CN102489036A - Method for extracting lycopene by using continuous countercurrent ultrasonic extractor - Google Patents
Method for extracting lycopene by using continuous countercurrent ultrasonic extractor Download PDFInfo
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- CN102489036A CN102489036A CN2011104336605A CN201110433660A CN102489036A CN 102489036 A CN102489036 A CN 102489036A CN 2011104336605 A CN2011104336605 A CN 2011104336605A CN 201110433660 A CN201110433660 A CN 201110433660A CN 102489036 A CN102489036 A CN 102489036A
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Abstract
The invention provides a technical scheme of a method for extracting lycopene by using a continuous countercurrent ultrasonic extractor. In the scheme, the method comprises the following steps of: I, quantitatively inputting tomato paste into a dispersing device, heating with the tomato paste and a dispersing solvent by using a heat exchanger in the weight (kilogram) to volume (liter) ratio of 1:(0.5-3), and inputting into a dispersing device; II, uniformly mixing the tomato paste and the dispersing solvent in the dispersing device; III, inputting a mixture of the tomato paste and the dispersing agent into an extracting pipe from the feeding hole of the ultrasonic extractor, heating the tomato paste and an extraction solvent in the weight (kilogram) to volume (liter) ratio of 1:(1-5), and inputting into the extracting pipe through the residue discharging hole of the ultrasonic extractor; IV, performing countercurrent ultrasonic extraction on the tomato paste and the extraction solvent in the extracting pipe of the ultrasonic extractor at the normal temperature under the normal pressure for 45-60 minutes; and V, after extraction is completed, discharging tomato paste residues from the residue discharging hole of the ultrasonic extractor, treating and recovering the solvent, draining an extracting solution from the draining hole of the ultrasonic extractor, and performing concentration and desolventizing treatment to obtain finished lycopene.
Description
Technical field:
What the present invention relates to is a kind of method for distilling, especially utilizes the continuous flow upstream ultrasonic extractor to extract lycopene method.
Background technology:
Lycopene is the main pigment of ripe tomato, is a kind of oxygen-free carotenoid, has extremely strong antioxidation activity, and the effect of removing free radical outclass other carotenoid and vitamin E, therefore is the precious raw material of medicine and health products.Utilize catsup to extract lycopene method in the prior art; Technique known is equipment extraction lycopenes such as employing multi-function extractor; It is longer to utilize multi-function extractor to extract lycopene general extraction time, and the organic solvent that extracts in the tomato pomace of back is difficult to reclaim, and the consumption of solvent is big; And be difficult for realizing continuous automatic production that this is the existing in prior technology weak point.
Summary of the invention:
The present invention is exactly not enough to existing in prior technology, and provides a kind of continuous flow upstream ultrasonic extractor that utilizes to extract the lycopene method technical scheme, and this scheme is to be employed on the continuous flow upstream ultrasonic extractor; Dilute catsup with dispersion solvent; With extracting solvent counter-flow extraction lycopene, extraction efficiency is improved, the consumption of solvent reduces; And under the condition of normal temperature, sealing, accomplish leaching process, guaranteed the extraction quality of lycopene.
This programme is realized through following technical measures: this programme utilizes the continuous flow upstream ultrasonic extractor to extract lycopene method, and it is that processing step is following:
Step 1: catsup is quantitatively imported dispersal device, with catsup and dispersion solvent by weight the ratio that rises of kilogram and volume be 1 after heat exchanger is heated to 30-60 ℃, to import dispersal device than the dispersion solvent of 0.5-3;
Step 2: the catsup and the dispersion solvent of step 1 are evenly mixed in dispersal device;
Step 3: the mixture of catsup that mixes in the step 2 and the dispersion solvent charging aperture by the continuous flow upstream ultrasonic extractor is input in the extraction tube, will extracts solvent simultaneously in catsup and extract the weight of solvent kilogram and ratio that volume rises is that the 1 extraction solvent than 1-5 is heated to the 30-60 ℃ of deslagging end by the continuous flow upstream ultrasonic extractor through heat exchanger and is input in the extraction tube;
Step 4: the catsup after the dilution carried out the adverse current ultrasonic Extraction 30-60 minute with the extraction solvent under normal temperature, the normal pressure in the extraction tube of continuous flow upstream ultrasonic extractor;
Step 5: after the adverse current ultrasonic Extraction of completing steps four, discharge the tomato residue of soya, again the tomato residue of soya is handled the recovery solvent by the slag-drip opening of continuous flow upstream ultrasonic extractor; Leakage fluid dram by the continuous flow upstream ultrasonic extractor is discharged extract, and this extract gets the lycopene finished product through concentrated, carrying out precipitation treatment.
