CN105498275A - Low-cost low-energy-consumption CO2 supercritical extraction device and process - Google Patents
Low-cost low-energy-consumption CO2 supercritical extraction device and process Download PDFInfo
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- CN105498275A CN105498275A CN201510868689.4A CN201510868689A CN105498275A CN 105498275 A CN105498275 A CN 105498275A CN 201510868689 A CN201510868689 A CN 201510868689A CN 105498275 A CN105498275 A CN 105498275A
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- tank
- barrier film
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- 238000000194 supercritical-fluid extraction Methods 0.000 title claims abstract description 16
- 238000000034 method Methods 0.000 title claims abstract description 14
- 238000005265 energy consumption Methods 0.000 title abstract description 7
- 239000002775 capsule Substances 0.000 claims abstract description 72
- 239000010720 hydraulic oil Substances 0.000 claims abstract description 27
- 238000003860 storage Methods 0.000 claims abstract description 17
- 230000004888 barrier function Effects 0.000 claims description 60
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 27
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 13
- 239000001569 carbon dioxide Substances 0.000 claims description 13
- 230000003068 static effect Effects 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 8
- 239000002994 raw material Substances 0.000 claims description 7
- 238000005086 pumping Methods 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 230000009466 transformation Effects 0.000 claims description 3
- 238000000605 extraction Methods 0.000 abstract description 10
- 238000000926 separation method Methods 0.000 abstract description 3
- 239000007788 liquid Substances 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 4
- 238000004040 coloring Methods 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000029058 respiratory gaseous exchange Effects 0.000 description 2
- GLWKVDXAQHCAIO-REYDXQAISA-N 3-[(2z,5z)-2-[[3-(2-carboxyethyl)-5-[[(2r)-4-ethenyl-3-methyl-5-oxo-1,2-dihydropyrrol-2-yl]methyl]-4-methyl-1h-pyrrol-2-yl]methylidene]-5-[[(3z,4r)-3-ethylidene-4-methyl-5-oxopyrrol-2-yl]methylidene]-4-methylpyrrol-3-yl]propanoic acid Chemical compound C\C=C1\[C@@H](C)C(=O)N=C1\C=C(/N\1)C(C)=C(CCC(O)=O)C/1=C/C1=C(CCC(O)=O)C(C)=C(C[C@@H]2C(=C(C=C)C(=O)N2)C)N1 GLWKVDXAQHCAIO-REYDXQAISA-N 0.000 description 1
- IGJXAXFFKKRFKU-UHFFFAOYSA-N Phycoerythrobilin Natural products CC=C/1C(NC(C1C)=O)=Cc2[nH]c(C=C3/N=C(CC4NC(=O)C(=C4C)C=C)C(=C3CCC(=O)O)C)c(CCC(=O)O)c2C IGJXAXFFKKRFKU-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 238000003913 materials processing Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 108010012759 phycoerythrobilin Proteins 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 229920002379 silicone rubber Polymers 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000341 volatile oil Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/0203—Solvent extraction of solids with a supercritical fluid
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/02—Solvent extraction of solids
- B01D11/0207—Control systems
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Automation & Control Theory (AREA)
- Extraction Or Liquid Replacement (AREA)
- Apparatus For Making Beverages (AREA)
Abstract
The invention relates to a low-cost low-energy-consumption CO2 supercritical extraction device and process. The low-cost low-energy-consumption CO2 supercritical extraction device comprises a CO2 storage tank, a charging bucket, an extraction tank and a separation tank, wherein the CO2 storage tank is communicated with a diaphragm capsule A in a hydraulic diaphragm tank A by a pipeline; the diaphragm capsule A in the hydraulic diaphragm tank A is communicated with the extraction tank by a pipeline; the extraction tank is communicated with a diaphragm capsule B in a hydraulic diaphragm tank B by a pipeline; the diaphragm capsule B in the hydraulic diaphragm tank B is communicated with the separation tank by a pipeline; an annular cavity between the diaphragm capsule A and the hydraulic diaphragm tank A is filled with hydraulic oil; an annular cavity between the diaphragm capsule B and the hydraulic diaphragm tank B is filled with hydraulic oil. According to the application, the energy consumption of the CO2 extraction process is reduced, the equipment cost is lowered and the application range of the process is broadened.
