CN106634037B - A kind of capsanthin solvent extraction liquid method of evaporating and evaporation equipment - Google Patents
A kind of capsanthin solvent extraction liquid method of evaporating and evaporation equipment Download PDFInfo
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- CN106634037B CN106634037B CN201611267256.4A CN201611267256A CN106634037B CN 106634037 B CN106634037 B CN 106634037B CN 201611267256 A CN201611267256 A CN 201611267256A CN 106634037 B CN106634037 B CN 106634037B
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- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09B—ORGANIC DYES OR CLOSELY-RELATED COMPOUNDS FOR PRODUCING DYES, e.g. PIGMENTS; MORDANTS; LAKES
- C09B61/00—Dyes of natural origin prepared from natural sources, e.g. vegetable sources
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/22—Evaporating by bringing a thin layer of the liquid into contact with a heated surface
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The present invention provides a kind of capsanthin solvent extraction liquid method of evaporating, the following steps are included: 1) capsanthin solvent extraction liquid initially enters climbing film evaporator, it is evaporated in vacuo, 2) liquid phase after step 1) flash distillation enters falling film evaporator, in falling film evaporator tube side, it inside flows from the top to the bottom, the hot water with 70~80 DEG C in falling film evaporator shell side carries out heat exchange；3) liquid phase of falling film evaporator discharge enters rotary film evaporator, is evaporated in vacuo；4) liquid phase of rotary film evaporator bottom enters molecular distillation evaporator, distills under vacuum conditions.Method proposed by the present invention, is rationally arranged the equipment and operating procedure condition of climbing-film evaporation, falling film evaporation, rotating thin film evaporation and molecular distillation evaporation, and the temperature of evaporation is low, energy consumption is reduced, treatment effeciency is high, and solvent consumption is few, cost substantially reduces, it is easy to accomplish serialization industrial production.
Description
Technical field
The invention belongs to the extraction fields to vegetable raw material, and in particular to a kind of extracting method using evaporation equipment.
Background technique
Capsanthin has the spies such as colorability is strong, color is vivid, stability is good, safety is high as a kind of natural pigment
Point.It is widely used in the products such as meat products, Flour product, bean product and pickled vegetable, is that current most popular natural oil is molten
Property pigment.
Capsanthin industrial production generallys use solvent extraction, and there are processing capacities for traditional capsanthin solvent evaporation procedure
The disadvantages of small, temperature is high, and capsanthin loss is more, and precipitation effect is undesirable, and solvent consumption is high.Capsanthin main component is grease
Class, but impurity is more in its extracting solution, and itself is again heat-sensitive substance, and to processing technology, more stringent requirements are proposed.Therefore, it is necessary to
There is the extracting solution evaporation that the processing capacity specifically for capsanthin feature is big, evaporating temperature is low, precipitation effect is good, solvent consumption is few
Technique.
In the patent of Publication No. CN102504947A, short-path evaporator recycling mixed cotton seed oil is connect using climbing film evaporator
In solvent, but because in capsanthin solvent extraction liquid impurity it is more, be easy to make using climbing film evaporator when solvent content is lower
At blocking, this technique is unsuitable for the concentration of capsanthin extracting solution.To (solvent extraction capsicum in capsanthin extraction process linguistic term
Influence of the haematochrome to absorption ratio, Su Guangping, Food Additives Used in China, 2014 (4)), capsanthin extracting solution one is steamed using liter film
Evaporator, two steam using thin film evaporator, and three steam using the purification of nitrogen precipitation, and because nitrogen precipitation is pot group type operation, there are de-
The problems such as molten time is long, and processing capacity is small, and energy consumption is high, and chroma loss is more.In paper, " solvent extraction capsicum red pigment is to extinction
In the influence of ratio ", liquid evaporation is successively extracted using falling film evaporation, climbing-film evaporation, thin film evaporation, equally exists climbing-film evaporation
The susceptible to plugging problem of device, at the same it is molten residual still higher after thin film evaporation, it will cause different solvents composite pollution in subsequent processing.Always
It, it is not ideal capsanthin large-scale industrial production technique that there are various disadvantages for traditional solvent evaporation.