The concrete characteristics of this programme also have, and the described dispersion solvent of step 1 is 95% ethanol or methyl alcohol or acetone.The described extraction solvent of step 3 is a benzinum.Described benzinum or be 90-120 gasoline or chloroform or ether.It is that the tomato residue of soya is input in the desolventizing machine that the tomato residue of soya of the said solvent recovery of step 5 is handled; Earlier the tomato residue of soya is preheating to 50-70 ℃; Input pressure makes the solvent vaporization at the saturated vapor of 0.01-0.05Mpa then; Solvent gas after the vaporization is input to knockout drum through 10-30 ℃ cooling water is cooled to liquid in condenser after, in knockout drum, two kinds of separated from solvent is reclaimed, be input in the storage tank separately subsequent use.The concentration of the said extract of step 5 is that extract is imported the slag liquid/gas separator; Extract after slag liquid separates is input to the one-level evaporator, and the control evaporating temperature makes the 80-95% of extract evaporation and concentration to extract total amount between 25-40 ℃; To be input to the dual evaporation jar through the extract after one-level concentrates again; Control dual evaporation temperature discharges the qualified back of extract evaporation and concentration, precipitation to dissolvent residual after one-level concentrates between 25-40 ℃, promptly gets the lycopene finished product.Evaporate the solvent that in the extract, gaseous state is condensed in the liquid input solvent tank subsequent use through condenser again.
The beneficial effect of this programme can be learnt according to the narration to such scheme; Because this scheme is to utilize the continuous flow upstream ultrasonic extractor to accomplish by extracting lycopene in the catsup through five steps; Leaching process has adopted two kinds of solvents, a kind of be the conventional solvent such as ethanol, methyl alcohol of indissoluble lycopene as dispersion solvent, be used to dilute catsup; Reduce the viscosity of catsup, another kind is can dissolve the conventional solvent benzinum of lycopene as extracting solvent.Catsup after the charging aperture input dilution of continuous flow upstream ultrasonic extractor gets into extraction tube, and the slag-drip opening to the continuous flow upstream ultrasonic extractor moves in extraction tube.Extract solvent in the slag-drip opening input of continuous flow upstream ultrasonic extractor and get into extraction tube, and reverse mobile to the leakage fluid dram of continuous flow upstream ultrasonic extractor in extraction tube.Catsup is opposite with the flow direction that extracts solvent in extraction tube, and the lycopene in the catsup is dissolved in the extraction solvent fast under the effect of the ultrasonic of extraction tube and stirring, accomplishes leaching process.Because whole leaching process is to accomplish under the condition of normal temperature, normal pressure and sealing in extraction tube, therefore, the good quality of product of extraction, the content of lycopene is higher in the product, can be greater than 10%, the residual quantity of solvent is less than 25ppm.Because ultrasonic effect is arranged in leaching process, so extraction rate is fast, general extraction rate was less than 60 minutes, and extraction efficiency is high, yield is high, and extract yield can be more than 90%.In addition, the consumption that is exactly solvent is few, and in whole process of production, the waste less than 1% of solvent so reduced production cost, has also reduced the pollution to environment.This shows that the present invention compared with prior art has outstanding substantive distinguishing features and obvious improvement, the beneficial effect of its enforcement also is conspicuous.
The specific embodiment:
For clearly demonstrating the technical characterstic of this programme, through a specific embodiment, this programme is set forth below.
