CN209669104U - The production equipment of aurantiamarin - Google Patents
The production equipment of aurantiamarin Download PDFInfo
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- CN209669104U CN209669104U CN201920237963.1U CN201920237963U CN209669104U CN 209669104 U CN209669104 U CN 209669104U CN 201920237963 U CN201920237963 U CN 201920237963U CN 209669104 U CN209669104 U CN 209669104U
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- QUQPHWDTPGMPEX-UTWYECKDSA-N aurantiamarin Natural products COc1ccc(cc1O)[C@H]1CC(=O)c2c(O)cc(O[C@@H]3O[C@H](CO[C@@H]4O[C@@H](C)[C@H](O)[C@@H](O)[C@H]4O)[C@@H](O)[C@H](O)[C@H]3O)cc2O1 QUQPHWDTPGMPEX-UTWYECKDSA-N 0.000 title claims abstract description 69
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 35
- 238000002425 crystallisation Methods 0.000 claims abstract description 57
- 230000008025 crystallization Effects 0.000 claims abstract description 46
- 238000002156 mixing Methods 0.000 claims abstract description 46
- 230000001105 regulatory effect Effects 0.000 claims abstract description 27
- 239000007788 liquid Substances 0.000 claims abstract description 26
- 239000002002 slurry Substances 0.000 claims abstract description 22
- 239000002904 solvent Substances 0.000 claims abstract description 21
- 239000000706 filtrate Substances 0.000 claims abstract description 16
- 235000013399 edible fruits Nutrition 0.000 claims abstract description 13
- 239000007787 solid Substances 0.000 claims abstract description 12
- 240000004307 Citrus medica Species 0.000 claims abstract description 9
- 239000002245 particle Substances 0.000 claims abstract description 6
- 230000001276 controlling effect Effects 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 5
- 239000012530 fluid Substances 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 5
- 239000000284 extract Substances 0.000 abstract description 5
- 238000000605 extraction Methods 0.000 abstract description 5
- 239000000243 solution Substances 0.000 description 25
- 238000011084 recovery Methods 0.000 description 6
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 230000032258 transport Effects 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 235000020971 citrus fruits Nutrition 0.000 description 3
- 239000013078 crystal Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 2
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 description 2
- 241000207199 Citrus Species 0.000 description 2
- 241001672694 Citrus reticulata Species 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- 241001093501 Rutaceae Species 0.000 description 2
- 229960000583 acetic acid Drugs 0.000 description 2
- 239000012670 alkaline solution Substances 0.000 description 2
- 210000002421 cell wall Anatomy 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 235000019441 ethanol Nutrition 0.000 description 2
- 229930182470 glycoside Natural products 0.000 description 2
- 150000002338 glycosides Chemical class 0.000 description 2
- 230000002045 lasting effect Effects 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 2
- 238000004080 punching Methods 0.000 description 2
- 150000003384 small molecules Chemical class 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 241000219495 Betulaceae Species 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- DQFBYFPFKXHELB-UHFFFAOYSA-N Chalcone Natural products C=1C=CC=CC=1C(=O)C=CC1=CC=CC=C1 DQFBYFPFKXHELB-UHFFFAOYSA-N 0.000 description 1
- 244000183685 Citrus aurantium Species 0.000 description 1
- 235000007716 Citrus aurantium Nutrition 0.000 description 1
- 240000002319 Citrus sinensis Species 0.000 description 1
- 235000005976 Citrus sinensis Nutrition 0.000 description 1
- AEMRFAOFKBGASW-UHFFFAOYSA-N Glycolic acid Chemical compound OCC(O)=O AEMRFAOFKBGASW-UHFFFAOYSA-N 0.000 description 1
- 241000207923 Lamiaceae Species 0.000 description 1
- 244000046052 Phaseolus vulgaris Species 0.000 description 1
- 235000010627 Phaseolus vulgaris Nutrition 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000005513 chalcones Nutrition 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- ODLMAHJVESYWTB-UHFFFAOYSA-N ethylmethylbenzene Natural products CCCC1=CC=CC=C1 ODLMAHJVESYWTB-UHFFFAOYSA-N 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 229930003935 flavonoid Natural products 0.000 description 1
- 235000017173 flavonoids Nutrition 0.000 description 1
- 150000002215 flavonoids Chemical class 0.000 description 1
- 239000012362 glacial acetic acid Substances 0.000 description 1