Summary of the invention
In view of the above-mentioned problems, there is processing the object of the present invention is to provide a kind of capsanthin solvent extraction liquid method of evaporating
Ability is big, evaporating temperature is low, capsanthin chroma loss is few, the advantage that precipitation effect is good, solvent consumption is few.
It is a further object of the present invention to provide a kind of equipment of capsanthin solvent extraction liquid evaporation.
Realize the technical solution of the object of the invention are as follows:
A kind of capsanthin solvent extraction liquid method of evaporating, comprising the following steps:
1) capsanthin solvent extraction liquid initially enters climbing film evaporator, is evaporated in vacuo, and capsanthin solvent extraction liquid is walked
60~70 DEG C of hot water carries out heat exchange in climbing film evaporator tube side, with liter putamina journey；Extracting solution is being flashed through entering flash tank
Evaporation, solvent vapo(u)r remove condensate recycling device by pipeline in case, and to be recycled, red Capsaicin is through flash tank bottom drain mouth
It drains by flow container.
2) liquid phase after step 1) flash distillation enters falling film evaporator, in falling film evaporator tube side, inside flows from the top to the bottom, with
70~80 DEG C of hot water carries out heat exchange in falling film evaporator shell side；
3) liquid phase of falling film evaporator discharge enters rotary film evaporator, is evaporated in vacuo；
4) liquid phase of rotary film evaporator bottom enters molecular distillation evaporator, and extracting solution is in each evaporator by the external world
Under heat source and vacuum equipment conditioning, forced evaporation, removing solvent achieve the purpose that purify capsanthin.
Wherein, the capsanthin solvent extraction liquid is capsicum particle organic solvent extracting solution extracted, described organic
Solvent is one of the alkane of C1~C8, the dihydric alcohol of C2~C8, acetone, butanone or a variety of, capsicum particle and organic solvent
Solid-liquid ratio be 1kg:2~5L.
Further, the solvent is the alkane of 2~8:1 of volume ratio and the mixed solvent of acetone.
Preferably, the gas phase temperature of the climbing film evaporator is 54~58 DEG C, the vacuum degree of flash tank is -0.02~-
0.06MPa, 58~63 DEG C of the gas phase temperature of the falling film evaporator, in falling film evaporator tube side vacuum degree be -0.05~-
0.07MPa。
Wherein, the gas phase temperature control of the rotary film evaporator outlet is 72~76 DEG C, in rotary film evaporator
Vacuum degree be -0.06~-0.009MPa,
Wherein, 78~82 DEG C of the gas phase temperature of the molecular distillation evaporator, vacuum degree are -0.08-0.1MPa.Solvent steams
20~28 DEG C of cooling water in vapour and molecular distillation center cooling coil carries out heat exchange, and not condensed solvent vapo(u)r is again
It is emptied after -5~-2 DEG C of chilled brine depth are cooling.Chilled brine is the refrigerant of factory's routine, wherein containing calcium chloride
Or sodium chloride.
Wherein, the rotary film evaporator is heated with 80~90 DEG C of hot water, and the molecular distillation evaporator is used
80~90 DEG C of hot water is heated.
A kind of capsanthin solvent extraction liquid evaporation equipment comprising sequentially connected climbing film evaporator, falling film evaporator, rotation
Turn thin film evaporator and molecular distillation evaporator,
The climbing film evaporator top is connected with climbing-film evaporation flash tank, climbing-film evaporation flash tank bottom by gas equalizing line
Liquid outlet is arranged in portion；
The falling film evaporator lower part is connected with falling film evaporation flash tank, falling film evaporation flash tank bottom by gas equalizing line
Liquid outlet is arranged in portion；
The rotation film evaporator top is connected with rotation film flash vaporization case by gas equalizing line, and rotation film evaporation is dodged
Liquid outlet is arranged in steam box bottom；
Discharging pump, discharge pipe connection molecule evaporator for distillation top are connected on the discharge pipe of rotary film evaporator
Portion is connected with gas equalizing line between the vacuum pump set connecting with molecular distillation evaporator.
