CN106634037A - Capsanthin solvent extracting solution evaporation method and device - Google Patents
Capsanthin solvent extracting solution evaporation method and device Download PDFInfo
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- CN106634037A CN106634037A CN201611267256.4A CN201611267256A CN106634037A CN 106634037 A CN106634037 A CN 106634037A CN 201611267256 A CN201611267256 A CN 201611267256A CN 106634037 A CN106634037 A CN 106634037A
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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
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- Chemical Kinetics & Catalysis (AREA)
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a capsanthin solvent extracting solution evaporation method. The method comprises the following steps that 1, a capsanthin solvent extracting solution enters a climbing film evaporator at first, and vacuum evaporation is performed; 2, a liquid phase obtained after flashing is performed in the step 1 enters a falling film evaporator, flows from top to bottom in the tube pass of the falling film evaporator, and is subjected to heat exchange with hot water under the temperature of 70-80 DEG C inside the shell pass of the falling film evaporator; 3, the liquid phase drained by the falling film evaporator enters a rotary film evaporator, and vacuum evaporation is performed; 4, the liquid phase at the bottom of the rotary film evaporator enters a molecular distillation evaporator, and distillation is performed under the vacuum condition. According to the method, climbing film evaporation, falling film evaporation, rotary film evaporation and molecular distillation evaporation equipment and operation technological conditions are reasonably set, the evaporation temperature is low, energy consumption is lowered, the treatment efficiency is high, the solvent consumption is small, the cost is greatly lowered, and continuous industrial production is achieved easily.
Description
Technical field
The invention belongs to the extraction field to vegetable raw material, and in particular to a kind of extracting method of utilization evaporation equipment.
Background technology
Capsanthin as a kind of natural colouring matter, with spies such as colorability strong, color is vivid, good stability, security height
Point.It is current most popular natural oil soluble in being widely used in the products such as meat products, Flour product, bean product and catsup and pickled vegetables
Property pigment.
Capsanthin industrial production generally adopts solvent extraction, traditional capsanthin solvent evaporation procedure to there is disposal ability
Little, temperature is high, and capsanthin loss is more, and precipitation effect is undesirable, the shortcomings of solvent consumption is high.Capsanthin main component is grease
Impurity is more in class, but its extract, and itself is again heat-sensitive substance, and processing technology is put forward higher requirement.Therefore, it is necessary to
There is the extract evaporation that the disposal ability for being specifically designed 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, connect short-path evaporator using climbing film evaporator and reclaim mixed cotton seed oil
In solvent, but because in capsanthin solvent extraction liquid impurity it is many, be easy to using climbing film evaporator make when solvent is relatively low
Into blocking, this technique is unsuitable for the concentration of capsanthin extract.To (solvent extraction capsicum in capsanthin extraction process linguistic term
Impact of the haematochrome to absorption ratio, Su Guangping, Food Additives Used in China, 2014 (4)), capsanthin extract one is steamed using liter film
Evaporimeter, two steamings adopt thin film evaporator, and three steam refined using nitrogen precipitation, because nitrogen precipitation is pot group type operation, exist de-
The molten time is long, and disposal ability is little, high energy consumption, the problems such as chroma loss is more.In paper, " solvent extraction capsicum red pigment is to extinction
In the impact of ratio ", successively extract evaporation is carried out using falling film evaporation, climbing-film evaporation, thin film evaporation, equally exist climbing-film evaporation
The susceptible to plugging problem of device, at the same it is molten residual still higher after thin film evaporation, different solvents composite pollution in subsequent treatment can be caused.Always
It, there are various shortcomings in traditional solvent evaporation, be not preferable capsanthin large-scale industrial production technique.
The content of the invention
For the problems referred to above, it is an object of the invention to provide a kind of capsanthin solvent extraction liquid method of evaporating, with process
Ability is big, evaporating temperature is low, capsanthin chroma loss is few, and precipitation effect is good, the advantage that 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.
