CN201312997Y - Effective ingredients extracting-separating device of natural product - Google Patents
Effective ingredients extracting-separating device of natural product Download PDFInfo
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- CN201312997Y CN201312997Y CNU200820185336XU CN200820185336U CN201312997Y CN 201312997 Y CN201312997 Y CN 201312997Y CN U200820185336X U CNU200820185336X U CN U200820185336XU CN 200820185336 U CN200820185336 U CN 200820185336U CN 201312997 Y CN201312997 Y CN 201312997Y
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Abstract
The utility model relates to an effective ingredients extracting-separating device of a natural product, which comprises an automatic control system, a continuous reverse-flow percolation extracting system, an extraction system and an extracting solution transfer pot. The continuous reverse-flow percolation extracting system comprises a first continuous reverse-flow percolation extracting machine set, a second continuous reverse-flow percolation extracting machine set and a third continuous reverse-flow percolation extracting machine set; each continuous reverse-flow percolation extracting machine set comprises a feeding pump, a heater, a reverse-flow percolation pot, a sand filter and an ultraviolet ray detector which are sequentially connected; the feeding pump is used for feeding material liquid, the reverse-flow percolation pot is used for holding plant raw materials, the ultraviolet ray detector which is connected with the automatic control system is used for detecting the content of the effective ingredients in solution output by the sand filter, and the extraction system is connected with the transfer pot. Under the function of the automatic control system, the first, second and third continuous reverse-flow percolation extracting machine sets are led to sequentially compose the first, second and third two-stage extraction, and the recycling is carried out in this way; meanwhile, the effective ingredients in the extracting solution coming from the transfer pot are continuously extracted by the extraction system.
Description
Technical field
The utility model relates to a kind of natural products effective ingredient and extracts separator.
Background technology
Chinese patent literature notification number CN2792590 discloses a kind of effective ingredients in plant and has extracted separator, it is characterized in that: include extraction cell, be connected in the sedimentation separation chamber on extraction cell top, described extraction cell has insulation jacket, the bottom is provided with slag-drip opening and extractant import, top is provided with dog-house and extracts solvent inlet, and inside is provided with rabbling mechanism; Bottom, described sedimentation separation chamber is communicated with extraction cell, and top is provided with the extract outlet and extracts the solvent recovery outlet, and the bottom is provided with remaining extractant outlet.
Chinese patent literature publication number CN1973940 discloses the method for active ingredient in a kind of continuous extraction separating plant, on choice of Solvent, the solvent of utilization a little less than to the active ingredient dissolubility, exchange the means strong for to the dopant type selectivity, mode by solvent continuous-flow is extracted continuously, again by another phase solvent or adsorbent Continuous Selection transfer active ingredient or solvent reclamation circulation extraction separation.
Chinese patent literature notification number CN2691674 discloses a kind of continuous flow upstream diacolation jar group, be characterized in: be provided with some groups and have diacolation jar, last liquid receiver, following liquid receiver, barometric pipe, the continuous diacolation device that connects into by the control valve infusion pipeline, line up order, wherein the liquid outlet of the following liquid receiver of each group links to each other with two groups the inlet of last liquid receiver in addition that is arranged in order by pump and control valve infusion pipeline, constitute continuous flow upstream diacolation jar group, be equivalent to every group of diacolation stroke stack.
Above-mentioned prior art has following weak point: existing effective ingredients in plant extraction system can not realize the function of real continuous extraction extraction, and production efficiency is lower, production cost is higher and complicated operating process.
The utility model content
Technical problem to be solved in the utility model provides a kind of natural products effective ingredient and extracts separator, with when the active ingredient of plant is extracted continuously, carries out continuous extraction, thereby enhances productivity greatly.
For solving the problems of the technologies described above, the technical solution adopted in the utility model provides a kind of natural products effective ingredient and extracts separator, it comprises: automatic control system, continuous flow upstream diacolation extraction system, extracting system and extract transfer jar, continuous flow upstream diacolation extraction system comprises that three groups of adverse current diacolations extract unit, that is: the first adverse current diacolation extracts unit, the second adverse current diacolation extracts unit and the 3rd adverse current diacolation extracts unit; Each adverse current diacolation extracts unit and comprises: successively the feed pump that is used for sending into feed liquid of Xiang Lianing, heater, be used to hold adverse current diacolation jar, the sand filter of plant material and link to each other with automatic control system be used to detect the ultraviolet detector of exporting the active constituent content of solution by sand filter; Ultraviolet detector can realize that the on-line synchronous of active ingredient in the continuous flow upstream percolate detects.Extracting system links to each other with the transfer jar.