Description
Technical field:
The present invention relates to carbon dioxide supercritical extraction device and technology field, specifically relate to a kind of low cost low power consuming carbon dioxide supercritical extraction device and technique.
Technical background:
CO
2the existing history for many years of discovery of extraction theory and method, it utilizes CO
2gas, entering supercriticality more than when 7.32MPa pressure and more than 31.3 DEG C, has the double grading of gas and liquid, greatly improves nature major part lipid material solubility, and pressure more high-dissolvability is larger.Solute is separated out when pressure decreases, completes extraction.Due to CO
2extract nontoxic, pollution-free, do not destroy solute physicochemical characteristics without high temperature, so be widely used in Chinese medicine, natural colouring matter, natural essential oil processing refine in.
Due to CO
2in extraction process, first want CO
2make super-low liquid (-30 DEG C), then use special high-pressure pump to low temperature CO
2pressurization.Produce CO
2consume energy during cryogenic liquid huge.The equipment costs such as refrigeration machine, heat exchanger, high-pressure pump are high.For above-mentioned reasons, current CO
2extraction process only uses, as natural colouring matter, hot phycoerythrobilin and precious Chinese medicine and nutriment in very high value material refining.
Summary of the invention:
In order to solve the technical problem existed in background technology, the application provides a kind of low cost low power consuming carbon dioxide supercritical extraction device and technique, and the application can make CO
2extraction process reduces energy consumption, reduces equipment cost, widens this process application scope.
The technical solution used in the present invention is: a kind of low cost low power consuming carbon dioxide supercritical extraction device comprises CO
2storage tank, batch can, extractor and knockout drum, described CO
2storage tank is communicated with the barrier film capsules A in hydraulic diaphragm tank A by pipeline, barrier film capsules A in hydraulic diaphragm tank A is communicated with extractor by pipeline, extractor is communicated with the barrier film capsule B in hydraulic diaphragm tank B by pipeline, barrier film capsule B in hydraulic diaphragm tank B is communicated with knockout drum by pipeline, be filled with hydraulic oil in ring cavity between described barrier film capsule and hydraulic diaphragm tank A, in the ring cavity between described barrier film capsule B and hydraulic diaphragm tank B, be filled with hydraulic oil.
In such scheme, hydraulic diaphragm tank A bottom face is provided with electronic weight instrument, and hydraulic diaphragm tank A bottom has pipeline to be communicated with electric control reversing valve.The bottom of hydraulic diaphragm tank B has pipeline to be communicated with electric control reversing valve, and electric control reversing valve has pipeline to be communicated with the port of export with hydraulic pump arrival end respectively.Pipeline between extractor and hydraulic diaphragm tank B is provided with electrically-controlled valve A, the pipeline between hydraulic diaphragm tank B and knockout drum is provided with electrically-controlled valve B.Electrically-controlled valve A, electrically-controlled valve B, electric control reversing valve and electronic weight instrument are communicated with electronic controller respectively and are controlled by electronic controller.
