CN200960414Y - Device suitable for various solvents to carrying out polar and nonpolar intermediate extracting - Google Patents
Device suitable for various solvents to carrying out polar and nonpolar intermediate extracting Download PDFInfo
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- CN200960414Y CN200960414Y CN 200620135969 CN200620135969U CN200960414Y CN 200960414 Y CN200960414 Y CN 200960414Y CN 200620135969 CN200620135969 CN 200620135969 CN 200620135969 U CN200620135969 U CN 200620135969U CN 200960414 Y CN200960414 Y CN 200960414Y
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Abstract
The utility model relates to an extraction device for active ingredients in raw material of animals and plants, in particular to a constituting and connecting way of the device for polarity and non-polarity middle-body extraction with a plurality of solvents. The device is applied for a plurality of solvents to achieve the polarity and non-polarity mid-body extraction. By changing the extracting solvents and movement procedures of a valve, a pipeline and the device in the system, the requirements of extracting temperature, pressure, time, and flow direction for different solvents can be satisfied, the dissolve and diffused ability of the solvents can be accelerated, and the extraction of the active ingredients in raw material of animals and plants can be accomplished. At the same time, by changing the temperature and pressure of the mixing solution provided from extracting, the transformation between the gas and the liquid of the solvents is controlled, the separation of the solvents and the active ingredients can be accomplished, thereby solving the situation of that a device can only accomplish the extraction and the manufacture of one specific product, and the extracting technical requirements of non-polarity and polarity active ingredients can not be cared.
Description
Technical field:
The utility model relates generally to the extraction equipment of active ingredient in the animal-plant material, relates in particular to be applicable to that the multiple solvent of employing carries out the formation and the connected mode of the device of polarity, the extraction of nonpolar intermediate respectively.
Background technology:
The dissolution properties of compound in different solvents according to various components in the animal and plant raw material, according to " similar mixing " principle, select for use required active component solubility big, to not needing the little solvent of stripping composition solubility, active ingredient is dissolved out in raw tissue, resolve then and reclaim extractant, to finish extraction, to separate process.
The industrial extraction method of prior art natural materials active ingredient, the power consumption of ubiquity technology is high, and solvent-oil ratio is big, and the security of device systems is poor, the problem that environmental hazard is serious.The production technology of lipid oil particularly, great majority still adopt cold (heat) press for extracting juice, No. 6 solvent lixiviates, No. 4 methods such as solvent lixiviate, and the former oil yield is low, and loss of effective components is big; Though and the latter has than high oil recovery, the solvent that adopts is flammable and combustible liquids (or gas), and production process is absolutely unsafe, and is difficult to reach the requirement of safe handling.
Because the active ingredient in the animal-plant material is very complicated, has both had polarity active ingredient, also has low pole and nonpolar active ingredient.At the opposed polarity of target extract (solute), select the solvent of adding also inequality, be used to extract polar intermediate as ethanol, water, benzinum, ethyl acetate, CO
2Fluids etc. can only be used to extract nonpolar intermediate.Because the extractant of opposed polarity, to process conditions such as raw material granularity, extraction time, the extraction temperature of extraction, extract requirement such as pressure and have nothing in common with each other, cause traditional extraction equipment to have nothing in common with each other.Often a covering device can only be suitable for one type of extractant, carries out the extraction of multiple intermediate if desired, just must adopt many complete equipments, causes investment big, and utilization rate of equipment and installations is low.
Summary of the invention:
The purpose of this utility model is to avoid the deficiencies in the prior art part and provides a kind of and be applicable to that multiple solvent carries out the device of the nonpolar intermediate of polarity extraction.By changing the operation program of valve, pipeline, equipment in extractant and the system, satisfy the requirement of different solvents to extraction temperature, pressure, time and the flow direction, the dissolving diffusivity of accelerated solvent is finished the extraction to active ingredient in the animal-plant material; Simultaneously, by changing the temperature and pressure of extraction gained mixed solution, thereby the conversion of control solvent gas, liquid, finish separating of solvent and active ingredient, solve a kind of device thus and can only finish the extraction processing of a certain class feature product, can't take into account the situation that extraction process nonpolar, polarity active ingredient requires.