Under the effect of automatic control system, open the described first adverse current diacolation and extract unit and second adverse current diacolation extraction unit, close described the 3rd adverse current diacolation simultaneously and extract unit, at this moment, the extract of the first adverse current diacolation jar output in the first adverse current diacolation extraction unit is sent into the second stream diacolation jar in the second adverse current diacolation extraction unit, the extract of the second stream diacolation jar output is sent into extract transfer jar, that is: first adverse current diacolation extraction unit and second adverse current diacolation extraction unit constitute the extraction of first two-stage successively, also are that continuous flow upstream diacolation extraction system is in first two-stage extraction state;
When the concentration that records the active ingredient in the extract of first adverse current diacolation jar output by described ultraviolet detector when automatic control system is lower than preset value, closes the described first adverse current diacolation and extract unit, and open described the 3rd adverse current diacolation and extract unit; At this moment, the extract of the described second stream diacolation jar output is sent into the 3rd adverse current diacolation jar in the 3rd adverse current diacolation extraction unit, the extract of the 3rd stream diacolation jar output is sent into extract transfer jar, that is: second adverse current diacolation extraction unit and the 3rd adverse current diacolation extraction unit constitute the extraction of second two-stage successively, also are that continuous flow upstream diacolation extraction system is in second two-stage extraction state;
When the concentration that records the active ingredient in the extract of the second stream diacolation jar output by described ultraviolet detector when automatic control system is lower than preset value, closes the described second adverse current diacolation and extract unit, and open the described first adverse current diacolation and extract unit; At this moment, the extract of the 3rd stream diacolation jar output is sent into the described first adverse current diacolation jar, the extract of first adverse current diacolation jar output is sent into extract transfer jar, that is: the 3rd adverse current diacolation extraction unit and first adverse current diacolation extraction unit constitute the extraction of the 3rd two-stage successively, also are that continuous flow upstream diacolation extraction system is in the 3rd two-stage extraction state;
When automatic control system records active ingredient in the extract of the 3rd stream diacolation jar output and is lower than preset value by described ultraviolet detector, make continuous flow upstream diacolation extraction system be in described first two-stage and extract state, circulation so repeatedly;
Simultaneously, the extracting system continuous extraction is from the active ingredient in the extract of transfer jar.
For guaranteeing continuous production, in technique scheme, also comprise the material-compound tank that is used to prepare described feed liquid; Be connected with liquid valve and feed liquid transfer jar on the liquid outlet of material-compound tank in turn, the liquid outlet of feed liquid transfer jar links to each other with the inlet of described each feed pump, the liquid outlet of each feed pump links to each other with the inlet of described each heater respectively, the liquid outlet of each heater links to each other with the inlet of described each adverse current diacolation pot bottom respectively, the liquid outlet of each adverse current diacolation tank top links to each other with the inlet of described each sand filter respectively, the liquid outlet of each sand filter is connected with ultraviolet detector, the liquid outlet of each ultraviolet detector in parallel with the liquid outlet of each adverse current diacolation jar respectively and through in rotary valve link to each other with the inlet of extract transfer jar.
The utlity model has positive effect: (1) the utility model natural products effective ingredient is extracted in the separator, three groups of adverse current diacolations extract unit and are circulated in first two-stage extraction state, second two-stage extraction state and the 3rd two-stage extraction state all the time successively, wherein, when second two-stage is extracted, send the remaining feed liquid in the first adverse current diacolation jar back to feed liquid transfer jar (but also emptying), and the raw material that more renews; When the 3rd two-stage is extracted, send the remaining feed liquid in the second adverse current diacolation jar back to feed liquid transfer jar (but also emptying), and the raw material that more renews; When first two-stage is extracted, send the remaining feed liquid in the 3rd adverse current diacolation jar back to feed liquid transfer jar (but also emptying), and the raw material that more renews; So circulation has realized the continuous extraction to effective ingredients in plant repeatedly, carries out continuous extraction by extracting system simultaneously, so improved production efficiency greatly.