This programme utilizes the continuous flow upstream ultrasonic extractor to extract lycopene method, and its processing step is following:
Step 1: catsup 100kg is quantitatively imported dispersal device; With the ethanol of catsup and 95% or methyl alcohol or acetone is retarder thinner; The ethanol of this specific embodiment employing 95% is dispersion solvent, and kilogram is 1 ratio than 0.5-3 with the ratio that volume rises by weight, and this specific embodiment adopts 1 to 1 w/v; The dispersion solvent ethanol that is 100L is heated to 30-60 ℃ through heat exchanger, and this specific embodiment is to import dispersal device after being heated to 35 ℃;
Step 2: the catsup and the dispersion solvent ethanol of step 1 are evenly mixed in dispersal device;
Step 3: the mixture of catsup that mixes in the step 2 and the dispersion solvent ethanol charging aperture by the continuous flow upstream ultrasonic extractor is input in the extraction tube; Simultaneously with benzinum as extracting solvent; In catsup with extract the solvent benzinum by weight kilogram be 1 ratio with the ratio that volume rises than 1-5; Ratio that to be the weight kilogram rise with volume that this specific embodiment adopts is 1 to 3 extraction solvent benzinum; Be heated to 30-60 ℃ through heat exchanger, this specific embodiment is to be heated to 35 ℃, is input in the extraction tube by the slag-drip opening of continuous flow upstream ultrasonic extractor;
Step 4: the catsup after the dilution carried out the adverse current ultrasonic Extraction 45-60 minute with extraction solvent benzinum under normal temperature, the normal pressure in the extraction tube of continuous flow upstream ultrasonic extractor, this specific embodiment is to extract 50 minutes;
Step 5: after the adverse current ultrasonic Extraction of completing steps four, discharge the tomato residue of soya, again the tomato residue of soya is handled the recovery solvent by the slag-drip opening of continuous flow upstream ultrasonic extractor; Leakage fluid dram by the continuous flow upstream ultrasonic extractor is discharged extract, and this extract gets the lycopene finished product through concentrated, carrying out precipitation treatment.
It is that the tomato residue of soya is input in the desolventizing machine that the tomato residue of soya of said solvent recovery is handled; Earlier the tomato residue of soya is preheating to 50-60 ℃; Controlling input pressure then makes hydrone substitute the solvent molecule in the slag at the saturated vapor of 0.01-0.02Mpa; Solvent gas after the vaporization is cooled to liquid and enters into knockout drum in condenser, in knockout drum, two kinds of solvents are carried out Separation and Recovery after 5-20 ℃ of cooling water heat exchange, be input in the storage tank separately subsequent use.
The concentration of said extract is extract to be imported the slag liquid/gas separator extract is carried out the crude separation of slag liquid; Extract filters through 200-800 order filter again; Extract after filtering is input to the one-level evaporator, and the control evaporating temperature makes 15% of extract evaporation and concentration to extract total amount between 25-40 ℃; To be input to the dual evaporation jar through the concentrate after one-level concentrates again; Control dual evaporation temperature makes extract evaporation and concentration, precipitation after one-level concentrates discharge to detecting the residual qualified back of solvent between 25-40 ℃, is the lycopene finished product.Evaporate the solvent that in the extract, gaseous state is condensed in the liquid input solvent tank subsequent use through condenser again.
Claims (6)
1. one kind is utilized the continuous flow upstream ultrasonic extractor to extract lycopene method, it is characterized in that processing step is following:
Step 1: catsup is quantitatively imported dispersal device, with catsup and dispersion solvent by weight the ratio that rises of kilogram and volume be 1 after heat exchanger is heated to 30-60 ℃, to import dispersal device than the dispersion solvent of 0.5-3;
Step 2: the catsup and the dispersion solvent of step 1 are evenly mixed in dispersal device;
Step 3: the mixture of catsup that mixes in the step 2 and the dispersion solvent charging aperture by the continuous flow upstream ultrasonic extractor is input in the extraction tube, will extracts solvent simultaneously in catsup and extract the weight of solvent kilogram and ratio that volume rises is that the 1 extraction solvent than 1-5 is heated to the 30-60 ℃ of deslagging end by the continuous flow upstream ultrasonic extractor through heat exchanger and is input in the extraction tube;
Step 4: the catsup after the dilution carried out the adverse current ultrasonic Extraction 30-60 minute with the extraction solvent under normal temperature, the normal pressure in the extraction tube of continuous flow upstream ultrasonic extractor;
Step 5: after the adverse current ultrasonic Extraction of completing steps four, discharge the tomato residue of soya, again the tomato residue of soya is handled the recovery solvent by the slag-drip opening of continuous flow upstream ultrasonic extractor; Leakage fluid dram by the continuous flow upstream ultrasonic extractor is discharged extract, and this extract gets the lycopene finished product through concentrated, carrying out precipitation treatment.