The purpose of this utility model can be by realizing by the following technical solutions: a kind ofly be applicable to that multiple solvent carries out the device of the nonpolar intermediate extraction of polarity, include storage tank (1), extractor (4a, 4b), extraction-container (9), each equipment is equipped with valve between connecting, and its main feature also includes:
(i), storage tank (1) outlet is connected with delivery pump (2a) inlet, delivery pump (2a) export with preheat exchanger (3a), extractor (4a, 4b) between be connected by pipeline, valve;
(ii), through the outlet of extractor (4a, 4b), wherein one the tunnel connects the input port, upper end of temporary jar (6) through delivery pump (2b) back; Another road is by the inlet of delivery pump (2b) back connection filter (7), through connecting the following end interface of temporary jar (6) behind the centre exit of filter (7);
(iii), the bottom delivery outlet of temporary jar (6) is connected with extraction-container (9a) inlet by pipeline with delivery pump (2c), heat exchanger (3b); The lower end outlet of extraction-container (9a) is divided into two-way, and the delivery pump (2d) of leading up to connects the last end entrance of secondary extraction-container (9b); Another road is connected with heat exchanger (3b) through the outlet of delivery pump (2d), and heat exchanger (3b), extraction-container (9a) constitute the local circulation loop;
(iv), the centre entrance of filter (7) is connected with the outlet of delivery pump (2b), the top exit end divides two-way to be connected respectively with vavuum pump (12a, 12b) inlet;
(v), extraction-container (9a, 9b) top exit is communicated with vavuum pump (12a, 12b) respectively;
(vi), extraction-container (9b) outlet at bottom is connected with " venturi " generator (16) centre entrance, " venturi " generator (16) port of export is connected with disperser (14) inlet; N
2Or CO
2Gas piping is connected with " venturi " generator (16) entrance point, and disperser (14) outlet at bottom is connected with " venturi " generator (16) centre entrance;
(vii), the last end interface of extractor (4a, 4b) is connected with sprayed tank (5), behind sprayed tank (5) the outlet process surge tank (8a), one tunnel connection vavuum pump (12a) passes through condenser (11b) then and is communicated with surge tank (8b), compressor (13a), surge tank (8c); Another road directly is communicated with surge tank (8c) inlet through compressor (13b) back;
(viii), surge tank (8c) outlet links to each other with heat exchanger (3b) import, preheat exchanger (3b) lower end exports to enter the mouth with condenser (11a) and is connected;
(ix), condenser (11a) outlet both was communicated with solvent tank (1), also entering the mouth with extractor (4a, 4b) respectively is communicated with.
Describedly be applicable to that multiple solvent carries out the device of the nonpolar intermediate of polarity extraction, the outlet that also includes entrainer jar (15) enters the mouth with delivery pump (2e) and is connected, and the outlet of delivery pump (2e) is connected with preheat exchanger (3a).
The described device that is applicable to that multiple solvent carries out the extraction of the nonpolar intermediate of polarity also includes extraction-container (9a, 9b) centre exit and is communicated with recycling can (10) respectively, top exit is communicated with vavuum pump (12a, 12b) respectively, and recycling can (10) top port is communicated with vavuum pump (12b), condenser (11b, 11c) respectively.
The described device that is applicable to that multiple solvent carries out the extraction of the nonpolar intermediate of polarity also includes storage tank (17) outlet and is connected with delivery pump (2f) inlet, delivery pump (2f) export with preheat exchanger (3a), extractor (4a, 4b) between be connected by pipeline, valve.
The utility model serves as the extraction solvent at the physicochemical characteristics of nonpolar functional group in the raw material with nonpolar SF6 solution, extracts, separates nonpolar active ingredient.(seeing the subcritical fluid extraction solvent and the extracting process of application on the same day).Also be included in add ethanol in the nonpolar SF6 extractant, acetone is entrainer, and mixed solvent is adjusted into the low pole solvent, extracts, separates low pole active ingredient.At the physicochemical characteristics of intermediate product Semi-polarity functional group, be extractant with water, ethanol, extract separating polar (water-soluble) active ingredient.