A kind of low cost low power consuming carbon dioxide supercritical extraction technique: hydraulic diaphragm tank A, check valve, electronic weight instrument, electric control reversing valve, hydraulic pump composition CO
2hydraulic diaphragm pumping system, by this system CO
2the low pressure CO of 6 ~ 7MPa in storage tank
2boosting enters static mixer, meanwhile, is extracted raw material and enters static mixer by batch can through feed pump, feed check valve, under the effect of static mixer, and high pressure CO
2fully mix with raw material, make CO
2at utmost dissolve solute.Mixture enters after in extractor, carries the CO of solute
2enter the barrier film capsule B in hydraulic diaphragm tank B through electrically-controlled valve A, because hydraulic diaphragm tank B is communicated with hydraulic diaphragm tank A with electric control reversing valve, hydraulic pump, hydraulic oil flows back and forth between hydraulic diaphragm tank B and hydraulic diaphragm tank A.When hydraulic oil flows from hydraulic diaphragm tank B to hydraulic diaphragm tank A, barrier film capsules A pressurized, interior middle CO
2boosting, electrically-controlled valve A opens simultaneously, the high pressure CO of band solute
2enter in the capsule of hydraulic diaphragm tank B, and drive hydraulic oil to enter hydraulic diaphragm tank A.Now the inlet pressure of hydraulic pump is higher than outlet pressure.Electrically-controlled valve A closedown afterwards, electrically-controlled valve B are also closed conditions, and along with hydraulic pump is to hydraulic diaphragm tank A pump liquid, in hydraulic diaphragm tank B, pressure reduces, and in hydraulic diaphragm tank A, pressure continues to raise also CO
2extrude.When the barrier film capsules A volume in hydraulic diaphragm tank A reaches preset lower limit, electronic weight instrument output voltage, through electronic controller, electric control reversing valve is commutated, hydraulic oil flows to hydraulic diaphragm tank B from hydraulic diaphragm tank A, electrically-controlled valve B is opened, the CO containing solute in the barrier film capsule B in hydraulic diaphragm tank B simultaneously
2press-in knockout drum, now, because hydraulic oil flows to hydraulic diaphragm tank B from hydraulic diaphragm tank A, in hydraulic diaphragm tank A, pressure reduces, CO
2storage tank mesolow CO
2in the barrier film capsules A that check valve enters in hydraulic diaphragm tank A, electronic weighing instrument 4 output voltage when barrier film capsules A volume reaches higher limit, makes electric control reversing valve commutate through electronic controller and repeats above-mentioned steps.
In such scheme, the volume of hydraulic diaphragm tank A is 1/5 ~ 1/7 of extractor volume, and the maximum non-telescope volume of barrier film capsules A is 80% ~ 90% of hydraulic diaphragm tank A volume, and the minimum volume of barrier film capsules A is 10% ~ 15% of hydraulic diaphragm tank A volume.The withstand voltage twice for outlet maximum pressure of hydraulic diaphragm tank A.Hydraulic pump conversion time is barrier film capsules A transformation period between maximum volume and minimum volume is 1 ~ 3 minute, and the maximum output pressure of hydraulic pump 15 is CO
2export 1.5 times of maximum pressure.
The beneficial effect that the present invention has is: the application adopts hydraulic diaphragm pumping system to CO
2the pressure that adds high pressure reaches 20MPa ~ 40MPa, need not make super-low liquid during pressurization, CO after being directly separated solute
2(7.32MPa, about 31.3 DEG C) pressurize, and can save CO
2the expensive device of ultralow temperature (-30 DEG C) liquid processed and a large amount of energy consumption.
Accompanying drawing illustrates:
Fig. 1 is structural representation of the present invention;
Fig. 2 is hydraulic diaphragm pump system diagram.
In figure: 1-CO
2storage tank; 2-hydraulic diaphragm tank A; 3-1 check valve A; 3-2-check valve B; 4-electronic weight instrument; 5-static mixer; 6-extractor; 7-electrically-controlled valve A; 8-electrically-controlled valve B; 9-hydraulic diaphragm tank B; 10-knockout drum; 11-products pot; 12-electronic controller; 13-slag ladle; 14-electric control reversing valve; 15-hydraulic pump; 16-feed check valve; 17-feed pump; 18-batch can; 19-barrier film capsules A; 20-barrier film capsule B.
Detailed description of the invention:
Below in conjunction with concrete technology, the present invention is further described:
The low cost low power consuming carbon dioxide supercritical extraction device of the application comprises CO
2storage tank 1, batch can 18, extractor 6 and knockout drum 10, described CO
2storage tank 1 is communicated with the barrier film capsules A 19 in hydraulic diaphragm tank A2 by pipeline, CO
2by CO
2storage tank 1 enters in barrier film capsules A 19 boosted, and the barrier film capsules A 19 in hydraulic diaphragm tank A2 is communicated with extractor 6 by pipeline, the CO after boosting
2enter extractor 6 with after raw material mixing, extractor 6 is communicated with the barrier film capsule B20 in hydraulic diaphragm tank B9 by pipeline, and the barrier film capsule B20 in hydraulic diaphragm tank B9 is communicated with knockout drum 6 by pipeline, is dissolved with the CO of solute
2be separated with solute in knockout drum 10, in the ring cavity between described barrier film capsules A 19 and hydraulic diaphragm tank A2, be filled with hydraulic oil, in the ring cavity between described barrier film capsule B20 and hydraulic diaphragm tank B9, be filled with hydraulic oil.Hydraulic oil flows back and forth between hydraulic diaphragm tank A2 and hydraulic diaphragm tank B9.