The technical scheme for realizing the object of the invention is：
A kind of capsanthin solvent extraction liquid method of evaporating, comprises 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；Extract Jing enters flash tank, in flash distillation
Evaporation in case, solvent vapo(u)r removes condensate recycling device by pipeline, to recycle, red Capsaicin Jing flash tanks bottom drain mouth
Drain into by flow container.
2) step 1) liquid phase after flash distillation enters falling film evaporator, in falling film evaporator tube side, inside flows from the top down, with
70～80 DEG C of hot water carries out heat exchange in falling film evaporator shell side；
3) liquid phase that falling film evaporator is discharged enters rotary film evaporator, is evaporated in vacuo；
4) liquid phase of rotary film evaporator bottom enters molecular clock evaporimeter, extract outer boundary in each evaporimeter
Under thermal source and vacuum equipment conditioning, forced evaporation, desolvation reach the purpose of purifying capsanthin.
Wherein, the capsanthin solvent extraction liquid is the extract after the extraction of capsicum particle organic solvent, described organic
Solvent is one or more in the alkane of C1～C8, the dihydroxylic alcohols of C2～C8, acetone, butanone, capsicum particle and organic solvent
Solid-liquid ratio be 1kg：2～5L.
Further, the solvent is volume ratio 2～8:1 alkane and the mixed solvent of acetone.
Preferably, the gas phase temperature of the climbing film evaporator is 54～58 DEG C, the vacuum 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 be -0.05～-
0.07MPa。
Wherein, the gas phase temperature of the rotary film evaporator outlet is controlled to 72～76 DEG C, in rotary film evaporator
Vacuum be -0.06～-0.009MPa,
Wherein, 78～82 DEG C of the gas phase temperature of the molecular clock evaporimeter, vacuum is -0.08-0.1MPa.Solvent steams
The cooling water of 20～28 DEG C in vapour and molecular clock center cooling coil carries out heat exchange, and the solvent vapo(u)r not being condensed is again
Empty Jing after -5～-2 DEG C of chilled brine depth coolings.Chilled brine is the conventional refrigerant of factory, 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 clock evaporimeter is used
80～90 DEG C of hot water is heated.
A kind of capsanthin solvent extraction liquid evaporation equipment, it includes climbing film evaporator, falling film evaporator, the rotation being sequentially connected with
Turn thin film evaporator and molecular clock evaporimeter,
The climbing film evaporator top is connected with climbing-film evaporation flash tank, climbing-film evaporation flash tank bottom by gas equalizing line
Portion arranges liquid outlet；
The falling film evaporator bottom is connected with falling film evaporation flash tank, falling film evaporation flash tank bottom by gas equalizing line
Portion arranges liquid outlet；
The rotation film evaporator top is connected with rotation film flash vaporization case by gas equalizing line, and rotation film evaporation is dodged
Steam box bottom arranges liquid outlet；
Discharging pump, discharge pipe connection molecule evaporator for distillation top are connected with the discharge pipe of rotary film evaporator
Portion, between the vacuum pump set being connected with molecular clock evaporimeter gas equalizing line is connected with.
Wherein, chuck, chuck are provided with outside the wall of the rotary film evaporator and the molecular clock evaporimeter
Interior flowing plus thermal medium, described plus thermal medium is hot water.
Wherein, gear pump is provided with the drain pipe road of the molecular clock evaporimeter, drain pipe road connection inlet is high
In molecular clock evaporimeter top, the supporting fluid reservoir with identical vacuum condition, the supporting liquid storage pot bottom passes through pipeline
Atmospheric storage tank is connected to excavationg pump.
Compared with prior art advantage is the present invention：
(1), method proposed by the present invention, rationally arranges climbing-film evaporation, falling film evaporation, rotating thin film evaporation and molecular clock
The equipment and operating procedure condition of evaporation, the temperature of evaporation is low, reduces energy consumption；Capsanthin chroma loss is few, colour value yield
More than 99%；
(2), precipitation effect is good, and dissolvent residual is less than 20ppm；
(3), serialization evaporation, precipitation, treatment effeciency is high, and solvent consumption is few, and cost is substantially reduced；
(4), it is easily achieved serialization industrial production.