Description of drawings
Fig. 1 is the structural representation that the natural products effective ingredient among the embodiment is extracted material-compound tank, feed liquid transfer jar and first adverse current diacolation extraction unit etc. in the separator;
Fig. 2 is that the natural products effective ingredient among the embodiment is extracted the second adverse current diacolation in the separator and extracted the structural representation that unit and the 3rd adverse current diacolation extract unit etc.;
Fig. 3 is the structural representation that the natural products effective ingredient among the embodiment is extracted the 5th heater in the first extraction unit and first extraction tower etc. in the separator;
Fig. 4 is the structural representation that the natural products effective ingredient among the embodiment is extracted first rotary film evaporator in the first extraction unit, first gas-liquid separator, first condenser etc. in the separator;
Fig. 5 is the structural representation that the natural products effective ingredient among the embodiment is extracted the second extraction unit, one-level recovery transfer jar and secondary recovery transfer jar etc. in the separator;
Fig. 6 is the structural representation that the natural products effective ingredient among the embodiment is extracted the automatic control system in the separator.
The specific embodiment
(embodiment 1)
See Fig. 1-6, the natural products effective ingredient of present embodiment is extracted separator and is comprised: material-compound tank 1, automatic control system, continuous flow upstream diacolation extraction system, extracting system and the extract transfer jar 8 of preparation feed liquid.
See Fig. 1-2, continuous flow upstream diacolation extraction system comprises that three groups of adverse current diacolations extract unit, that is: the first adverse current diacolation extracts unit, the second adverse current diacolation extracts unit and the 3rd adverse current diacolation extracts unit; Each adverse current diacolation extracts unit and comprises: successively the feed pump that is used to send into feed liquid of Xiang Lianing, with vapours as the heater of thermal source, the sand filter that is used to hold the adverse current diacolation jar of plant material and is used for impurity screening, and link to each other with automatic control system be used for detecting the ultraviolet detector that sand filter is exported the active constituent content of solution.Each extracts and is respectively equipped with the first sand filter pump 6I, the second sand filter pump 6II and the 3rd sand filter pump 6III between adverse current diacolation jar and each sand filter.
Be connected with liquid valve 1-1 and feed liquid transfer jar 2 on the liquid outlet of material-compound tank 1 in turn, the liquid outlet of feed liquid transfer jar 2 links to each other with the inlet of described each feed pump, the liquid outlet of each feed pump links to each other with the inlet of described each heater respectively, the liquid outlet of each heater links to each other with the inlet of described each adverse current diacolation pot bottom respectively, the liquid outlet of each adverse current diacolation tank top links to each other with the inlet of described each sand filter respectively, and rotary valve (comprising: rotary valve 22I in first in the liquid outlet warp of each adverse current diacolation jar, rotary valve 22III among the rotary valve 22II and the 3rd in second) links to each other with the inlet of extract transfer jar 8.
The raffinate outlet of each adverse current diacolation jar reclaims inlet through a control valve with the feed liquid of feed liquid transfer jar 2 respectively and links to each other.
The liquid outlet that the described first adverse current diacolation extracts the first adverse current diacolation jar 5I in the unit links to each other with the inlet that the described second adverse current diacolation extracts the secondary heater 4II in the unit through the first control valve 19I, the liquid outlet of the described second stream diacolation jar 5II links to each other with the inlet that described the 3rd adverse current diacolation extracts the 3rd heater 4III in the unit through the second control valve 19II, and the liquid outlet of the 3rd adverse current diacolation jar 5III links to each other with the inlet that the described first adverse current diacolation extracts the primary heater 4I in the unit through the 3rd control valve 19III.