Hydraulic diaphragm tank A2 bottom face is provided with electronic weight instrument 4, hydraulic diaphragm tank A2 bottom has pipeline to be communicated with electric control reversing valve 14, the bottom of hydraulic diaphragm tank B9 has pipeline to be communicated with electric control reversing valve 14, and electric control reversing valve 14 has pipeline to be communicated with the port of export with hydraulic pump 15 arrival end respectively.When hydraulic diaphragm tank A2 reaches higher limit or the lower limit of setting, electronic weight instrument 4 output voltage is to electronic controller 12 signal, and electronic controller 12 outputs signal to electric control reversing valve 14 makes electric control reversing valve 14 commutate, and then makes hydraulic oil reverse flow.
Pipeline between barrier film capsule B20 in extractor 6 and hydraulic diaphragm tank B9 is provided with electrically-controlled valve A7, the barrier film capsule B20 in hydraulic diaphragm tank B9 and the pipeline between knockout drum 10 are provided with electrically-controlled valve B8.Electrically-controlled valve A7, electrically-controlled valve B8, electric control reversing valve 14 and electronic weight instrument 4 are controlled by electronic controller 12 respectively.Both high-low pressure CO had been ensured
2smooth transfer, ensures again the breathing ratio of barrier film capsules A 19 and barrier film capsule B20.The accurate control of the breathing ratio of capsule can extend the capsule life-span.
The existing pressurized equipment of current technology is mainly divided into hydraulic oil water pump, gas pump, also has special liquid-solid two-phase pump.But low-pressure supercritical CO
2belong to half liquid half gaseity, density is (0.4 ~ 0.5g/cm between gas-liquid
3), compression ratio is significantly smaller than gas (5 ~ 10 times), only has 1.5 ~ 2 times.Can not the little volume hydraulic oil pump of high speed be used like this, can not with the large volumetric gas pump of middling speed.
According to low-pressure supercritical CO
2physical characteristic, the application devises the hydraulic diaphragm pump of volume in low speed.As shown in Figure 2, hydraulic diaphragm tank A2, check valve A3-1, check valve B3-2, electronic weight instrument 4, electronic controller 12, electric control reversing valve 14, hydraulic pump 15 form CO to structure
2hydraulic diaphragm pumping system. by this system CO
2the low pressure CO of 6 ~ 7MPa in storage tank
2boost to pressure be 20MPa ~ 40MPa laggard enter static mixer 5, meanwhile, be extracted raw material and enter static mixer 5 by batch can 18 through feed pump 17, feed check valve 16, under the effect of static mixer 5, high pressure CO
2fully mix with raw material, make CO
2at utmost dissolving solute. mixture enters after in extractor 6, and the slag charge after stripping solute sinks at the bottom of tank, finally enters slag ladle 13.Carry the CO of solute
2the barrier film capsule B20 in hydraulic diaphragm tank B9 is entered through electrically-controlled valve A7.Because hydraulic diaphragm tank B9 is communicated with hydraulic diaphragm tank A2 with electric control reversing valve 14, hydraulic pump 15, hydraulic oil flows back and forth under the driving of liquor pump 15 between hydraulic diaphragm tank B9 and hydraulic diaphragm tank A2.When hydraulic oil flows from hydraulic diaphragm tank B9 to hydraulic diaphragm tank A2, electrically-controlled valve A7 opens, the high pressure CO of band solute
2enter the barrier film capsule B20 in hydraulic diaphragm tank B9, barrier film capsule B20 expands gradually, and the hydraulic oil in hydraulic diaphragm tank B9 is extruded.Now the inlet pressure of hydraulic pump 15 is higher than outlet pressure, so hydraulic pump 15 not only not consuming electric power, on the contrary exportable energy, this is one of energy-conservation point of this flow process.After barrier film capsule B20 and extractor 6 pressure basic one balance, electrically-controlled valve A7 closes, and now electrically-controlled valve B8 is also closed condition.Along with hydraulic pump 15 is to hydraulic diaphragm tank A2 pump liquid, due to CO in hydraulic diaphragm tank B9