Description of the drawings
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 is spinner flowmeter, and 102 is climbing-film evaporation flash tank, and 103 is climbing-film evaporation
The hot water inlet of device, 104 is the hot water outlet of climbing film evaporator, and 105 is climbing film evaporator condenser, and 2 is falling film evaporator,
201 is falling film evaporator hot water inlet, and 202 is falling film evaporator hot water outlet, and 204 is falling film evaporator condenser, and 3 are rotation
Thin film evaporator, 301 is rotary film evaporator hot water inlet, and 302 is rotary film evaporator hot water outlet, and 304 are rotation
Thin film evaporator condenser, 305 is discharging pump, and 4 is molecular clock evaporimeter, and 401 is molecular clock evaporimeter hot water inlet,
402 is molecular clock evaporimeter hot water outlet, and 403 is molecular clock boil-off gas balance pipe, and 404 is that molecular clock evaporimeter is cold
Condenser.405 is supporting fluid reservoir, and 406 is atmospheric storage tank.
Specific embodiment
Below technical solution of the present invention is further illustrated with preferred embodiment.
Those skilled in the art are it is to be understood that following examples are only used for illustrating the present invention, and are not limited to the present invention
Scope.
The selection of experimental example solvent
Capsicum particle is extracted using 95% reflow of alcohol, facility yield higher (5.13%), but its absorbance is relatively low, says
Bright impurity is more.
Same a collection of capsicum particle petroleum ether refluxing extraction, the absorbance of product is higher, but yields poorly.
Extracted with acetone, not only pigment absorbance is high, and 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.Acetone and n-hexane 2 are found by comparing：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 the climbing film evaporator, falling film evaporator, the rotating thin film that are sequentially connected with
Evaporimeter.
Capsicum particle volume ratio 8:2 n-hexane and acetone mixed solvent, by 1kg:The solid-liquid ratio of 3L carries out extracting
Capsanthin solvent extraction liquid,
1) by capsanthin solvent extraction liquid that colour value is 7.85 with 11 ± 0.2m3/ h flow velocity Jing rotor meters flow 101 is measured,
The climbing film evaporator tube side of 150 ㎡ is squeezed into by centrifugal pump, with 65 ± 1 DEG C of hot water in liter putamina journey heat exchange is carried out, rise membrane tube
In -0.05 ± 0.005MPa, at 54 ± 1 DEG C, extract Jing rises film to climbing-film evaporation gaseous phase outlet temperature control to Stress control in journey
Upper gas balance pipe enters flash tank, evaporates in flash tank, and solvent vapo(u)r goes condensation to reclaim by pipeline, recycles,
Red Capsaicin Jing flash tanks bottom drain mouth is drained into by flow container.
2) the falling film evaporator pipe that film is squeezed into F=120 ㎡ (F represents heat exchange area) by flow container efflux Jing centrifugal pumps 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 evaporation gas phase outlet temperature is controlled at 59 ± 1 DEG C, and extract Jing falling liquid film bottom gas balance pipes enter flash tank, in flash tank
Interior evaporation, solvent vapo(u)r goes condensation to reclaim by pipeline, recycles, and red Capsaicin Jing flash tanks bottom drain mouth is drained into by liquid
Tank.
3) falling liquid film is squeezed into the thin film evaporator barrel of F=15 ㎡ by flow container efflux Jing centrifugal pumps, with thin film evaporator folder
85 ± 1 DEG C of hot water carries out heat exchange in set, and Stress control is in -0.07 ± 0.005MPa, thin film evaporator in thin film evaporator
At 74 ± 1 DEG C, extract Jing films bottom drains into by flow container gaseous phase outlet temperature control, and solvent vapo(u)r is gone cold by gas phase pipeline
It is solidifying to reclaim to recycle.
Per hour can output 570kg product, molten residual 1100.ppm, colour value E150.58, colour value yield 99.40%.