The liquid outlet that the described first adverse current diacolation extracts the first sand filter 7I in the unit links to each other with the inlet that the described second adverse current diacolation extracts the secondary heater 4II in the unit through the first ultraviolet detector 29I, the liquid outlet that the described second adverse current diacolation extracts the second sand filter 7II in the unit links to each other with the inlet of described the 3rd heater 4III through the second ultraviolet detector 29II, and the liquid outlet that described the 3rd adverse current diacolation extracts the 3rd sand filter 7III in the unit links to each other with the inlet of described primary heater 4I through the 3rd ultraviolet detector 29III.
Described extracting system comprises the first extraction unit and the second extraction unit; The first extraction unit comprises: the first extraction tower 10I, the first rotary film evaporator 11I, first cooler 16 and the one-level that adopt the spacer mode of heating to heat reclaim transfer jar 13; The second extraction unit comprises: the second extraction tower 10II, the second rotary film evaporator 11II, second cooler 17 and the secondary recovery transfer jar 15 that adopt the spacer mode of heating to heat.
See Fig. 2-4, be connected with the 4th material pump 3IV and the 5th heater 9 on the liquid outlet of extract transfer jar 8 in turn, the liquid outlet of the 5th heater 9 links to each other with the extract inlet of the first extraction tower 10I, the outlet at the first extraction tower 10I top links to each other with the inlet of the first rotary film evaporator 11I, is connected with the first gas-liquid separator 11I-1, the first condenser 11I-2 and first cooler 16 on the venthole of the first rotary film evaporator 11I in turn; The liquid outlet of first cooler 16 links to each other with the inlet that one-level reclaims transfer jar 13.
See Fig. 3 and 5, the heavy liquid exit of first extraction tower 10I bottom links to each other with the inlet of the second extraction tower 10II through the 5th material pump 3V, the purified liquor outlet at the second extraction tower 10II top links to each other with the inlet of the second rotary film evaporator 11II, is connected with second gas-liquid separator, second condenser and second cooler 17 on the venthole of the second rotary film evaporator 11II in turn; The liquid outlet of second cooler 17 links to each other with the inlet of secondary recovery transfer jar 15; The heavy liquid exit of second extraction tower 10II bottom links to each other with the inlet of described feed liquid transfer jar 2 through the 7th material pump 3VII.
The liquid outlet that described one-level reclaims transfer jar 13 links to each other with the colvent inlet of the first extraction tower 10I with the 6th heater 12 through the 6th material pump 3VI; The liquid outlet of secondary recovery transfer jar 15 links to each other with the colvent inlet of the second extraction tower 10II with the 7th heater 14 through the 8th material pump 3VIII.
Described automatic control system comprises: program logic controller PLC21, the ultraviolet detector that links to each other with PLC21, link to each other with PLC21 be used to control the frequency-variable controller 20 that described three groups of adverse current diacolations extract the duty of unit and extracting system; PLC21 links to each other with the control signal input of described liquid valve 1-1, middle rotary valve, the first control valve 19I, the second control valve 19II, the 3rd control valve 19III, each ultraviolet detector 29I, 29II, 29III.Frequency-variable controller 20 links to each other with second power end that extracts the main motor in the unit with the described first extraction unit, links to each other with described each feed pump (comprising: the first feed pump 3I, the first feed pump 3II and the 3rd feed pump 3III), the 4th material pump 3IV, the 5th material pump 3V, the 6th material pump 3VI, the 7th material pump 3VII simultaneously.
Before beginning effective ingredients in plant extracted and extract, earlier the feed liquid that is prepared by solvent and fresh water (FW) etc. in the material-compound tank 1 is sent into feed liquid transfer jar 2, in described each adverse current diacolation jar, drop into quantitative plant material simultaneously.
Automatic control system opens described first adverse current diacolation extraction unit and second adverse current diacolation extraction unit (is promptly opened the first feed pump 3I, steam valve on the primary heater 4I, the first control valve 19I, steam valve on the secondary heater 4II, the second stream diacolation jar 5II, rotary valve 22II in second, pump 6I, the first sand filter 7I, the first ultraviolet detector 29I, close the first control valve 19I, the second control valve 19II), close described the 3rd adverse current diacolation simultaneously and extract unit, after feed liquid in the described feed liquid transfer jar 2 is delivered to primary heater 4I preheating by the first feed pump 3I, enter the first adverse current diacolation jar 5I, the extract of the liquid outlet output of the first adverse current diacolation jar 5I enters described secondary heater 4II through the first control valve 19I, enters the second stream diacolation jar 5II after the heating; Extract rotary valve 22II in second of the liquid outlet output of the second stream diacolation jar 5II sends into extract transfer jar 8, and this moment, described continuous flow upstream diacolation extraction system was in first two-stage extraction state.