Wherein, collet, collet are provided with outside the wall of the rotary film evaporator and the molecular distillation evaporator
Interior flowing heat medium, the heat medium are hot water.
Wherein, the outlet tube road of the molecular distillation evaporator is provided with gear pump, and it is high that outlet tube road connects inlet
At the top of molecular distillation evaporator, the mating fluid reservoir with identical vacuum condition, the mating liquid storage pot bottom passes through pipeline
Atmospheric storage tank is connected to discharge pump.
Advantage is the present invention compared with prior art:
(1), climbing-film evaporation, falling film evaporation, rotating thin film evaporation and molecular distillation is rationally arranged in method proposed by the present invention
The equipment and operating procedure condition of evaporation, the temperature of evaporation is low, reduces energy consumption；Capsanthin chroma loss is few, color value yield
99% or more；
(2), precipitation effect is good, and dissolvent residual is lower than 20ppm；
(3), serialization evaporation, precipitation, treatment effeciency is high, and solvent consumption is few, and cost substantially reduces；
(4), it is easily achieved serialization industrial production.
Detailed description of the invention
Fig. 1: the structure diagram of capsanthin solvent extraction liquid evaporation equipment of the present invention.
In figure, 1 is climbing film evaporator, and 101 be spinner flowmeter, and 102 be climbing-film evaporation flash tank, and 103 be climbing-film evaporation
The hot water inlet of device, 104 be the hot water outlet of climbing film evaporator, and 105 be climbing film evaporator condenser, and 2 be falling film evaporator,
201 be falling film evaporator hot water inlet, and 202 be falling film evaporator hot water outlet, and 204 be falling film evaporator condenser, and 3 be rotation
Thin film evaporator, 301 be rotary film evaporator hot water inlet, and 302 be rotary film evaporator hot water outlet, and 304 be rotation
Thin film evaporator condenser, 305 be discharging pump, and 4 be molecular distillation evaporator, and 401 be molecular distillation evaporator hot water inlet,
402 be molecular distillation evaporator hot water outlet, and 403 be molecular distillation boil-off gas balance pipe, and 404 is cold for molecular distillation evaporator
Condenser.405 be mating fluid reservoir, and 406 be atmospheric storage tank.
Specific embodiment
With preferred embodiment, further explanation of the technical solution of the present invention below.
Those skilled in the art should know following embodiment is only used to illustrate the present invention, and is not limited to the present invention
Range.
The selection of experimental example solvent
Capsicum particle is extracted using 95% reflow of alcohol, and facility yield is higher (5.13%), but its absorbance is lower, says
Bright impurity is more.
Same a batch capsicum particle petroleum ether refluxing extraction, the absorbance of product is higher, but low output.
It is extracted with acetone, not only pigment absorbance is high, but also yield is also higher, but acetone extraction pigment finished product is sticky, product
Matter is poor, so using acetone and n-hexane mixed solvent as Extraction solvent.By comparing discovery acetone and n-hexane 2:8
The viscosity of the mixed solvent of (volume ratio) is the most suitable, can in industrial equipment smooth operation.
Embodiment 1
Capsanthin solvent extraction liquid evaporation equipment, including sequentially connected climbing film evaporator, falling film evaporator, rotating thin film
Evaporator.