- 235000021552 granulated sugar Nutrition 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- QUQPHWDTPGMPEX-QJBIFVCTSA-N hesperidin Chemical compound C1=C(O)C(OC)=CC=C1[C@H]1OC2=CC(O[C@H]3[C@@H]([C@@H](O)[C@H](O)[C@@H](CO[C@H]4[C@@H]([C@H](O)[C@@H](O)[C@H](C)O4)O)O3)O)=CC(O)=C2C(=O)C1 QUQPHWDTPGMPEX-QJBIFVCTSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 235000013372 meat Nutrition 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000009965 odorless effect Effects 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 230000009967 tasteless effect Effects 0.000 description 1
- DQFBYFPFKXHELB-VAWYXSNFSA-N trans-chalcone Chemical compound C=1C=CC=CC=1C(=O)\C=C\C1=CC=CC=C1 DQFBYFPFKXHELB-VAWYXSNFSA-N 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a kind of production equipments of aurantiamarin.The production equipment of aurantiamarin, including for impregnating dried immature fruit of citron orange particle and forming the infuser device of slurry, for installing the solvent device of aurantiamarin extracting solution, the output end of infuser device and the output end of solvent device are connected to moment mixing arrangement, equipment for separating liquid from solid in moment mixing arrangement output end, the pH regulating device of filtrate output end in equipment for separating liquid from solid, the crystallization apparatus of the output end in pH regulating device；Slurry and extracting solution are liquidated by pressurization in moment mixing arrangement carries out moment and mixes.The extracting solution dosage that the production equipment of aurantiamarin uses is few, and room temperature extracts aurantiamarin, does not need consumption steam, short extraction time is moment extracting mode, and it can operate continuously, i.e., be crystallized when extracting, yield is big, and production capacity is high, at low cost, aurantiamarin high income reaches 30~35%.
Description
Technical field
The utility model relates to aurantiamarin production fields, particularly, are related to a kind of production equipment of aurantiamarin.
Background technique
Aurantiamarin be prevalent in the leaf of the citrus kind of bitter orange, sweet orange, Wenzhou dried immature fruit of citron orange and other Rutaceae, bark,
It is one of main flavonoids in tangerine peel in colored and discarded pericarp.The leftover bits and pieces of citrus fruit per ton such as pericarp, fruit
The aurantiamarin of 10kg~15kg can be obtained in meat etc..With fruit grow up and it is mature, the content of aurantiamarin is decreased obviously, and diameter is
The aurantiamarin that the fruit of 1.5cm~2cm contains accounts for 20% of dry weight or more, but when diameter increases to the fruit of 2.5cm~3.5cm
The aurantiamarin contained in fact accounts for 15% or less dry weight.Other than citrus, there is also aurantiamarins in other plants, such as in beans
Section, Labiatae, all exists in rutaceae Betulaceae, these plants are grown on Hongkong mostly.In addition, being grown in uncommon
Also there is the existing report of aurantiamarin in the root of the cured short Ji of two species and angle Ji and Sichuan Province's wilsonii.
Aurantiamarin is tasteless odorless, and sterling is in Microelements in Hair acicular crystal, and color is white or faint yellow, and melting range is 258
DEG C~260 DEG C.Molecular formula is C28H34O15, molecular weight 610.5.It is readily soluble in alkaline solution and pyridine, obtains clear Huang
Color solution is slightly soluble in methanol, glacial acetic acid, is practically insoluble between propyl alcohol, benzene and chloroform, is acicular crystallization in dilute acetic acid.
Open loop forms chalcone in alkaline solution, is flaxen crystallization.Since aurantiamarin and other similar glycocide compositions are multiple
Miscellaneous crystal largely influences its solubility and other physical properties, so hardly resulting in its standard items.It is existing to set
Standby generally to prepare aurantiamarin using common apparatus, the device is complicated, at high cost, and the wastewater flow rate generated is big, and process time is longer,
Recovery rate reduces, and purity is poor.
Utility model content
The utility model provides a kind of production equipment of aurantiamarin, is mentioned with solving the aurantiamarin that common apparatus is prepared
Take rate low, the technical issues of purity difference.