Comparative example 1
Operation is with embodiment 1, wherein step 1)：By capsanthin solvent extraction liquid that colour value is 7.85 with 10m3/ h flow velocitys,
Or 12m3/ h flow velocitys enter climbing film evaporator tube side, then find the molten residual beyond index request (being more than 20ppm) of product, adjust in time
Whole evaporating temperature and vacuum can make it is molten it is residual meet the requirements, but yield reduce, production cost increase.
Embodiment 2
Referring to Fig. 1, capsanthin solvent extraction liquid evaporation equipment, including the climbing film evaporator 1, falling film evaporator being sequentially connected with
2nd, rotary film evaporator 3 and molecular clock evaporimeter 4,
The top of the climbing film evaporator 1 is connected with climbing-film evaporation flash tank 102, climbing-film evaporation flash distillation by gas equalizing line
The bottom of case 102 arranges liquid outlet；
The top of the falling film evaporator 2 is connected with falling film evaporation flash tank, falling film evaporation flash distillation by gas equalizing line 203
Bottom portion arranges liquid outlet；
The rotation top of film evaporator 3 is connected with rotation film flash vaporization case, rotation film evaporation by gas equalizing line
Flash tank bottom arranges liquid outlet；
Discharging pump 305, discharge pipe connection molecule evaporator for distillation 4 are connected with the discharge pipe of rotary film evaporator
Its top feed mouth, molecular clock evaporimeter 4 is connected with molecular clock evaporator-condenser 404, with molecular clock evaporator condensation
Molecular clock boil-off gas balance pipe 403 is connected between the vacuum pump set of the connection of device 404.
Flowing in chuck, chuck is provided with outside the wall of the rotary film evaporator and the molecular clock evaporimeter
Plus thermal medium, the thermal medium that adds of each equipment is hot water, respectively by the hot water of the hot water inlet 103, evaporimeter of climbing film evaporator
Outlet 104, falling film evaporator hot water inlet 201, falling film evaporator hot water outlet 202, rotary film evaporator hot water inlet
301st, rotary film evaporator hot water outlet 302, molecular clock evaporimeter hot water inlet 401, molecular clock evaporimeter hot water go out
Mouth 402 is heated.
Gear pump is provided with the drain pipe road of the molecular clock evaporimeter, drain pipe road connection inlet is higher than molecule
Evaporator for distillation top, the supporting fluid reservoir 405 with identical vacuum condition, the supporting liquid storage pot bottom is by pipeline and row
Go out pump and be connected to atmospheric storage tank 406.
Comparative example 2
Using the capsanthin solvent extraction liquid vapo(u)rization system with the same scale of embodiment 2, adjusting device order, capsanthin is molten
Agent extract is directly added into falling film evaporator, but climbing film evaporator is entered after falling liquid film, can be because the extract after concentration is dense
Degree is high, and liquid film can not rise.
Embodiment 3
Using the equipment of embodiment 2.Capsicum particle volume ratio 8:2 n-hexane and acetone mixed solvent, by 1:3 material
Liquor ratio carries out extracting to obtain capsanthin solvent extraction liquid,
1) by capsanthin solvent extraction liquid that colour value is 7.85 with 11 ± 0.2m3/ h flow velocitys, Jing rotor meter flow measurements, by
Centrifugal pump squeezes into the climbing film evaporator tube side of 150 ㎡, and with 65 ± 1 DEG C of hot water in liter putamina journey heat exchange is carried out, and rises membrane tube journey
In -0.05 ± 0.005MPa, at 54 ± 1 DEG C, extract Jing rises on film climbing-film evaporation gaseous phase outlet temperature control interior Stress control
Portion's gas equalizing line enters flash tank, evaporates in flash tank, and solvent vapo(u)r goes condensation to reclaim by pipeline, recycles, red
Capsaicin Jing flash tank bottom drain mouths are drained into by flow container.