The n-hexane and acetone mixed solvent of capsicum particle volume ratio 8:2 extract by the solid-liquid ratio of 1kg:3L
Capsanthin solvent extraction liquid,
1) by color value be 7.85 capsanthin solvent extraction liquid with 11 ± 0.2m3/ h flow velocity is measured through rotor meter flow 101,
65 ± 1 DEG C of hot water carries out heat exchange in the climbing film evaporator tube side for squeezing into 150 ㎡ by centrifugal pump, with liter putamina journey, rises membrane tube
Pressure control is controlled in -0.05 ± 0.005MPa, climbing-film evaporation gaseous phase outlet temperature at 54 ± 1 DEG C in journey, and extracting solution is through a liter film
Upper gas balance pipe enters flash tank, evaporates in flash tank, and solvent vapo(u)r goes condensing recovery by pipeline, is recycled,
Red Capsaicin is drained into through flash tank bottom drain mouth by flow container.
2) the falling film evaporator pipe that film is squeezed into F=120 ㎡ (F indicates heat exchange area) by flow container efflux through centrifugal pump is risen
75 ± 1 DEG C of hot water carries out heat exchange in journey, with falling liquid film shell side, and the control of falling liquid film tube side internal pressure power is in -0.06 ± 0.005MPa, drop
Film evaporates the control of gas phase outlet temperature at 59 ± 1 DEG C, and extracting solution enters flash tank through falling liquid film bottom gas balance pipe, in flash tank
Interior evaporation, solvent vapo(u)r go condensing recovery by pipeline, are recycled, and red Capsaicin is drained into through flash tank bottom drain mouth by liquid
Tank.
3) falling liquid film is squeezed into the thin film evaporator barrel of F=15 ㎡ by flow container efflux through centrifugal pump, is pressed from both sides with thin film evaporator
85 ± 1 DEG C of hot water carries out heat exchange in set, and pressure control is in -0.07 ± 0.005MPa, thin film evaporator in thin film evaporator
Gaseous phase outlet temperature is controlled at 74 ± 1 DEG C, and extracting solution is drained into through film bottom by flow container, and solvent vapo(u)r is gone cold by gas phase pipeline
Solidifying recycling is to be recycled.
Per hour can output 570kg product, molten residual 1100.ppm, color value E150.58, color value yield 99.40%.
Comparative example 1
Operation is with embodiment 1, wherein step 1): by color value be 7.85 capsanthin solvent extraction liquid with 10m3/ h flow velocity,
Or 12m3/ h flow velocity enters climbing film evaporator tube side, then finds the molten residual beyond index request (being greater than 20ppm) of product, adjust in time
Whole evaporating temperature and vacuum degree can make it is molten it is residual meet the requirements, but yield reduce, the production cost increases.
Embodiment 2
Referring to Fig. 1, capsanthin solvent extraction liquid evaporation equipment, including sequentially connected climbing film evaporator 1, falling film evaporator
2, rotary film evaporator 3 and molecular distillation evaporator 4,
1 top of climbing film evaporator is connected with climbing-film evaporation flash tank 102, climbing-film evaporation flash distillation by gas equalizing line
Liquid outlet is arranged in 102 bottom of case；
2 top of falling film evaporator is connected with falling film evaporation flash tank, falling film evaporation flash distillation by gas equalizing line 203
Liquid outlet is arranged in bottom portion；
3 top of rotation film evaporator is connected with rotation film flash vaporization case, rotation film evaporation by gas equalizing line
Liquid outlet is arranged in flash tank bottom；
Discharging pump 305, discharge pipe connection molecule evaporator for distillation 4 are connected on the discharge pipe of rotary film evaporator
Top feed mouth, molecular distillation evaporator 4 are connected with molecular distillation evaporator-condenser 404, with molecular distillation evaporator condensation
Molecular distillation boil-off gas balance pipe 403 is connected between the vacuum pump set that device 404 connects.
Collet, flowing in collet are provided with outside the wall of the rotary film evaporator and the molecular distillation evaporator
Heat medium, the heat medium of each equipment are hot water, pass through the hot water inlet 103 of climbing film evaporator, the hot water of evaporator respectively
Outlet 104, falling film evaporator hot water inlet 201, falling film evaporator hot water outlet 202, rotary film evaporator hot water inlet
301, rotary film evaporator hot water outlet 302, molecular distillation evaporator hot water inlet 401, molecular distillation evaporator hot water go out
Mouth 402 is heated.