Described each heater is a coiled, and its heating-up temperature can be provided by vapours.
When the concentration that records the active ingredient in the extract of first adverse current diacolation jar 5I output by described ultraviolet detector as the PLC21 in the automatic control system is lower than preset value, close described first adverse current diacolation extraction unit and (promptly close the first feed pump 3I, steam valve on the primary heater 4I, the first control valve 19I, the first sand filter pump 6I, the first sand filter 7I, the first ultraviolet detector 29I), and open described the 3rd adverse current diacolation and extract unit, the described second adverse current diacolation extracts unit and remains on opening (at this moment promptly: the second feed pump 3II, steam valve on the secondary heater 4II, the second control valve 19II, steam valve on the 3rd heater 4III), open rotary valve 22III in the 3rd, the second sand filter pump 6II, the second sand filter 7II, the second ultraviolet detector V closes the second control valve 19II, rotary valve 22III in the 3rd.At this moment, the extract of the described second stream diacolation jar 5II output is sent into the 3rd adverse current diacolation jar 5III in the 3rd adverse current diacolation extraction unit, extract rotary valve 22III in the 3rd of the 3rd stream diacolation jar 5III output sends into extract transfer jar 8, that is: second adverse current diacolation extraction unit and the 3rd adverse current diacolation extraction unit constitute the extraction of second two-stage successively.Open the residual liquid discharge valve of the first adverse current diacolation jar 5I simultaneously, make raffinate be back to transfer jar 2, treat that raffinate drains, open the pneumatic slag door of diacolation jar 5I deslagging, drop into new plant material.
When the concentration that records the active ingredient in the extract of the second stream diacolation jar 5II output by described ultraviolet detector as the PLC21 in the automatic control system is lower than preset value, closing described second adverse current diacolation extraction unit (promptly closes: the described second feed pump 3II, steam valve on the secondary heater 4II, the second control valve 19II, the second sand filter pump 6II, the second sand filter 7II, the second ultraviolet detector 29II, rotary valve 22III in the 3rd), and open the described first adverse current diacolation and extract unit, described the 3rd adverse current diacolation extracts unit and remains on opening (at this moment promptly: the 3rd feed pump 3III, steam valve on the 3rd heater 4III, the 3rd sand filter pump 6III, the 3rd sand filter 7III, the 3rd ultraviolet detector 29III), open the 3rd control valve 19III simultaneously, close rotary valve 22III in the 3rd, at this moment, the extract of the 3rd stream diacolation jar 5III output is sent into the described first adverse current diacolation jar 5I, extract rotary valve 22I in first of first adverse current diacolation jar 5I output sends into extract transfer jar 8, that is: the 3rd adverse current diacolation extraction unit and first adverse current diacolation extraction unit constitute the extraction of the 3rd two-stage successively.
When automatic control system records active ingredient in the extract of the 3rd stream diacolation jar 5III output and is lower than preset value by described ultraviolet detector, make continuous flow upstream diacolation extraction system be in described first two-stage and extract state, circulation so repeatedly.
Simultaneously, the extracting system continuous extraction is from the active ingredient in the extract of transfer jar 8.