Between the different operations of the utility model extraction equipment utilization in the solvent concentration difference of active ingredient carry out " gradient " extraction, owing to be provided with two extraction kettles, so particularly preferred method is with the 3rd, 4 extraction of extraction kettle (4a) gained low concentration mixed liquor, directly inject extraction kettle (4b) and carry out its immersion of the 1st, 2 time extraction, vice versa, so that the active ingredient amount that dissolves in the raising solvent, the solvent evaporation treatment capacity of minimizing extraction-container reduces energy resource consumption.
The utility model extraction equipment effectively removes the dissolvent residual in the intermediate product: the outlet of secondary extraction-container (9b) lower end is connected with disperser (14) lower part outlet with " venturi " generator (16) centre entrance respectively, with pure gaseous state N
2Or CO
2Be diffusant, utilize " Wen Qiuli " absorption principle that liquid primary extract is mixed at " venturi " generator (16) mutually with diffusant, under the pressure of 0.5MPa, repeat to mix---injection---diffusion process, the gas diffusant carries the trace solvent of retaining in the product and discharges system, thereby the dissolvent residual in the target component is removed.
Extraction equipment is by changing extractant, change control, the connected mode of extraction parameter and extraction equipment simultaneously, thereby constitute different extraction mode of operations, extracting product is respectively nonpolar or low pole active ingredient, the extraction of also compatible polarity active ingredient.
Difference according to employed extractant, its mode of operation can be divided into two states: be extractant with nonpolar sulfur hexafluoride, HFC-134a, heptafluoro-propane, 406A and fluid-mixing thereof 1,, or be that solvent extracts with the fluid-mixing of above-mentioned solvent and ethanol, acetone, it extracts product is nonpolar or the grease of low pole and ester soluble components; 2, Yi Shui, ethanol are the traditional extraction pattern of solvent, and it extracts product is polarity (water-soluble) active ingredient.
The beneficial effects of the utility model are:
1, on a covering device, carries out the extraction production of polar solvent and non-polar solven respectively, satisfy of the multiple requirement of the intermediate product of opposed polarity extraction process.
2, design entrainer system in extraction equipment utilizes entrainer to change polarity of solvent, makes solvent and entrainer performance synergy to improve extraction efficiency.
3, make full use of the physical characteristic of non-polar solven uniqueness, make whole extraction process under relatively safer low-pressure state, to finish, the dischargeable capacity of equipment is subjected to the restriction of processing technology little, the safe performance indexes of system improves relatively, simultaneously, the technology difficulty and the construction costs of device fabrication have been reduced significantly.
4, adopt two-stage to resolve vapo(u)rization system, make extractant rapid evaporation in 10 ℃ to 50 ℃ temperature range, guarantee that solvent separates fully with solute, effectively avoid the loss and the destruction of " thermal sensitivity " composition simultaneously, preserve the activity of product active ingredient as far as possible, improve product quality.
5, reclaim, compress solvent stage by stage, the high efficiente callback solvent reduces energy resource consumption.
6, adopt the environmental friendliness material as extractant, neither destroy the build-in attribute of product, reach the purpose of protection environment again to guarantee extraction process.
7, extraction, separation both can be finished continuously, also can carry out by operation break-down, and accommodation is extensive.
8, the continuous operation under Light Condition of this device can reach the purpose of purging system; When production needs, also can adopt water or ethanol purging system inside; The automatic upper and lower materials device of this device configuration closed prevents that production process from producing excessive dust and influencing environment, alleviates working strength of workers simultaneously as far as possible; The fluid of this device is carried and is all adopted diaphragm delivery pump, and each process procedure all is in air-tight state, effectively to avoid personnel, the environment influence to product quality.
Description of drawings:
Fig. 1 is the nonpolar SF6 solvent extraction Seabuckthorm Seed Oil process principle figure of the utility model embodiment 1;
Fig. 2 is the weak polar solvent extraction tanshinone IIA process principle figure of the utility model embodiment 2;
Fig. 3 is the utility model extraction equipment process principle figure.
The specific embodiment:
Be described in further detail below in conjunction with the most preferred embodiment shown in the accompanying drawing:
Embodiment 1: see the nonpolar SF6 solvent extraction of Fig. 1 Seabuckthorm Seed Oil process principle figure, this device includes SF6 solvent tank 1, extractor 4a, 4b, and extraction-container 9, each equipment is equipped with valve between connecting, and also includes:
(1), connects and composes basic extraction cells by pipeline, valve between storage tank 1 and delivery pump 2a, preheat exchanger 3a, extractor 4a, the 4b.