The technical solution adopted in the utility model is as follows:
A kind of production equipment of aurantiamarin, including for impregnating dried immature fruit of citron orange particle and forming the infuser device of slurry, for holding
Fill the solvent device of aurantiamarin extracting solution, the output end of infuser device and the output end of solvent device are connected to moment and mix dress
It sets, moment mixing arrangement output end is connected to equipment for separating liquid from solid, the pH tune that the filtrate output end of equipment for separating liquid from solid is connected to
Regulating device, the crystallization apparatus of the output end in pH regulating device；The slurry of infuser device output is mentioned with what solvent device exported
It takes liquid to export by pressurization and liquidates in moment mixing arrangement to realize that moment mixes.
Further, the output end of infuser device is connected with the first connecting pipeline, and the output end of solvent device is connected with the second company
Siphunculus road；First connecting pipeline is equipped with the device for exerting for pressurizeing to slurry；Second connecting pipeline is equipped with for mentioning
The device for exerting for taking liquid to pressurize.
Further, the first connecting pipeline and the second connecting pipeline are one；Alternatively, the first connecting pipeline and second connects
Siphunculus road is multiple, the first connecting pipeline and the one-to-one correspondence laying of the second connecting pipeline.
Further, the inner cavity fluid pressure of the first connecting pipeline and the second connecting pipeline is 0.5MPa~2MPa；First
The pressure sensor for signal piping inner cavity fluid pressure is additionally provided on connecting pipeline and/or the second connecting pipeline.
Further, moment mixing arrangement is equipped with the first regulating part for controlling the first connecting pipeline flow；Moment
Mixing arrangement is equipped with the second regulating part for controlling the second connecting pipeline flow.
Further, moment mixing arrangement is equipped with the spray head being connected to the first connecting pipeline and/or the second connecting pipeline；
Further, it is 3~5 that pH regulating device, which adjusts the pH value of filtrate,.
Further, crystallization apparatus uses continuous crystallisation device；Continuous crystallisation device uses the crystallization of at least thtee-stage shiplock
Unit.
Further, continuous crystallisation device uses level Four crystallizer unit；Level Four crystallizer unit uses previous stage
The bottom discharge end of crystallizer unit is connected to the top feed end of rear stage crystallizer unit by transfer pipeline.
Further, crystallization apparatus is equipped with the cooling device for reducing inner cavity temperature；Crystallization apparatus inner cavity temperature be 10 DEG C~
30℃。
The utility model has the following beneficial effects:
The production equipment of the aurantiamarin of the utility model, including infuser device, solvent device, moment mixing arrangement, solid-liquid
Separator, pH regulating device and crystallization apparatus, wherein slurry and extracting solution, which are under pressure, in moment mixing arrangement to form pair
Punching reaches moment mixing, extracts the aurantiamarin in slurry.On the one hand, the abrupt release so that feed liquid is pressurizeed divides moment mixing arrangement
Dissipate into small-molecule substance, increase the contact area with extracting solution, and pressurize abrupt release but also the dried immature fruit of citron orange cell wall rupture,
Aurantiamarin outflow, aurantiamarin are easier to incorporate in extracting solution, improve the recovery rate of aurantiamarin；On the other hand, moment mixing arrangement
What the new feed liquid inside ejected touched is all new extracting solution, and concentration difference is larger, and aurantiamarin extraction effect is more preferable.Orange peel
The extracting solution dosage that the production equipment of glycosides uses is few, and room temperature extracts aurantiamarin, does not need consumption steam, and extraction time is short, and
It can operate continuously, i.e., be crystallized when extracting, yield is big, and production capacity is high, at low cost, aurantiamarin high income, up to 30~
35%.Each device of the production equipment of aurantiamarin can be used in series, and also can be used alone, to meet different production
It is required that requiring with technique, the scope of application is wider.
Other than objects, features and advantages described above, there are also other purposes, feature and excellent for the utility model
Point.Below with reference to accompanying drawings, the utility model is described in further detail.
Detailed description of the invention
The attached drawing constituted part of this application is used to provide a further understanding of the present invention, the utility model
Illustrative embodiments and their description are not constituteed improper limits to the present invention for explaining the utility model.In attached drawing
In:
Fig. 1 is the production equipment schematic diagram of the aurantiamarin of the preferred embodiment in the utility model.
Description of symbols:
1, infuser device；11, the first connecting pipeline；2, solvent device；21, the second connecting pipeline；3, mixing arrangement；4, solid
Liquid separating apparatus；5, pH regulating device；6, crystallization apparatus.