The outlet tube road of the molecular distillation evaporator is provided with gear pump, and outlet tube road connects inlet and is higher than molecule
Evaporator for distillation top, the mating fluid reservoir 405 with identical vacuum condition, the mating liquid storage pot bottom pass through pipeline and row
Pump is connected to atmospheric storage tank 406 out.
Comparative example 2
Using the capsanthin solvent extraction liquid vapo(u)rization system with the same scale of embodiment 2, equipment sequence is adjusted, capsanthin is molten
Agent extracting solution is directly added into falling film evaporator, but enters climbing film evaporator after falling liquid film, can be because the extract liquor after concentration is dense
Degree is high, and liquid film cannot rise.
Embodiment 3
Using the equipment of embodiment 2.The n-hexane and acetone mixed solvent of capsicum particle volume ratio 8:2, by the material of 1:3
Liquor ratio carries out extracting to obtain capsanthin solvent extraction liquid,
1) by color value be 7.85 capsanthin solvent extraction liquid with 11 ± 0.2m3/ h flow velocity, through rotor meter flow measurement, by
Centrifugal pump squeezes into the climbing film evaporator tube side of 150 ㎡, and the hot water with 65 ± 1 DEG C in liter putamina journey carries out heat exchange, rises membrane tube journey
Interior pressure control is in -0.05 ± 0.005MPa, and climbing-film evaporation gaseous phase outlet temperature is controlled at 54 ± 1 DEG C, and extracting solution is through on liter film
Portion's gas equalizing line enters flash tank, evaporates in flash tank, and solvent vapo(u)r goes condensing recovery by pipeline, is recycled, red
Capsaicin is drained into through flash tank bottom drain mouth by flow container.
2) the falling film evaporator tube side that film is squeezed into F=120 ㎡ by flow container efflux through centrifugal pump is risen, in falling liquid film shell side 75
± 1 DEG C of hot water carries out heat exchange, and falling liquid film tube side internal pressure power is controlled in -0.06 ± 0.005MPa, falling film evaporation gaseous phase outlet temperature
At 59 ± 1 DEG C, extracting solution enters flash tank through falling liquid film bottom gas balance pipe, evaporates in flash tank, solvent vapo(u)r for degree control
Condensing recovery is gone by pipeline, is recycled, red Capsaicin is drained into through flash tank bottom drain mouth by flow container.
3) falling liquid film is squeezed into the thin film evaporator barrel of F=15 ㎡ by flow container efflux through centrifugal pump, is pressed from both sides with thin film evaporator
85 ± 1 DEG C of hot water carries out heat exchange in set, and pressure control is in -0.07 ± 0.005MPa, thin film evaporator in thin film evaporator
Gaseous phase outlet temperature is controlled at 74 ± 1 DEG C, and extracting solution is drained into through film bottom by flow container, and solvent vapo(u)r is gone cold by gas phase pipeline
Solidifying recycling.It is recycled,
4) film is squeezed into the heating plate of the molecular distillation of 16 ㎡ by flow container efflux through gear pump, in molecular distillation collet
85 ± 1 DEG C of hot water carries out heat exchange, and pressure control is steamed in -0.09 ± 0.005MPa, solvent vapo(u)r and molecule in molecular distillation
It evaporates 25 DEG C of cooling water in the cooling coil of center and carries out heat exchange, not condensed solvent vapo(u)r -4 DEG C of freezing water depths of warp again
It is emptied after cooling.Thin film evaporator gaseous phase outlet temperature is controlled at 80 ± 1 DEG C, and extracting solution is drained into through film bottom by flow container, molten
Agent steam goes condensing recovery to be recycled by gas phase pipeline, and molecular distillation heavy phase is cooled to 20-30 DEG C of placement through condenser
Finished pot.