Under the control of automatic control system, the solvent that one-level reclaims in transfer jar 13 and the secondary recovery transfer jar 15 enters the first extraction tower 10I and the second extraction tower 10II through heating, is full of this two extraction towers until solvent; By the 4th material pump 3IV the extract in the extract transfer jar 8 is entered the first extraction tower 10I after 9 heating of the 5th heater; (for example: the solvent that contains lipid) enter the first rotary film evaporator 11I, the heavy-fluid of exporting from the heavy liquid exit of the first extraction tower 10I enters the second extraction tower 10II to the clear liquid of the purified liquor outlet output at the first extraction tower 10I top; In addition, (for example: lipid) and from the products export of its bottom export after concentrating, the first rotary film evaporator 11I gets a component, isolated solvent enters one-level successively and reclaims transfer jar 13 after the first gas-liquid separator 11I-1, the first condenser 11I-2 and 16 coolings of first cooler, and send into the first extraction tower 10I through described the 6th material pump 3VI and the 6th heater 12, use with recovery set; The clear liquid of the purified liquor outlet output at the second extraction tower 10II top enters the second rotary film evaporator 11II, and heavy-fluid is returned into transfer jar 2 again from the heavy liquid exit of its bottom, uses with recovery set; In addition, (for example: flavonoids) and from the products export of its bottom export after concentrating, rotary film evaporator 11II gets two components, isolated solvent enters secondary transfer jar 15 successively after second gas-liquid separator, second condenser and the cooling of second cooler, and send into the second extraction tower 10II through described the 8th material pump 3VIII and the 7th heater 14, use with recovery set; The heavy-fluid of the heavy liquid exit of the second extraction tower 10II is sent into feed liquid transfer jar 2 through the 7th material pump 3VII, uses with recovery set.
Among the figure, LICS is that liquid level indication control interlock, LT are that liquid level temperature-detecting device, LI are that level instruction device, FI are that indicator for flow rate, PI are that pressure-indication means, AECS are that analyzing and testing control interlock, TI are that temperature indicating device, TIC are that temperature indication control device, TT temperature conveyer, PIC are that pressure indication control device, FIC are that flow indication control device, LT are that liquid level conveyer, LIC are liquid level indication control device.
Claims (7)
1, a kind of natural products effective ingredient is extracted separator, it is characterized in that comprising: automatic control system, continuous flow upstream diacolation extraction system, extracting system and extract transfer jar (8); Continuous flow upstream diacolation extraction system comprises that three groups of adverse current diacolations extract unit, that is: the first adverse current diacolation extracts unit, the second adverse current diacolation extracts unit and the 3rd adverse current diacolation extracts unit; Each adverse current diacolation extracts unit and comprises: successively the feed pump that is used for sending into feed liquid of Xiang Lianing, heater, be used to hold adverse current diacolation jar, the sand filter of plant material and link to each other with automatic control system be used to detect the ultraviolet detector of exporting the active constituent content of solution by sand filter; Extracting system links to each other with transfer jar (8).
2, natural products effective ingredient according to claim 1 is extracted separator, it is characterized in that: also comprise the material-compound tank (1) that is used to prepare described feed liquid; Be connected with liquid valve (1-1) and feed liquid transfer jar (2) on the liquid outlet of material-compound tank (1) in turn, the liquid outlet of feed liquid transfer jar (2) links to each other with the inlet of described each feed pump, the liquid outlet of each feed pump links to each other with the inlet of described each heater respectively, the liquid outlet of each heater links to each other with the inlet of described each adverse current diacolation pot bottom respectively, the liquid outlet of each adverse current diacolation tank top links to each other with the inlet of described each sand filter respectively, the liquid outlet of each sand filter is connected with ultraviolet detector, the liquid outlet of each ultraviolet detector in parallel with the liquid outlet of each adverse current diacolation jar respectively and through in rotary valve link to each other with the inlet of extract transfer jar (8).
3, natural products effective ingredient according to claim 2 is extracted separator, it is characterized in that: the liquid outlet of the described first adverse current diacolation jar (5I) links to each other with the inlet that the described second adverse current diacolation extracts the secondary heater (4II) in the unit through first control valve (19I), the liquid outlet of the described second adverse current diacolation jar (5II) links to each other with the inlet that described the 3rd adverse current diacolation extracts the 3rd heater (4III) in the unit through second control valve (19II), and the liquid outlet of the 3rd adverse current diacolation jar (5III) links to each other with the inlet that the described first adverse current diacolation extracts the primary heater (4I) in the unit through the 3rd control valve (19III).