2the bulbs of pressure reduce, due to the CO in barrier film capsules A 19 in hydraulic diaphragm tank A2
2continued to raise also CO by compression pressure
2extrude through check valve B3-2.The now hydraulic pump 15 consuming electric power stage.When in hydraulic diaphragm tank A2, capsule volume reaches lower limit, electronic weight instrument 14 output voltage, makes electric control reversing valve 14 commutate through electronic controller 12, electrically-controlled valve B8 is opened, CO in the barrier film capsule B20 in hydraulic diaphragm tank B9 simultaneously
2press-in knockout drum 10.Because pressure in hydraulic diaphragm tank A2 is higher than pressure in hydraulic diaphragm tank B9, this period hydraulic pump 15 does not consume energy, along with hydraulic oil flows to hydraulic diaphragm tank B9 from hydraulic diaphragm tank A2, barrier film capsules A 19 bulbs of pressure in hydraulic diaphragm tank A2 reduce, when pressure in hydraulic diaphragm tank A2 is slightly lower than CO
2cO during pressure in storage tank 1
2flow in the barrier film capsules A 19 in hydraulic diaphragm tank A2 through check valve A3-1, this period hydraulic diaphragm tank A2 and hydraulic diaphragm tank B9 pressure close, hydraulic pump 15 consumes energy very low.When hydraulic diaphragm tank A2 volume reaches higher limit, electronic weight instrument 4 output voltage makes electric control reversing valve 14 commutate through electronic controller 12, completes circulation.Can be found out by above-mentioned flow process, when hydraulic pump 15 works 70%-75% time inlet pressure higher than or close to outlet pressure, for not consuming energy or the low power consuming period, because of pump energy consumption power=(back pressure-inlet pressure) * flow, reach energy-conservation object.
Solute heavier in knockout drum 10, through cyclonic separation, falls at the bottom of tank, runs up to a certain amount ofly to put into products pot 11.Compared with the CO of lightweight
2cO is returned from tank deck
2storage tank 1 recycles.Whole flow process is airtight does not discharge CO
2, not blowdown.
The volume of hydraulic diaphragm tank A2 is 1/5 ~ 1/7 of extractor 6 volume, the volume 80%-90% that the non-telescope volume (volume when namely expanding into maximum) of barrier film capsule is hydraulic diaphragm tank.The minimum volume (namely barrier film capsule is by volume when being pressed onto minimum) of barrier film capsule is 10% ~ 15% of hydraulic diaphragm tank volume.The withstand voltage twice for outlet maximum pressure of hydraulic diaphragm tank.Hydraulic pump 15 conversion time, the maximum output pressure of hydraulic pump 15 was CO in order to be 1 ~ 3 minute for barrier film capsule transformation period between maximum volume and minimum volume
2export 1.5 times of maximum pressure.
Barrier film capsules A 19 and barrier film capsule B20 are composited by silicon rubber, Obstruct membrane and external protection, have the performance of anti-low temperature (-100 to 200 DEG C), Anti-steam-leakage, rub resistance, because start, shut down CO when pressure has a sudden change
2occasional forms dry ice (-65 DEG C) so barrier film capsule needs low temperature resistant.Barrier film capsules A 19 and barrier film capsule B20 completely cut off that gas performance is good, good springiness, long service life, and permeation rate is lower than General Purpose Rubber 100 times.
Current conventional CO
2extraction equipment processing Chinese medicine cost is at about 3.5 ten thousand yuan per ton, and the prices such as processing natural colouring matter are higher, and the present invention estimates after building up device that materials processing cost per ton can below ten thousand yuan, and cost reduces by three to five times, and application prospect is boundless.