Per hour can output 560kg product, molten residual 19ppm, color value 153.12, color value yield 99.30%.
Embodiment 4
Using the equipment of embodiment 2.The n-hexane and acetone mixed solvent of capsicum particle volume ratio 8:2, by the material of 1:3
Liquor ratio carries out extracting to obtain capsanthin solvent extraction liquid,
1) by color value be 7.76 capsanthin solvent extraction liquid with 11 ± 0.2m3/ h flow velocity through rotor meter flow measurement, by
Centrifugal pump squeezes into the climbing film evaporator tube side of F=150 ㎡, and the hot water with 63 ± 1 DEG C in liter putamina journey carries out heat exchange, rises membrane tube
Pressure control is controlled in -0.05 ± 0.005MPa, climbing-film evaporation gaseous phase outlet temperature at 55 ± 1 DEG C in journey, and extracting solution is through a liter film
Upper gas balance pipe enters flash tank, evaporates in flash tank, and solvent vapo(u)r goes condensing recovery by pipeline, is recycled,
Red Capsaicin is drained into through flash tank bottom drain mouth by flow container.
2) the falling film evaporator tube side that film is squeezed into F=120 ㎡ by flow container efflux through centrifugal pump is risen, in falling liquid film shell side 73
± 1 DEG C of hot water carries out heat exchange, and falling liquid film tube side internal pressure power is controlled in -0.05 ± 0.005MPa, falling film evaporation gaseous phase outlet temperature
At 58 ± 1 DEG C, extracting solution enters flash tank through falling liquid film bottom gas balance pipe, evaporates in flash tank, solvent vapo(u)r for degree control
Condensing recovery is gone by pipeline, is recycled, red Capsaicin is drained into through flash tank bottom drain mouth by flow container.
3) falling liquid film is squeezed into the thin film evaporator barrel of F=15 ㎡ by flow container efflux through centrifugal pump, is pressed from both sides with thin film evaporator
85 ± 1 DEG C of hot water carries out heat exchange in set, and pressure control is in -0.07 ± 0.005MPa, thin film evaporator in thin film evaporator
Gaseous phase outlet temperature is controlled at 75 ± 1 DEG C, and extracting solution is drained into through film bottom by flow container, and solvent vapo(u)r is gone cold by gas phase pipeline
It is solidifying to recycle to be recycled,
4) film is squeezed into the heating plate of the molecular distillation of F=16 ㎡ by flow container efflux through gear pump, is pressed from both sides with molecular distillation
85 ± 1 DEG C of hot water carries out heat exchange in set, in molecular distillation pressure control in -0.09 ± 0.005MPa, solvent vapo(u)r with point
25 DEG C of cooling water in the cooling coil of sub- distillation center carries out heat exchange, and not condensed solvent vapo(u)r passes through -4 DEG C of chilled waters again
It is emptied after depth is cooling.
The control of thin film evaporator gaseous phase outlet temperature is at 80 ± 1 DEG C, and extracting solution is drained into through film bottom by flow container, and solvent steams
Vapour goes condensing recovery to be recycled by gas phase pipeline, and molecular distillation heavy phase is cooled to 20-30 DEG C of placement finished product through condenser
Tank.
Per hour can output 548.08kg product, molten residual 19ppm, color value 154.20, color value yield 99.00%.
The above embodiments are only used to illustrate the present invention, and not limitation of the present invention, in relation to the common of technical field
Technical staff can also make a variety of changes and modification without departing from the spirit and scope of the present invention, therefore all
Equivalent technical solution also belongs to scope of the invention, and scope of patent protection of the invention should be defined by the claims.