(2), through the outlet of extractor 4a, 4b, wherein one the tunnel through connecting temporary jar 6 input port, upper end behind the delivery pump 2b; Another road connects temporary jar 6 following end interface by connecting the inlet of filter 7 behind the delivery pump 2b behind the process centre exit of filter 7, constitute the filtration memory cell of extract with this.
(3), temporary jar 6 bottom delivery outlet is connected with extraction-container 9a inlet by pipeline with delivery pump 2c, heat exchanger 3b; The lower end outlet of extraction-container 9a is divided into two-way, and the delivery pump 2d of leading up to connects the last end entrance of secondary extraction-container 9b; Another road is connected with heat exchanger 3b through the outlet of delivery pump 2d, and heat exchanger 3b, extraction-container 9a constitute local circulation and resolve the loop.
(4), the centre entrance of filter 7 is connected with the outlet of delivery pump 2b, the top exit end divides two-way to be connected respectively with vavuum pump 12a, 12b inlet, formation local vacuum-pumping loop.
(5), extraction-container 9a, 9b top exit are communicated with formation vacuum analysis loop respectively with vavuum pump 12a, 12b.
(6), extraction-container 9b outlet at bottom is connected with " venturi " generator 16 centre entrances, " venturi " generator 16 ports of export are connected with disperser 14 inlets; N
2Or CO
2Gas piping is connected with " venturi " generator 16 entrance points, and disperser 14 outlet at bottoms are connected with " venturi " generator 16 centre entrances, constitutes gas diffusion precipitation loop.
(7), the last end interface of extractor 4a, 4b is connected with sprayed tank 5, sprayed tank 5 outlets through surge tank 8a after, the one tunnel is communicated with surge tank 8b, compressor 13a, surge tank 8c through condenser 11b after connecting vavuum pump 12a outlet; Directly be communicated with surge tank 8c inlet behind the process compressor 13b of another road, the two-way connected mode satisfies the needs that single compressor or double-compressor reclaim solvent respectively.
(8), surge tank 8c outlet links to each other with heat exchanger 3b import, makes the heat of compression that compressor 13 work produce after heat exchange, provides the solvent parsing required heat power to extraction-container 9; Preheat exchanger 3b lower end outlet enters the mouth with condenser 11a and is connected, thereby so that solvent vapo(u)r is converted into liquid state by the gaseous state condensation is reclaimed.
(9), condenser 11a outlet both was communicated with solvent tank 1, also entering the mouth with extractor 4a, 4b respectively is communicated with, and makes condensed liquid solvent both can return storage tank, also can directly inject extractor and circulate next time.
Concrete extraction process is:
1, automatic charging machine is sent raw material into extraction kettle 4a, when the raw material volume reaches extraction kettle volume 1/3, stops material loading, closes input and output material control butterfly valve.
2, vavuum pump 12a is extraction kettle 4a vacuum drop to 1 * below the 104pa, on-condensible gas in the removal system.
3, mix with the sea-buckthorn raw material in extraction kettle 4a being in liquid sulfur hexafluoride solution in the storage tank 1, be warming up to 45 ℃-50 ℃, extracting pressure rises to more than the 3.5MPa, 40 minutes retention times, after finishing once immersion extraction, mixed solution is delivered into temporary storage kettle jar 6; Sulfur hexafluoride solution secondary input extraction kettle and raw material are mixed, and intensification pressurize 50 minutes is finished secondary and is soaked extraction; Re-extract three to four times, and with the 3rd, 4 extraction gained low concentration mixed liquor, inject extraction kettle 4b and carry out its immersion of the 1st, 2 time extraction, so that improve the active ingredient amount that dissolves in the solvent.
4, merge re-extract gained mixed liquor to temporary storage kettle 6, the extraction mixed solution in the temporary storage kettle 6 is injected one-level extraction-container 9a through high-pressure delivery pump 2c; Delivery pump 2d carries the mixed solution circulation, makes it repeatedly by heat exchanger 3b and jacketed heat exchanger heating, keeps 30 ℃-50 ℃ of system temperatures, 1 * 10
4Pa-5 * 10
-2Under the pa vacuum state, mixed solution is resolved evaporation in extraction-container 9a, finish the initial gross separation of solvent and Seabuckthorm Seed Oil.
