization tank by pipeline, the inlet of the second crystallization tank is communicated to the crude product powder tank by pipeline, the outlet of the second crystallization tank is communicated with second separator by pipeline, the solid phase outlet of the second separator is communicated with second dryer, the outlet of the second dryer is communicated with second crystal tank, and the liquid phase outlet of the second separator is communicated with second crystallization mother liquor tank by pipeline.Stevia leaf is extracted, flocculated, decolorized and resolved to obtain steviol glycoside crude product powder, and the obtained steviol glycoside crude product powder and the aqueous solution of ethanol or methanol are added into dissolving tank, the dissolving solution is crystallized, and the solid phase after the crystallization material is separated by first separator is dried by first dryer to obtain rebaudioside A crystal I, and the crystallization mother liquor of liquid phase enters second crystallization tank, and the steviol glycoside crude product powder is added and resolved, and is dissolved and crystallized in second crystal tank, and the solid phase after the crystallization material is separated by second separator is dried by second dryer to obtain rebaudioside A crystal II, and the crystallization mother liquor of liquid phase enters second crystallization mother liquor tank.Secondary crystallization is carried out after new material is dissolved using primary crystallization mother liquor as solvent, solvent and solvent recovery energy consumption are saved, the yield of product is improved, the additional value of mother liquor sugar is increased, cost is low, and it is suitable for industrial production.

[0015] The outlet of the second crystallization mother liquor tank is communicated with first dealcoholization tank by pipeline, and the upper outlet of the first dealcoholization tank is communicated with first recovery tank by pipeline.Second crystallization mother liquor is heated and concentrated, and solvent is recovered, to avoid waste.

[0016] The lower outlet of the first dealcoholization tank is communicated with third dryer by pipeline, and the outlet of the third dryer is communicated with powder tank.After dealcoholization, material enters third dryer, and powder is obtained after spray drying, to reduce the waste of raw materials.

[0017] The outlet of the powder tank is communicated with a third crystallization tank through a pipeline, the inlet of the third crystallization tank is communicated with a second solvent tank through a pipeline, the outlet of the third crystallization tank is communicated with a third separator through a pipeline, the solid phase outlet of the third separator is communicated with a fourth dryer, the outlet of the fourth dryer is communicated with a third crystal tank, and the liquid phase outlet of the third separator is communicated with a third crystallization mother liquor tank. The powder and the methanol solution enter the third crystallization tank, are separated through the third separator after cooling and crystallization, the solid phase obtained is dried through the fourth dryer, and the sweet glycoside STV crystal I is obtained.

[0018] The outlet of the third crystallization mother liquor tank is communicated with a fourth crystallization tank through a pipeline, the inlet of the fourth crystallization tank is communicated with the powder tank through a pipeline, the outlet of the fourth crystallization tank is communicated with a fourth separator through a pipeline, the solid phase outlet of the fourth separator is communicated with a fifth dryer, the outlet of the fifth dryer is communicated with a fourth crystal tank, and the liquid phase outlet of the fourth separator is communicated with a fourth crystallization mother liquor tank. The third crystallization mother liquor obtained through the third separator enters the fourth crystallization tank and is mixed with the powder dried through the third dryer, is separated through the fourth separator after cooling and crystallization, and the solid phase is dried through the fifth dryer, so that the sweet glycoside STV crystal II is obtained.

[0019] The outlet of the fourth crystallization mother liquor tank is communicated with a second dealcoholization tank through a pipeline, and the upper outlet of the second dealcoholization tank is communicated with a second recovery tank through a pipeline. The fourth crystallization mother liquor obtained through the fourth separator enters the second dealcoholization tank for dealcoholization, and the solvent is recovered, so that waste is avoided.

[0020] The lower outlet of the second dealcoholization tank is communicated with a sixth dryer through a pipeline, and the outlet of the sixth dryer is communicated with a glycoside recovery tank. The solid phase obtained through the fourth separator is dried through the sixth dryer, and the powder obtained is extracted for other glycosides, so that economic benefits are improved. BRIEF DESCRIPTION OF DRAWINGS

[0021] The utility model will be further explained in connection with the drawings and examples.

[0022] Figure 1 It is the structural schematic diagram of the utility model embodiment;

[0023] Wherein: 1, extraction tank; 2, flocculation tank; 3, decolorization tank; 4, analysis tank; 5, crude powder tank; 6, dissolving tank; 7, first solvent tank; 8, first crystallization tank; 9, first separator; 10, first dryer; 11, first crystal tank; 12, first crystallization mother liquor tank; 13, second crystallization tank; 14, second separator; 15, second dryer; 16, second crystal tank; 17, second crystallization mother liquor tank; 18, first dealcoholization tank; 19, first recovery tank; 20, third dryer; 21, powder tank; 22, third crystallization tank; 23, second solvent tank; 24, third separator; 25, fourth dryer; 26, third crystal tank; 27, third crystallization mother liquor tank; 28, fourth crystallization tank; 29, fourth separator; 30, fifth dryer; 31, fourth crystal tank; 32, fourth crystallization mother liquor tank; 33, second dealcoholization tank; 34, second recovery tank; 35, sixth dryer; 36, glycoside recovery tank. DETAILED DESCRIPTION

[0024] The utility model is further explained below in combination with the drawings and examples.