Claims (5)
1. a kind of capsanthin solvent extraction liquid method of evaporating, which comprises the following steps:
1) capsanthin solvent extraction liquid initially enters climbing film evaporator, is evaporated in vacuo, and capsanthin solvent extraction liquid walks a liter film
60~70 DEG C of hot water carries out heat exchange in evaporator tube side, with liter putamina journey；Extracting solution is through entering flash tank, in flash tank
Evaporation, solvent vapo(u)r remove condensate recycling device by pipeline, to be recycled；The gas phase temperature of the climbing film evaporator be 54~
58 DEG C, the vacuum degree of flash tank is -0.02~-0.06MPa,
2) liquid phase after step 1) flash distillation enters falling film evaporator, in falling film evaporator tube side, inside flows from the top to the bottom, with falling liquid film
70~80 DEG C of hot water carries out heat exchange in evaporator shell side；58~63 DEG C of the gas phase temperature of the falling film evaporator, falling liquid film steam
Sending out vacuum degree in device tube side is -0.05~-0.07MPa；
3) liquid phase of falling film evaporator discharge enters rotary film evaporator, is evaporated in vacuo, the rotary film evaporator
The gas phase temperature control of outlet is 72~76 DEG C, and the vacuum degree in rotary film evaporator is -0.06~-0.009MPa, described
Rotary film evaporator is heated with 80~90 DEG C of hot water；
4) liquid phase of rotary film evaporator bottom enters molecular distillation evaporator, distills under vacuum conditions, and the molecule steams
78~82 DEG C of the gas phase temperature of evaporator for distillation, vacuum degree are -0.08~-0.1MPa；Solvent vapo(u)r and molecular distillation center are cooling
20~28 DEG C of cooling water in coil pipe carries out heat exchange, and not condensed solvent vapo(u)r passes through -5~-2 DEG C of chilled brine depth again
It is emptied after cooling；The molecular distillation evaporator is heated with 80~90 DEG C of hot water；
The capsanthin solvent extraction liquid method of evaporating, the capsanthin solvent extraction liquid evaporation equipment of use include being sequentially connected with
Climbing film evaporator, falling film evaporator, rotary film evaporator and molecular distillation evaporator,
The climbing film evaporator top is connected with climbing-film evaporation flash tank by gas equalizing line, and climbing-film evaporation flash tank bottom is set
Set liquid outlet；
The falling film evaporator lower part is connected with falling film evaporation flash tank by gas equalizing line, and falling film evaporation flash tank bottom is set
Set liquid outlet；
The rotary film evaporator top is connected with rotating thin film flash vaporization case, rotating thin film evaporation by gas equalizing line
Liquid outlet is arranged in flash tank bottom；
It is connected with discharging pump on the discharge pipe of rotary film evaporator, at the top of discharge pipe connection molecule evaporator for distillation, with
Gas equalizing line is connected between the vacuum pump set of molecular distillation evaporator connection.
2. capsanthin solvent extraction liquid method of evaporating according to claim 1, which is characterized in that the capsanthin solvent mentions
Taking liquid is capsicum particle organic solvent extracting solution extracted, the organic solvent be the alkane of C1~C8, C2~C8 two
One of first alcohol, acetone, butanone are a variety of, and the solid-liquid ratio of capsicum particle and organic solvent is 1kg:2~5L.
3. capsanthin solvent extraction liquid method of evaporating according to claim 2, which is characterized in that the solvent is volume ratio
The alkane of 2~8:1 and the mixed solvent of acetone.
4. capsanthin solvent extraction liquid method of evaporating according to claim 1, which is characterized in that the rotating thin film evaporation
It is provided with collet outside the wall of device and the molecular distillation evaporator, flows heat medium in collet, the heat medium is
Hot water.
5. capsanthin solvent extraction liquid method of evaporating according to claim 1, which is characterized in that the molecular distillation evaporation
The outlet tube road of device is provided with gear pump, and outlet tube road connects inlet and is higher than at the top of molecular distillation evaporator, with identical
The mating fluid reservoir of vacuum condition, the mating liquid storage pot bottom are connected to atmospheric storage tank by pipeline and discharge pump.
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| CN106634037B true CN106634037B (en) | 2019-03-22 |
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