5, resolve the mixed solution of crude separation through delivery pump 2d injection secondary extraction-container 9b, by the jacketed heat exchanger heating, 5 * 10 through one-level
-2Under the pa high vacuum state, solvent is further resolved evaporation, finishes separating fully of solvent and Seabuckthorm Seed Oil.
6, resolve the solvent that evaporation is gaseous state, go into main condenser 11a and carry out heat exchange through vavuum pump group 12a extracting, compressor bank 13a compression are laggard, return solvent tank after gaseous solvent is converted into saturated liquid.
7, continue heating extraction kettle 4a, 4b by jacketed heat exchanger, the material slag in the continuous stirred tank is 5 * 10
-2Under the pa high vacuum state, the sulfur hexafluoride solvent in the material slag is resolved evaporation, finishes the recovery fully of residual solvent in the raw material;
8, extraction obtains Seabuckthorm Seed Oil, passes through N
2Diffusion removes solvent device 16,14, removes residual sulfur hexafluoride, can obtain the seabuckthorn seeds essential oil of dissolvent residual less than 3PPm.
Embodiment 2: see Fig. 2 weak polar solvent extraction tanshinone IIA process principle figure, a kind of device that is applicable to weak polar solvent extraction tanshinone IIA, the outlet that its device includes entrainer jar 15 is connected with delivery pump 2e inlet, and the outlet of delivery pump 2e is connected with preheat exchanger 3a.Extraction-container 9a, 9b centre exit are communicated with recycling can 10 respectively, and top exit is communicated with vavuum pump 12a, 12b respectively; Recycling can 10 top port are communicated with vavuum pump 12b, condenser 11b, 11c respectively.The connected mode of all the other devices is identical with embodiment 1.
Concrete extraction process is:
1, automatic charging machine is sent salvia miltiorrhiza raw material into extraction kettle 4a, when the raw material volume reaches extraction kettle volume 1/3, stops material loading, closes input and output material control butterfly valve.
2, vavuum pump 12b is with extraction kettle vacuum drop to 1 * 10
4Below the pa, get rid of on-condensible gas in the still.
3, the equal-volume mixed liquor injection extraction kettle 4a with liquid 406A and heptafluoro-propane in the storage tank 1 mixes with salvia miltiorrhiza raw material.
4, delivery pump 2e injects extraction kettle 4a with 95% ethanolic solution in the entrainer jar 15, to change the polarity of mixed solvent.
5, heating, extraction kettle 4a is warming up to 45 ℃, and extracting pressure rises to 3.5MPa, 40 minutes retention times, finishes once to soak and extracts; Re-extract three to four times, and with the 3rd, 4 extraction gained low concentration mixed liquor, inject extraction kettle 4b and carry out its immersion of the 1st, 2 time extraction, so that improve the active ingredient amount that dissolves in the solvent; Merge the extraction mixed liquor to temporary storage kettle 6.
6, delivery pump 2c injects extraction-container 9a with the extraction mixed solution in the temporary storage kettle, and delivery pump 2d carries the extraction mixed solution repeatedly by heat exchanger 3b and jacketed heat exchanger heating, to keep resolution temperature greater than 10 ℃, 1 * 10
4Under the pa vacuum state, the 406A in the mixed solution and the fluid-mixing of heptafluoro-propane are resolved evaporation in extraction-container 9a, go into shell and tube main condenser 11a and carry out heat exchange through vavuum pump group 12a extracting, compressor bank 13a compression is laggard, return solvent tank 1 after the gaseous state mixed solvent is converted into saturated liquid.
7, resolve the mixed solution that separates through one-level and inject secondary extraction-container 9b by delivery pump 2d, by the jacketed heat exchanger heating, vavuum pump group 12b continues extracting, 5 * 10
-2Under the pa high vacuum state, the ethanol entrainer is resolved evaporation, finishes alcohol solvent through recycling can 10 condensations and reclaims, and obtains tanshinone IIA medicinal extract at the secondary extraction-container simultaneously.