Specific embodiment
It should be noted that in the absence of conflict, the features in the embodiments and the embodiments of the present application can phase
Mutually combination.The utility model will be described in detail below with reference to the accompanying drawings and embodiments.
Fig. 1 is the production equipment schematic diagram of the aurantiamarin of the preferred embodiment in the utility model.
As shown in Figure 1, the production equipment of the aurantiamarin of the present embodiment, including for impregnating dried immature fruit of citron orange particle and forming slurry
Infuser device 1, for installing the solvent device 2 of aurantiamarin extracting solution, the output of the output end and solvent device 2 of infuser device 1
End is connected to moment mixing arrangement 3, and 3 output end of moment mixing arrangement is connected to equipment for separating liquid from solid 4, equipment for separating liquid from solid 4
The pH regulating device 5 that is connected to of filtrate output end, the crystallization apparatus 6 of the output end in pH regulating device 5；Infuser device 1
The extracting solution that the slurry and solvent device 2 of output export is exported by pressurization and is liquidated in moment mixing arrangement 3 with reality
Existing moment mixing.The production equipment of the aurantiamarin of the utility model, including it is infuser device, solvent device, moment mixing arrangement, solid
Liquid separating apparatus, pH regulating device and crystallization apparatus, wherein slurry and extracting solution, which are under pressure, in moment mixing arrangement to form pair
Punching reaches moment mixing, extracts the aurantiamarin in slurry.On the one hand, the abrupt release so that feed liquid is pressurizeed divides moment mixing arrangement
Dissipate into small-molecule substance, increase the contact area with extracting solution, and pressurize abrupt release but also the dried immature fruit of citron orange cell wall rupture,
Aurantiamarin outflow, aurantiamarin are easier to incorporate in extracting solution, improve the recovery rate of aurantiamarin；On the other hand, moment mixing arrangement
What the new feed liquid inside ejected touched is all new extracting solution, and concentration difference is larger, and aurantiamarin extraction effect is more preferable.Orange peel
The extracting solution dosage that the production equipment of glycosides uses is few, and room temperature extracts aurantiamarin, does not need consumption steam, and extraction time is short, and
It can operate continuously, i.e., be crystallized when extracting, yield is big, and production capacity is high, at low cost, aurantiamarin high income, up to 30~
35%.Each device of the production equipment of aurantiamarin can be used in series, and also can be used alone, to meet different production
It is required that requiring with technique, the scope of application is wider.
In the present embodiment, the output end of infuser device 1 is connected with the first connecting pipeline 11, and the output end of solvent device 2 is connected with
Second connecting pipeline 21.First connecting pipeline 11 is equipped with the device for exerting for pressurizeing to slurry.On second connecting pipeline 21
Equipped with the device for exerting for pressurizeing to extracting solution.Above-mentioned first connecting pipeline 11 connects infuser device 1 and moment mixing arrangement 3
Logical, solvent device 2 is connected to by the second connecting pipeline 21 with moment mixing arrangement 3, forms ongoing operation, continuous to extract.Pressure dress
It sets for controlling the pressure for entering slurry and extracting solution in moment mixing arrangement 3, moment releases in moment mixing arrangement 3 after pressurization
It puts, so that slurry liquidates with extracting solution formation, comes into full contact with.
In the present embodiment, the first connecting pipeline 11 and the second connecting pipeline 21 are one；Alternatively, the first connecting pipeline 11
It is multiple, the first connecting pipeline 11 and the one-to-one correspondence laying of the second connecting pipeline 21 with the second connecting pipeline 21.Above-mentioned first
Connecting pipeline 11 and the second connecting pipeline 21 are that one group of a formation liquidates.First connecting pipeline 11 and and the second connecting pipeline
21 be it is multiple, multiple first connecting pipelines 11 are corresponded with multiple second connecting pipelines 21 and are laid, that is, are formed multiple groups and liquidated.
Above-mentioned first connecting pipeline 11 and the quantity of the second connecting pipeline 21 setting can be designed according to treating capacity and time, with full
The different technique requirement of foot.And multiple groups, which liquidate, to be opened simultaneously, can also successively develop from the bottom to top, avoid influencing each other
Liquidate mixed effect.Above-mentioned every group of distance to liquidate is 0.3m~1m, and when distance is less than 0.3m, the distance that liquidates is smaller, and collision is not
Sufficiently, the efficiency of the two mixing is lower；When distance is greater than 1m, due to being affected by gravity, liquid does parabola operation, causes
The probability that the two directly crashes reduces.The angle to liquidate is 0~45 °, so that the two is uniformly mixed.