2. method according to claim 1 is characterized in that: the described dispersion solvent of step 1 is 95% ethanol or methyl alcohol or acetone.
3. method according to claim 1 is characterized in that: the described extraction solvent of step 3 is a benzinum.
4. method according to claim 3 is characterized in that: described benzinum or for 90-120 gasoline or chloroform or ether.
5. method according to claim 1; It is characterized in that: it is that the tomato residue of soya is input in the desolventizing machine that the tomato residue of soya of the said solvent recovery of step 5 is handled; Earlier the tomato residue of soya is preheating to 50-70 ℃, input pressure makes the solvent vaporization at the saturated vapor of 0.01-0.05Mpa then, and the solvent gas after the vaporization is input to knockout drum through 10-30 ℃ cooling water is cooled to liquid in condenser after; In knockout drum, two kinds of separated from solvent are reclaimed, be input in the storage tank separately subsequent use.
6. method according to claim 1; It is characterized in that: the concentration of the said extract of step 5 is that extract is imported the slag liquid/gas separator; Extract after slag liquid separates is input to the one-level evaporator, and the control evaporating temperature makes the 80-95% of extract evaporation and concentration to extract total amount between 25-40 ℃; To be input to the dual evaporation jar through the extract after one-level concentrates again; Control dual evaporation temperature discharges the qualified back of extract evaporation and concentration, precipitation to dissolvent residual after one-level concentrates between 25-40 ℃, promptly gets the lycopene finished product.
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| CN2011104336605A CN102489036A (en) | 2011-12-22 | 2011-12-22 | Method for extracting lycopene by using continuous countercurrent ultrasonic extractor |
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| CN2011104336605A CN102489036A (en) | 2011-12-22 | 2011-12-22 | Method for extracting lycopene by using continuous countercurrent ultrasonic extractor |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103483134A (en) * | 2013-04-18 | 2014-01-01 | 杨红梅 | Ultrasonic countercurrent extraction method for lycopene |
| CN104814917A (en) * | 2015-04-24 | 2015-08-05 | 新疆西域果宝生物科技有限公司 | Cosmetic composition |
| CN105061281A (en) * | 2015-09-12 | 2015-11-18 | 顾伟 | Method for extracting carotene through ultrasonic-assisted countercurrent extraction |
| CN114401775A (en) * | 2019-07-26 | 2022-04-26 | 卡利亚里大学 | Isolation of chromoplast carotenoids from fruit |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN2690024Y (en) * | 2004-03-19 | 2005-04-06 | 黑龙江省计算中心 | Supersonic reinforced continuous counter flow leaching device |
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2011
- 2011-12-22 CN CN2011104336605A patent/CN102489036A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2690024Y (en) * | 2004-03-19 | 2005-04-06 | 黑龙江省计算中心 | Supersonic reinforced continuous counter flow leaching device |
Non-Patent Citations (1)
| Title |
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| 蔡俊等: "番茄红素提取工艺的研究", 《食品与发酵工业》, vol. 26, no. 2, 20 April 2000 (2000-04-20), pages 50 - 53 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103483134A (en) * | 2013-04-18 | 2014-01-01 | 杨红梅 | Ultrasonic countercurrent extraction method for lycopene |
| CN103483134B (en) * | 2013-04-18 | 2015-05-13 | 杨红梅 | Ultrasonic countercurrent extraction method for lycopene |
| CN104814917A (en) * | 2015-04-24 | 2015-08-05 | 新疆西域果宝生物科技有限公司 | Cosmetic composition |
| CN104814917B (en) * | 2015-04-24 | 2018-03-27 | 新疆西域果宝生物科技有限公司 | Cosmetic composition |
| CN105061281A (en) * | 2015-09-12 | 2015-11-18 | 顾伟 | Method for extracting carotene through ultrasonic-assisted countercurrent extraction |
| CN114401775A (en) * | 2019-07-26 | 2022-04-26 | 卡利亚里大学 | Isolation of chromoplast carotenoids from fruit |
| CN114401775B (en) * | 2019-07-26 | 2023-11-07 | 卡利亚里大学 | Isolation of color body carotenoids from fruits |
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Application publication date: 20120613 |