8, continue heating extraction kettle 4a, 4b by jacketed heat exchanger, the material slag in the continuous stirred tank is 5 * 10
-2Under the pa high vacuum state, the 406A of material in the slag resolves with heptafluoro-propane, ethanol mixed solvent and evaporates, and finishes separating fully of raw material and solvent.
Embodiment 3 polar solvent ethanol extraction propolis flavones: its device includes storage tank 17 outlet and is connected with delivery pump 2f inlet, delivery pump 2f export with preheat exchanger 3a, extractor 4a, 4b between be connected by pipeline, valve.All the other devices are identical with embodiment 2.
Specific implementation process is:
1, " hair glue " raw material is crushed to the fragment of 1cm-2cm.
2, automatic charging machine is sent raw material into extraction kettle 4a, when the raw material volume reaches extraction kettle volume 1/6, stops material loading, closes input and output material control butterfly valve.
3,95% ethanol in the storage tank 17 is heated by preheat exchanger, inject extraction kettle 4a and mix with raw material.Control extraction kettle temperature is that 50 ℃-65 ℃, system pressure 0.1MPa are following, the extraction time is 100min-120min, finish once soak extract after, filter, separating material slag and extractant, alcohol mixed solution is delivered into the temporary storage kettle jar; Mix with the injection extraction kettle 4a of the ethanolic solution secondary in the solvent tank and with raw material, re-extract three to four times, and, inject extraction kettle 4b and carry out its immersion of the 1st, 2 time extraction, so that improve the active ingredient amount that dissolves in the solvent with the 3rd, 4 extraction gained low concentration mixed liquor; Merge the extraction mixed liquor to temporary storage kettle 6.
4, the mixed solution of temporary storage kettle 6 injects one-level extraction-container 9a by delivery pump 2c; The switching controls valve, delivery pump 2d delivers into heat exchanger 3b and jacketed heat exchanger heating repeatedly with mixed solution, at 40 ℃-60 ℃, 1 * 10
4Under the vacuum state of Pa, ethanol and mixed solution spray diffusion back and resolve evaporation in extraction-container 9a, finish separating of alcohol solvent and primary extract.
5, the mixed solution of resolving through one-level injects secondary extraction-container 9b by delivery pump 2d, is heated to 40 ℃-45 ℃ by jacketed heat exchanger, 5 * 10
-2Under the Pa high vacuum state, ethanol is further resolved evaporation, finishes separating fully of alcohol solvent and extract.
The alcohol vapour of I and II extraction-container evaporation is reclaimed after recycling can 10 condensations, and storage tank 17 is injected in transhipment.
6, collect the polarity active ingredient propolis flavone of retaining among the secondary extraction-container 9b, change subsequent handling over to and further handle.
7, continue heating extraction kettle 4a, 4b by jacketed heat exchanger, the material slag in the continuous stirred tank is 5 * 10
-2Under the Pa high vacuum state, the alcohol solvent in the material slag is resolved evaporation, is reclaimed after recycling can 10 condensations, finishes the recovery fully of alcohol solvent.
Claims (4)
1. one kind is applicable to that multiple solvent carries out the device of the nonpolar intermediate extraction of polarity, includes storage tank (1), extractor (4a, 4b), and extraction-container (9), each equipment is equipped with valve between connecting, and its feature also includes:
(i) storage tank (1) outlet is connected with delivery pump (2a) inlet, delivery pump (2a) export with preheat exchanger (3a), extractor (4a, 4b) between be connected by pipeline, valve;
(ii) through the outlet of extractor (4a, 4b), wherein one the tunnel through connecting the input port, upper end of temporary jar (6) behind the delivery pump (2b); Another road is by the inlet of delivery pump (2b) back connection filter (7), through connecting the following end interface of temporary jar (6) behind the centre exit of filter (7);
(iii) the bottom delivery outlet of temporary jar (6) is connected with extraction-container (9a) inlet by pipeline with delivery pump (2c), heat exchanger (3b); The lower end outlet of extraction-container (9a) is divided into two-way, and the delivery pump (2d) of leading up to connects the last end entrance of secondary extraction-container (9b); Another road is connected with heat exchanger (3b) through the outlet of delivery pump (2d), and heat exchanger (3b), extraction-container (9a) constitute the local circulation loop;
(iv) the centre entrance of filter (7) is connected with the outlet of delivery pump (2b), and the top exit end divides two-way to be connected respectively with vavuum pump (12a, 12b) inlet;
(v) extraction-container (9a, 9b) top exit is communicated with vavuum pump (12a, 12b) respectively;
(vi) extraction-container (9b) outlet at bottom is connected with " venturi " generator (16) centre entrance, and " venturi " generator (16) port of export is connected with disperser (14) inlet; N2 or CO2 gas piping are connected with " venturi " generator (16) entrance point, and disperser (14) outlet at bottom is connected with " venturi " generator (16) centre entrance;
(vii) the last end interface of extractor (4a, 4b) is connected with sprayed tank (5), behind sprayed tank (5) the outlet process surge tank (8a), be communicated with surge tank (8b), compressor (13a), surge tank (8c) through condenser (11b) behind one tunnel connection vavuum pump (12a); Another road directly is communicated with surge tank (8c) inlet through compressor (13b) back;
(vii) surge tank (8c) outlet links to each other with heat exchanger (3b) import, and the outlet of preheat exchanger (3b) lower end is connected with condenser (11a) inlet;
(ix) condenser (11a) outlet both was communicated with solvent tank (1), also was communicated with extractor (4a, 4b) inlet respectively.