[0025] As Figure 1As shown, a kind of recycling device of steviol glycoside mother liquor, including extraction tank 1, the outlet of the extraction tank 1 is communicated with flocculation tank 2 by pipeline, the outlet of the flocculation tank 2 is communicated with decoloring tank 3 by pipeline, the outlet of the decoloring tank 3 is communicated with resolution tank 4 by pipeline, the outlet of the resolution tank 4 is communicated with crude product powder tank 5 by pipeline, the inlet of the crude product powder tank 5 is communicated with first solvent tank 7 by pipeline, the outlet of the crude product powder tank 5 is communicated with dissolution tank 6 by pipeline, the inlet of the dissolution tank 6 is communicated with first solvent tank 7 by pipeline, the outlet of the dissolution tank 6 is communicated with first crystallization tank 8 by pipeline, the outlet of the first crystallization tank 8 is communicated with first separator 9 by pipeline, the solid phase outlet of the first separator 9 is communicated with first dryer 10, the outlet of the first dryer 10 is communicated with first crystal tank 11, the liquid phase outlet of the first separator 9 is communicated with first crystallization mother liquor tank 12 by pipeline;The outlet of the first crystallization mother liquor tank 12 is communicated with second crystallization tank 13 by pipeline, the inlet of the second crystallization tank 13 is communicated to the crude product powder tank 5 by pipeline, the outlet of the second crystallization tank 13 is communicated with second separator 14 by pipeline, the solid phase outlet of the second separator 14 is communicated with second dryer 15, the outlet of the second dryer 15 is communicated with second crystal tank 16, the liquid phase outlet of the second separator 14 is communicated with second crystallization mother liquor tank 17 by pipeline. Steviolbioside crude product powder is obtained by extraction, flocculation, decolorization and resolution of steviol leaf, and the obtained steviolbioside crude product powder and the aqueous solution of ethanol or methanol are added into the dissolution tank 6, the dissolution solution is crystallized, the solid phase after the crystallization material is separated by the first separator 9 is dried by the first dryer 10 to obtain rebaudioside A crystal I, and the crystallization mother liquor of the liquid phase enters the second crystallization tank 13, the steviolbioside crude product powder is added and resolved, is dissolved and crystallized in the second crystal tank 16, the solid phase after the crystallization material is separated by the second separator 14 is dried by the second dryer 15 to obtain rebaudioside A crystal II, and the crystallization mother liquor of the liquid phase enters the second crystallization mother liquor tank 17. The new material is dissolved by using the first crystallization mother liquor as a solvent for secondary crystallization, the solvent and the energy consumption of solvent recovery are saved, the yield of the product is improved, the additional value of the mother liquor sugar is increased, the cost is low, and the industrial production is suitable.

[0026] The outlet of the second crystallization mother liquor tank 17 is communicated with first dealcoholization tank 18 by pipeline, and the upper outlet of the first dealcoholization tank 18 is communicated with first recovery tank 19 by pipeline. The second crystallization mother liquor is heated and concentrated, and the solvent is recovered to avoid waste.

[0027] The lower outlet of the first dealcoholization tank 18 is communicated with third dryer 20 by pipeline, and the outlet of the third dryer 20 is communicated with powder tank 21. The material after dealcoholization enters the third dryer 20, is spray dried to obtain powder, and the waste of raw material is reduced.

[0028] The outlet of the powder tank 21 is communicated with a third crystallization tank 22 through a pipeline, the inlet of the third crystallization tank 22 is communicated with a second solvent tank 23 through a pipeline, the outlet of the third crystallization tank 22 is communicated with a third separator 24 through a pipeline, the solid phase outlet of the third separator 24 is communicated with a fourth dryer 25, the outlet of the fourth dryer 25 is communicated with a third crystal tank 26, and the liquid phase outlet of the third separator 24 is communicated with a third crystallization mother liquor tank 27. The powder and the methanol solution enter the third crystallization tank 22, are separated through the third separator 24 after cooling and crystallization, the solid phase obtained is dried through the fourth dryer 25, and the sweet glycoside STV crystal I is obtained.

[0029] The outlet of the third crystallization mother liquor tank 27 is communicated with a fourth crystallization tank 28 through a pipeline, the inlet of the fourth crystallization tank 28 is communicated with the powder tank 21 through a pipeline, the outlet of the fourth crystallization tank 28 is communicated with a fourth separator 29 through a pipeline, the solid phase outlet of the fourth separator 29 is communicated with a fifth dryer 30, the outlet of the fifth dryer 30 is communicated with a fourth crystal tank 31, and the liquid phase outlet of the fourth separator 29 is communicated with a fourth crystallization mother liquor tank 32. The third crystallization mother liquor obtained through the third separator 24 enters the fourth crystallization tank 28, is mixed with the powder dried through the third dryer 20, is separated through the fourth separator 29 after cooling and crystallization, and the solid phase is dried through the fifth dryer 30, so that the sweet glycoside STV crystal II is obtained.