In the present embodiment, the inner cavity fluid pressure of the first connecting pipeline 11 and the second connecting pipeline 21 be 0.5MPa~
2MPa.The pressure for signal piping inner cavity fluid pressure is additionally provided on first connecting pipeline 11 and/or the second connecting pipeline 21
Sensor.The pressure that above-mentioned pressurization liquidates, the at any time increase of pressure, aurantiamarin recovery rate also increase, but when the pressure to liquidate of pressurizeing
When power is more than 2MPa, under condition of high voltage, equipment loss is high, increases cost, and pressure is higher, the thermal energy of generation is more, avoids
The performance of high temperature influence aurantiamarin.Above-mentioned pressure sensor is used to show the pressure of pipeline intracavity liquid body, and control pressure is facilitated to exist
Within the scope of 0.5MPa~2MPa, so that generating void effect during abrupt release pressure, increase dried immature fruit of citron orange particle and extracting solution
Collision opportunity so that dried immature fruit of citron orange Particle Breakage refine, aurantiamarin outflow, improve the recovery rate of aurantiamarin.
In the present embodiment, moment mixing arrangement 3 is equipped with the first regulating part for controlling 11 flow of the first connecting pipeline.
Moment mixing arrangement 3 is equipped with the second regulating part for controlling 21 flow of the second connecting pipeline.First regulating part and second is adjusted
It saves part and uses valve, the slurry that infuser device 1 contains flows into the first connecting pipeline 11, and presses to slurry, and solvent device 2 is contained
The extracting solution of dress flows into the second connecting pipeline 21, and presses to extracting solution, and the first regulating part and the second regulating part stop at this time
Liquid flows into moment mixing arrangement 3, when opening the first regulating part and the second regulating part simultaneously, so that the first connecting pipeline 11 and the
Two connecting pipelines 21 are connected to moment mixing arrangement 3, and slurry and the pressure release of extracting solution moment, formation liquidate, and the two comes into full contact with, section
Raw material is saved, avoids generating excessive waste water.
In the present embodiment, moment mixing arrangement 3 is equipped with and is connected to the first connecting pipeline 11 and/or the second connecting pipeline 21
Spray head.The first connecting pipeline of slurry flows 11, presses by device for exerting, into moment mixing arrangement 3, abrupt release pressure,
And pass through spray head for slurry atomization into tiny drop, similarly, extracting solution is applied through the second connecting pipeline 21 by device for exerting
Extracting solution, into moment mixing arrangement 3, abrupt release pressure, and is atomized into tiny drop, unit volume by spray head by pressure
Increase the contact area of the two, improves aurantiamarin recovery rate.Above-mentioned equipment for separating liquid from solid 4 is plate-frame filtering device, to extract
It is filtered separation.
In the present embodiment, the pH value that pH regulating device 5 adjusts filtrate is 3~5.It is 3~5 that filtrate, which is adjusted pH value, so that
Acidity is presented in filtrate systems, and closed loop occurs in acid condition for aurantiamarin, and precipitating forms crystal and separated.It is above-mentioned to enter pH tune
The filtrate of regulating device 5 further includes enrichment facility after the pH value for adjusting filtrate, after filtrate is concentrated, enter back into crystallization apparatus 6 into
Row crystallization.
In the present embodiment, crystallization apparatus 6 uses continuous crystallisation device；Continuous crystallisation device uses the knot of at least thtee-stage shiplock
Brilliant unit.Crystallization apparatus 6 uses continuous crystallisation device, is crystallized in first degree crystalline unit, first degree crystalline is complete
Cheng Hou is transported by pipeline, is delivered in secondary crystallization unit and is crystallized again, is so connected, until forming aurantiamarin
Mixed liquor.It carries out multistage reset to crystallize, the aurantiamarin stacked area of formation is big, and quality is stablized.And crystallization generating device and
In transport pipeline, the temperature of strict control crystallization is avoided in the single crystallizing tank of tradition, and uneven heating influences crystallization effect, and
And during pipeline transports the crystallizer unit of lower level, molecule is promoted to increase collision opportunity, between acceleration molecular
Active force accelerates the speed of crystallization.Also, the time of continuous crystallisation device crystallization is 2h or so, greatly shortens crystallization time.And
And series connection crystallization, it can be lasting to discharge with continuous feed, meet the needs of production technology.However the prior art, crystallization time is at least
4h or more, and be interval discharging, it takes a long time.