2. as claimed in claim 1ly be applicable to that multiple solvent carries out the device of the nonpolar intermediate of polarity extraction, it is characterized in that the outlet that also includes entrainer jar (15) is connected with delivery pump (2e) inlet, the outlet of delivery pump (2e) is connected with preheat exchanger (3a).
3. as claimed in claim 1 or 2ly be applicable to that multiple solvent carries out the device of the nonpolar intermediate of polarity extraction, it is characterized in that also including extraction-container (9a, 9b) centre exit is communicated with recycling can (10) respectively, top exit is communicated with vavuum pump (12a, 12b) respectively, and recycling can (10) top port is communicated with vavuum pump (12b), condenser (11b, 11c) respectively.
4. as claimed in claim 3ly be applicable to that multiple solvent carries out the device of the nonpolar intermediate of polarity extraction, it is characterized in that also including storage tank (17) outlet and be connected with delivery pump (2f) inlet, delivery pump (2f) export with preheat exchanger (3a), extractor (4a, 4b) between be connected by pipeline, valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620135969 CN200960414Y (en) | 2006-10-11 | 2006-10-11 | Device suitable for various solvents to carrying out polar and nonpolar intermediate extracting |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200620135969 CN200960414Y (en) | 2006-10-11 | 2006-10-11 | Device suitable for various solvents to carrying out polar and nonpolar intermediate extracting |
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|---|---|
| CN200960414Y true CN200960414Y (en) | 2007-10-17 |
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| CN 200620135969 Expired - Fee Related CN200960414Y (en) | 2006-10-11 | 2006-10-11 | Device suitable for various solvents to carrying out polar and nonpolar intermediate extracting |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103398887A (en) * | 2013-08-08 | 2013-11-20 | 上海天科化工检测有限公司 | Step-by-step liquefied composite type trace extraction device |
| WO2015010551A1 (en) * | 2013-07-22 | 2015-01-29 | Cao Yong | Multifunctional continuous phase transition extraction apparatus |
| CN110255547A (en) * | 2019-07-27 | 2019-09-20 | 侯梦斌 | A kind of carbon material peel-off device and technique for intervening microwave energy |
-
2006
- 2006-10-11 CN CN 200620135969 patent/CN200960414Y/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015010551A1 (en) * | 2013-07-22 | 2015-01-29 | Cao Yong | Multifunctional continuous phase transition extraction apparatus |
| US10016700B2 (en) | 2013-07-22 | 2018-07-10 | Yong Cao | Multifunctional continuous phase transition extraction apparatus |
| CN103398887A (en) * | 2013-08-08 | 2013-11-20 | 上海天科化工检测有限公司 | Step-by-step liquefied composite type trace extraction device |
| CN103398887B (en) * | 2013-08-08 | 2016-05-25 | 上海天科化工检测有限公司 | A kind of combined type trace extraction device that liquefies step by step |
| CN110255547A (en) * | 2019-07-27 | 2019-09-20 | 侯梦斌 | A kind of carbon material peel-off device and technique for intervening microwave energy |
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