[0030] The outlet of the fourth crystallization mother liquor tank 32 is communicated with a second dealcoholization tank 33 through a pipeline, and the upper outlet of the second dealcoholization tank 33 is communicated with a second recovery tank 34 through a pipeline. The fourth crystallization mother liquor obtained through the fourth separator 29 enters the second dealcoholization tank 33 to be dealcoholized, and the solvent is recovered, so that waste is avoided.

[0031] The lower outlet of the second dealcoholization tank 33 is communicated with a sixth dryer 35 through a pipeline, and the outlet of the sixth dryer 35 is communicated with a glycoside recovery tank 36. The solid phase obtained through the fourth separator 29 is dried through the sixth dryer 35, and the powder obtained is extracted for other glycosides, so that economic benefits are improved.

[0032] It should be understood that the above embodiments are only used for illustrating the present application and are not used for limiting the scope of the present application. In addition, it should be understood that after reading the content of the present application, those skilled in the art can make various modifications or changes to the present application, and these equivalent forms also fall within the scope defined by the appended claims of the present application.

Claims

1. A device for recycling steviol glycoside mother liquor, comprising an extraction tank, the outlet of which is connected via a pipeline to a flocculation tank, the outlet of which is connected via a pipeline to a decolorization tank, the outlet of which is connected via a pipeline to a separation tank, and the outlet of which is connected via a pipeline to a crude powder tank, characterized in that: The outlet of the crude powder tank is connected to a dissolving tank via a pipeline. The inlet of the dissolving tank is connected to a first solvent tank via a pipeline. The outlet of the dissolving tank is connected to a first crystallization tank via a pipeline. The outlet of the first crystallization tank is connected to a first separator via a pipeline. The solid phase outlet of the first separator is connected to a first dryer. The outlet of the first dryer is connected to the first crystallization tank. The liquid phase outlet of the first separator is connected to a first crystallization mother liquor tank via a pipeline. The outlet of the first crystallization mother liquor tank is connected to a second crystallization tank via a pipeline. The inlet of the second crystallization tank is connected to the crude powder tank via a pipeline. The outlet of the second crystallization tank is connected to a second separator via a pipeline. The solid phase outlet of the second separator is connected to a second dryer. The outlet of the second dryer is connected to a second crystallization tank. The liquid phase outlet of the second separator is connected to the second crystallization mother liquor tank via a pipeline.

2. The device for recycling steviol glycoside mother liquor as described in claim 1, characterized in that: The outlet of the second crystallization mother liquor tank is connected to the first desalcoholization tank via a pipeline, and the upper outlet of the first desalcoholization tank is connected to the first recovery tank via a pipeline.

3. The device for recycling steviol glycoside mother liquor as described in claim 2, characterized in that: The lower outlet of the first dealcoholization tank is connected to a third dryer via a pipeline, and the outlet of the third dryer is connected to a powder tank.

4. The device for recycling steviol glycoside mother liquor as described in claim 3, characterized in that: The outlet of the powder tank is connected to a third crystallization tank via a pipeline. The inlet of the third crystallization tank is connected to a second solvent tank via a pipeline. The outlet of the third crystallization tank is connected to a third separator via a pipeline. The solid phase outlet of the third separator is connected to a fourth dryer. The outlet of the fourth dryer is connected to the third crystallization tank. The liquid phase outlet of the third separator is connected to a third crystallization mother liquor tank via a pipeline.

5. The device for recycling steviol glycoside mother liquor as described in claim 4, characterized in that: The outlet of the third crystallization mother liquor tank is connected to a fourth crystallization tank via a pipeline. The inlet of the fourth crystallization tank is connected to the powder tank via a pipeline. The outlet of the fourth crystallization tank is connected to a fourth separator via a pipeline. The solid phase outlet of the fourth separator is connected to a fifth dryer. The outlet of the fifth dryer is connected to the fourth crystallization tank. The liquid phase outlet of the fourth separator is connected to the fourth crystallization mother liquor tank via a pipeline.

6. The device for recycling steviol glycoside mother liquor as described in claim 5, characterized in that: The outlet of the fourth crystallization mother liquor tank is connected to a second dealcoholization tank via a pipeline, and the upper outlet of the second dealcoholization tank is connected to a second recovery tank via a pipeline.

7. The device for recycling steviol glycoside mother liquor as described in claim 6, characterized in that: The lower outlet of the second dealcoholization tank is connected to a sixth dryer via a pipeline, and the outlet of the sixth dryer is connected to a glycoside recovery tank.

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