4, natural products effective ingredient according to claim 3 is extracted separator, it is characterized in that: the liquid outlet that the described first adverse current diacolation extracts first sand filter (7I) in the unit links to each other with the inlet of first ultraviolet detector (29I), the liquid outlet of first ultraviolet detector (29I) links to each other with the inlet of described secondary heater (4II), the liquid outlet that the described second adverse current diacolation extracts second sand filter (7II) in the unit links to each other with the inlet of second ultraviolet detector (29II), the liquid outlet of second ultraviolet detector (29II) links to each other with the inlet of described the 3rd heater (4III), the liquid outlet that described the 3rd adverse current diacolation extracts the 3rd sand filter (7III) in the unit links to each other with the inlet of the 3rd ultraviolet detector (29III), and the liquid outlet of the 3rd ultraviolet detector (29III) links to each other with the inlet of described primary heater (4I).
5, extract separator according to the described natural products effective ingredient of one of claim 1-4, it is characterized in that: described extracting system comprises the first extraction unit; The first extraction unit comprises: first extraction tower (10I), first rotary film evaporator (11I), first cooler (16) and one-level reclaim transfer jar (13); Be connected with the 4th material pump (3IV) and the 5th heater (9) on the liquid outlet of extract transfer jar (8) in turn, the liquid outlet of the 5th heater (9) links to each other with the extract inlet of first extraction tower (10I), the purified liquor outlet at first extraction tower (10I) top links to each other with the inlet of first rotary film evaporator (11I), and the indirect steam outlet of first rotary film evaporator (11I) is connected with gas-liquid separator (11I-1), first condenser (11I-2) and first cooler (16) in turn; The liquid outlet of first cooler (16) links to each other with the inlet that one-level reclaims transfer jar (13).
6, natural products effective ingredient according to claim 5 is extracted separator, it is characterized in that: extracting system also comprises the second extraction unit, and the second extraction unit comprises: second extraction tower (10II), second rotary film evaporator (11II), second cooler (17) and secondary recovery transfer jar (15); The heavy liquid exit of first extraction tower (10I) bottom links to each other with the inlet of second extraction tower (10II) through the 5th material pump (3V), the purified liquor outlet at second extraction tower (10II) top links to each other with the inlet of second rotary film evaporator (11II), is connected with second gas-liquid separator, second condenser and second cooler (17) on the liquid outlet of second rotary film evaporator (11II) in turn; The liquid outlet of second cooler (17) links to each other with the inlet of secondary recovery transfer jar (15); The heavy liquid exit of second extraction tower (10II) bottom links to each other with the inlet of feed liquid transfer jar (2) through the 7th material pump (3V II).
7, natural products effective ingredient according to claim 6 is extracted separator, it is characterized in that: the liquid outlet that described one-level reclaims transfer jar (13) links to each other with the colvent inlet of the 6th heater (12) with first extraction tower (10I) through the 6th material pump (3VI); The liquid outlet of secondary recovery transfer jar (15) links to each other with the colvent inlet of the 7th heater (14) with second extraction tower (10II) through the 8th material pump (3VIII).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU200820185336XU CN201312997Y (en) | 2008-09-27 | 2008-09-27 | Effective ingredients extracting-separating device of natural product |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU200820185336XU CN201312997Y (en) | 2008-09-27 | 2008-09-27 | Effective ingredients extracting-separating device of natural product |
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| CN201312997Y true CN201312997Y (en) | 2009-09-23 |
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| CNU200820185336XU Expired - Fee Related CN201312997Y (en) | 2008-09-27 | 2008-09-27 | Effective ingredients extracting-separating device of natural product |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101748038B (en) * | 2009-12-30 | 2012-07-25 | 广东顺德酒厂有限公司 | Method for percolating and aging white spirit |
| CN102772912A (en) * | 2012-07-05 | 2012-11-14 | 西安鸿生生物技术有限公司 | Device and method for extracting effective components from natural plant by high-pressure spraying reverse-flow process |
-
2008
- 2008-09-27 CN CNU200820185336XU patent/CN201312997Y/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101748038B (en) * | 2009-12-30 | 2012-07-25 | 广东顺德酒厂有限公司 | Method for percolating and aging white spirit |
| CN102772912A (en) * | 2012-07-05 | 2012-11-14 | 西安鸿生生物技术有限公司 | Device and method for extracting effective components from natural plant by high-pressure spraying reverse-flow process |
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