Claims (6)
1. a low cost low power consuming carbon dioxide supercritical extraction device, comprises CO
2storage tank (1), batch can (18), extractor (6) and knockout drum (10), is characterized in that: described CO
2storage tank (1) is communicated with the barrier film capsules A (19) in hydraulic diaphragm tank A (2) by pipeline, barrier film capsules A (19) in hydraulic diaphragm tank A (2) is communicated with extractor (6) by pipeline, extractor (6) is communicated with the barrier film capsule B (20) in hydraulic diaphragm tank B (9) by pipeline, barrier film capsule B (20) in hydraulic diaphragm tank B (9) is communicated with knockout drum (10) by pipeline, hydraulic oil is filled with in ring cavity between described barrier film capsules A (19) and hydraulic diaphragm tank A (2), hydraulic oil is filled with in ring cavity between described barrier film capsule B (20) and hydraulic diaphragm tank B (9).
2. low cost low power consuming carbon dioxide supercritical extraction device according to claim 1, it is characterized in that: hydraulic diaphragm tank A (2) bottom face is provided with electronic weight instrument (4), hydraulic diaphragm tank A (2) bottom has pipeline to be communicated with electric control reversing valve (14), the bottom of hydraulic diaphragm tank B (9) has pipeline to be communicated with electric control reversing valve (14), and electric control reversing valve (14) has pipeline to be communicated with the port of export with hydraulic pump (15) arrival end respectively.
3. low cost low power consuming carbon dioxide supercritical extraction device according to claim 2, it is characterized in that: the pipeline between the barrier film capsule B (20) in extractor (6) and hydraulic diaphragm tank B (9) is provided with electrically-controlled valve A (7), the barrier film capsule B (20) in hydraulic diaphragm tank B (9) and the pipeline between knockout drum (10) are provided with electrically-controlled valve B (8).
4. low cost low power consuming carbon dioxide supercritical extraction device according to claim 3, is characterized in that: electrically-controlled valve A (7), electrically-controlled valve B (8), electric control reversing valve (14) and electronic weight instrument (4) are controlled by electronic controller (12) respectively.
5. a low cost low power consuming carbon dioxide supercritical extraction technique, is characterized in that: hydraulic diaphragm tank A (2), hydraulic diaphragm tank B (9), check valve (3), electronic weight instrument (4), electric control reversing valve (14), hydraulic pump (15) composition CO
2hydraulic diaphragm pumping system, by this system CO
2the low pressure CO of 6 ~ 7MPa in storage tank
2boosting enters static mixer (5), simultaneously, be extracted raw material and enter static mixer (5) by batch can (18) through feed pump (17), feed check valve (16), under the effect of static mixer (5), high pressure CO
2fully mix with raw material, make CO
2at utmost dissolve solute, mixture enters after in extractor (6), carries the CO of solute
2the barrier film capsule B (20) in hydraulic diaphragm tank B (9) is entered through electrically-controlled valve (7), because hydraulic diaphragm tank B (9) is communicated with hydraulic diaphragm tank A (2) with electric control reversing valve (14), hydraulic pump (15), hydraulic oil flows back and forth between hydraulic diaphragm tank B (9) and hydraulic diaphragm tank A (2), when hydraulic oil flows from hydraulic diaphragm tank B (9) to hydraulic diaphragm tank A (2), high pressure CO
2enter extractor (6) through check valve (3), electrically-controlled valve A (7) opens simultaneously, the high pressure CO of band solute
2enter the barrier film capsule B (20) in hydraulic diaphragm tank B (9), and drive hydraulic oil to enter hydraulic diaphragm tank A (2), now the inlet pressure of hydraulic pump (15) is higher than outlet pressure, electrically-controlled valve A (7) closes, electrically-controlled valve B (8) is also closed condition, along with hydraulic pump (15) is to the interior pump hydraulic oil of hydraulic diaphragm tank A (2), the interior pressure of hydraulic diaphragm tank B (9) reduces, and barrier film capsules A (19) pressure in hydraulic diaphragm tank A (2) continues to raise also CO
2extrude, when barrier film capsules A (19) volume in hydraulic diaphragm tank A (2) reaches preset lower limit, electronic weight instrument (4) output voltage, electric control reversing valve (14) commutation hydraulic oil reverse flow is made through electronic controller (12), electrically-controlled valve B (8) is opened, the CO containing solute in the barrier film capsule B (20) in hydraulic diaphragm tank B (9) simultaneously
2press-in knockout drum (10), now, because hydraulic oil flows to hydraulic diaphragm tank B (9) from hydraulic diaphragm tank A (2), in hydraulic diaphragm tank A (2), pressure reduces, CO
2storage tank (1) mesolow CO
2the barrier film capsules A (19) in hydraulic diaphragm tank A (2) is entered through check valve (3), when hydraulic diaphragm tank A (2) volume reaches higher limit, electronic weight instrument (4) output voltage makes electric control reversing valve (14) commutate through electronic controller (12), completes circulation.