Preferably, continuous crystallisation device uses level Four crystallizer unit；Level Four crystallizer unit uses previous stage knot
The bottom discharge end of brilliant unit is connected to the top feed end of rear stage crystallizer unit by transfer pipeline.In level-one
It is crystallized in crystallizer unit, after the completion of first degree crystalline, level-one aurantiamarin mixed liquor is transported by transfer pipeline to two
Grade crystallizer unit crystallized again, after the completion of secondary crystallization, by second level aurantiamarin mixed liquor by transfer pipeline transport to
Three-level crystallizer unit is crystallized, three-level crystallization after the completion of, by three-level aurantiamarin mixed liquor by transfer pipeline transport to
Level Four crystallizer unit is crystallized, and is connected to filter-pressing device by output channel.Progress level Four series system crystallization, every grade
The time of crystallization is 0.5h or so, and crystallization time is short, and forms lasting crystallization.
In the present embodiment, crystallization apparatus 6 is equipped with the cooling device for reducing inner cavity temperature.6 inner cavity temperature of crystallization apparatus is 10
DEG C~30 DEG C.6 inner cavity temperature of crystallization apparatus is 10 DEG C~30 DEG C.It is 10 DEG C~30 that cooling device, which keeps the temperature of crystallization apparatus 6,
DEG C, percent crystallization in massecuite is high, and product purity is high, high-quality.
The production equipment concrete operations of aurantiamarin in the present embodiment: 50kg granulated sugar mandarin orange be crushed into 150 mesh sieve and be added to
Infuser device 1, the calcium hydroxide mixed solution that with the volume fraction of 50L be 85% ethyl alcohol and mass fraction is 0.05% impregnate
1h obtains feed liquid, the hydroxide that the volume fraction of 150L is 85% ethyl alcohol and mass fraction is 0.1% is added in solvent device 2
Calcium mixed solution, infuser device 1 are connected on moment mixing arrangement 3 by the first connecting pipeline 11 and are equipped with valve, and first connects
Siphunculus road 11 is equipped with device for exerting, and solvent device 2 is connected on moment mixing arrangement 3 by the second connecting pipeline 21 and with the
A connecting pipe road 11 is symmetrically laid in 3 two sides of moment mixing arrangement respectively, and valve, and also are provided on moment mixing arrangement 3
Two connecting pipelines 21 are equipped with device for exerting, and device for exerting pressurizes, and the pressure of pressurization is 1MPa, open simultaneously valve, feed liquid
It liquidates with extracting solution in the formation of moment mixing arrangement 3, carries out moment mixing, form mixed liquor, mixed liquor enters separation of solid and liquid dress
4 acquisition filtrates are set, filtrate enters pH regulating device 5, and the pH value for adjusting filtrate is 3.5, connects into level Four and crystallizes unit
In, time of crystallization is 2h, and filtrate crystallizes in first degree crystalline unit, by delivery pump from first degree crystalline unit bottom
The pipeline of portion's output end is transported to secondary crystallization unit top feed end, is crystallized in secondary crystallization unit, then lead to
Delivery pump is crossed to transport from the pipeline of secondary crystallization unit bottom output end to three-level crystallizer unit top feed end, In
It crystallizes in three-level crystallizer unit, then is transported from the pipeline of three-level crystallizer unit bottom output end to four by delivery pump
Grade crystallization apparatus top feed end, crystallizes in level Four crystallizer unit, by cooling device, reduces level Four series connection crystallization and sets
Temperature is 15 DEG C in standby unit inner cavity, is connected to filter device and is separated by solid-liquid separation, obtains aurantiamarin.
The above descriptions are merely preferred embodiments of the present invention, is not intended to limit the utility model, for this
For the technical staff in field, various modifications and changes may be made to the present invention.It is all in the spirit and principles of the utility model
Within, any modification, equivalent replacement, improvement and so on should be included within the scope of protection of this utility model.