6. low cost low power consuming carbon dioxide supercritical extraction technique according to claim 5, it is characterized in that: the volume of hydraulic diaphragm tank A (2) is 1/5 ~ 1/7 of extractor (6) volume, the maximum volume of barrier film capsules A (19) is the 80%-90% of hydraulic diaphragm tank A (2) volume, the minimum volume of barrier film capsules A (19) is 10% ~ 15% of hydraulic diaphragm tank A (2) volume, the withstand voltage twice for outlet maximum pressure of hydraulic diaphragm tank A (2), hydraulic pump (15) conversion time is barrier film capsules A (19) transformation period between maximum volume and minimum volume is 1 ~ 3 minute, hydraulic pump (15) maximum output pressure is CO
2export 1.5 times of maximum pressure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510868689.4A CN105498275B (en) | 2015-12-01 | 2015-12-01 | A kind of inexpensive low power consuming carbon dioxide supercritical extraction device and technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510868689.4A CN105498275B (en) | 2015-12-01 | 2015-12-01 | A kind of inexpensive low power consuming carbon dioxide supercritical extraction device and technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105498275A true CN105498275A (en) | 2016-04-20 |
| CN105498275B CN105498275B (en) | 2017-08-11 |
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ID=55706811
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510868689.4A Active CN105498275B (en) | 2015-12-01 | 2015-12-01 | A kind of inexpensive low power consuming carbon dioxide supercritical extraction device and technique |
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| CN (1) | CN105498275B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111013188A (en) * | 2019-12-27 | 2020-04-17 | 江苏高科制药设备有限公司 | Novel entrained pharmaceutical method based on supercritical CO2 extraction |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1515619A (en) * | 1975-11-10 | 1978-06-28 | Varian Associates | Liquid chromatography pumping system with compensation means for liquid compressibility |
| CN101053596A (en) * | 2007-05-23 | 2007-10-17 | 浙江大学 | Supercritical carbon dioxide method for extracting high purity rhubarb free anthraquinones |
| CN101668949A (en) * | 2007-04-14 | 2010-03-10 | 斯图亚特波特（私有）有限公司 | Pump system |
-
2015
- 2015-12-01 CN CN201510868689.4A patent/CN105498275B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1515619A (en) * | 1975-11-10 | 1978-06-28 | Varian Associates | Liquid chromatography pumping system with compensation means for liquid compressibility |
| CN101668949A (en) * | 2007-04-14 | 2010-03-10 | 斯图亚特波特（私有）有限公司 | Pump system |
| CN101053596A (en) * | 2007-05-23 | 2007-10-17 | 浙江大学 | Supercritical carbon dioxide method for extracting high purity rhubarb free anthraquinones |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111013188A (en) * | 2019-12-27 | 2020-04-17 | 江苏高科制药设备有限公司 | Novel entrained pharmaceutical method based on supercritical CO2 extraction |
| WO2021128978A1 (en) * | 2019-12-27 | 2021-07-01 | 江苏高科制药设备有限公司 | Novel pharmaceutical manufacturing method based on entrainer-aided supercritical co2 extraction |
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| Publication number | Publication date |
|---|---|
| CN105498275B (en) | 2017-08-11 |
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