Claims (10)
1. a kind of production equipment of aurantiamarin, which is characterized in that
Including for impregnating dried immature fruit of citron orange particle and forming the infuser device (1) of slurry, the solvent for installing aurantiamarin extracting solution is filled
It sets (2), the output end of the infuser device (1) and the output end of the solvent device (2) are connected to moment mixing arrangement
(3), moment mixing arrangement (3) output end is connected to equipment for separating liquid from solid (4), the filtrate of the equipment for separating liquid from solid (4)
Output end is connected to pH regulating device (5), and the output end of the pH regulating device (5) is connected to crystallization apparatus (6)；
The slurry of infuser device (1) output and the extracting solution of solvent device (2) output are by pressurization output and mixed in the moment
It attaches together to set and be liquidated in (3) to realize that moment mixes.
2. the production equipment of aurantiamarin according to claim 1, which is characterized in that
The output end of the infuser device (1) is connected with the first connecting pipeline (11), and the output end of the solvent device (2) is connected with
Two connecting pipelines (21)；
First connecting pipeline (11) is equipped with the device for exerting for pressurizeing to the slurry；
Second connecting pipeline (21) is equipped with the device for exerting for pressurizeing to the extracting solution.
3. the production equipment of aurantiamarin according to claim 2, which is characterized in that
First connecting pipeline (11) and second connecting pipeline (21) are one；Or
First connecting pipeline (11) and second connecting pipeline (21) be it is multiple, first connecting pipeline (11) with
Second connecting pipeline (21), which corresponds, lays.
4. the production equipment of aurantiamarin according to claim 2, which is characterized in that
The inner cavity fluid pressure of first connecting pipeline (11) and second connecting pipeline (21) is 0.5MPa~2MPa；
It is additionally provided on first connecting pipeline (11) and/or second connecting pipeline (21) for signal piping inner cavity liquid
The pressure sensor of pressure.
5. the production equipment of aurantiamarin according to claim 2, which is characterized in that
The moment mixing arrangement (3) is equipped with the first regulating part for controlling the first connecting pipeline (11) flow；
The moment mixing arrangement (3) is equipped with the second regulating part for controlling the second connecting pipeline (21) flow.
6. the production equipment of aurantiamarin according to claim 2, which is characterized in that
The moment mixing arrangement (3) is equipped with to be connected with first connecting pipeline (11) and/or second connecting pipeline (21)
Logical spray head.
7. the production equipment of aurantiamarin according to claim 1, which is characterized in that
The pH value that the pH regulating device (5) adjusts the filtrate is 3~5.
8. the production equipment of aurantiamarin according to claim 1, which is characterized in that
The crystallization apparatus (6) uses continuous crystallisation device；
The continuous crystallisation device uses the crystallizer unit of at least thtee-stage shiplock.
9. the production equipment of aurantiamarin according to claim 8, which is characterized in that
The continuous crystallisation device uses level Four crystallizer unit；
The level Four crystallizer unit is connected to using the bottom discharge end of previous stage crystallizer unit by transfer pipeline
The top feed end of rear stage crystallizer unit.
10. the production equipment of aurantiamarin according to claim 8, which is characterized in that
The crystallization apparatus (6) is equipped with the cooling device for reducing inner cavity temperature；
Crystallization apparatus (6) the inner cavity temperature is 10 DEG C~30 DEG C.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109851647A (en) * | 2019-02-25 | 2019-06-07 | 涟源康麓生物科技有限公司 | The production equipment of aurantiamarin and the preparation method of aurantiamarin |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109851647A (en) * | 2019-02-25 | 2019-06-07 | 涟源康麓生物科技有限公司 | The production equipment of aurantiamarin and the preparation method of aurantiamarin |
| CN109851647B (en) * | 2019-02-25 | 2024-04-02 | 涟源康麓生物科技有限公司 | Equipment for producing hesperidin and preparation method of hesperidin |
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| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Hunan kangliyuan pectin Technology Co.,Ltd. Assignor: LIANYUAN KANGBIOTECH CO.,LTD. Contract record no.: X2023980053693 Denomination of utility model: Production equipment for hesperidin Granted publication date: 20191122 License type: Common License Record date: 20231225 Assignee: Lianyuan Orange Sweet Biotechnology Co.,Ltd. Assignor: LIANYUAN KANGBIOTECH CO.,LTD. Contract record no.: X2023980053571 Denomination of utility model: Production equipment for hesperidin Granted publication date: 20191122 License type: Common License Record date: 20231225 |
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