2) rise 75 in the falling film evaporator tube side that film is squeezed into F=120 ㎡ by flow container efflux Jing centrifugal pumps, with falling liquid film shell side
± 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, extract Jing falling liquid film bottom gas balance pipes enter flash tank for degree control, evaporate in flash tank, solvent vapo(u)r
Go condensation to reclaim by pipeline, recycle, red Capsaicin Jing flash tanks bottom drain mouth is drained into by flow container.
3) falling liquid film is squeezed into the thin film evaporator barrel of F=15 ㎡ by flow container efflux Jing centrifugal pumps, with thin film evaporator folder
85 ± 1 DEG C of hot water carries out heat exchange in set, and Stress control is in -0.07 ± 0.005MPa, thin film evaporator in thin film evaporator
At 74 ± 1 DEG C, extract Jing films bottom drains into by flow container gaseous phase outlet temperature control, and solvent vapo(u)r is gone cold by gas phase pipeline
It is solidifying to reclaim.Recycle,
4) film is squeezed into the heating plate of the molecular clock of 16 ㎡ by flow container efflux Jing gear pumps, in molecular clock chuck
85 ± 1 DEG C of hot water carries out heat exchange, and in -0.09 ± 0.005MPa, solvent vapo(u)r steams Stress control with molecule in molecular clock
Evaporating 25 DEG C in the cooling coil of center of cooling water carries out heat exchange, and the solvent vapo(u)r not being condensed freezes water depth for Jing -4 DEG C again
Empty after cooling.Thin film evaporator gaseous phase outlet temperature control is at 80 ± 1 DEG C, and extract Jing films bottom is drained into by flow container, molten
Agent steam goes condensation to reclaim to recycle by gas phase pipeline, and the condensed device of molecular clock heavy phase is cooled to 20-30 DEG C of placement
Finished pot.
Per hour can output 560kg product, molten residual 19ppm, colour value 153.12, colour value yield 99.30%.
Embodiment 4
Using the equipment of embodiment 2.Capsicum particle volume ratio 8:2 n-hexane and acetone mixed solvent, by 1:3 material
Liquor ratio carries out extracting to obtain capsanthin solvent extraction liquid,
1) by capsanthin solvent extraction liquid that colour value is 7.76 with 11 ± 0.2m3/ h flow velocity Jing rotor meter flow measurements, by
Centrifugal pump squeezes into the climbing film evaporator tube side of F=150 ㎡, and with 63 ± 1 DEG C of hot water in liter putamina journey heat exchange is carried out, and rises membrane tube
In -0.05 ± 0.005MPa, at 55 ± 1 DEG C, extract Jing rises film to climbing-film evaporation gaseous phase outlet temperature control to Stress control in journey
Upper gas balance pipe enters flash tank, evaporates in flash tank, and solvent vapo(u)r goes condensation to reclaim by pipeline, recycles,
Red Capsaicin Jing flash tanks bottom drain mouth is drained into by flow container.
2) rise 73 in the falling film evaporator tube side that film is squeezed into F=120 ㎡ by flow container efflux Jing centrifugal pumps, with falling liquid film shell side
± 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, extract Jing falling liquid film bottom gas balance pipes enter flash tank for degree control, evaporate in flash tank, solvent vapo(u)r
Go condensation to reclaim by pipeline, recycle, red Capsaicin Jing flash tanks bottom drain mouth is drained into by flow container.
3) falling liquid film is squeezed into the thin film evaporator barrel of F=15 ㎡ by flow container efflux Jing centrifugal pumps, with thin film evaporator folder
85 ± 1 DEG C of hot water carries out heat exchange in set, and Stress control is in -0.07 ± 0.005MPa, thin film evaporator in thin film evaporator
At 75 ± 1 DEG C, extract Jing films bottom drains into by flow container gaseous phase outlet temperature control, and solvent vapo(u)r is gone cold by gas phase pipeline
It is solidifying to reclaim to recycle,
4) film is squeezed into the heating plate of the molecular clock of F=16 ㎡ by flow container efflux Jing gear pumps, with molecular clock folder
85 ± 1 DEG C of hot water carries out heat exchange in set, in molecular clock Stress control in -0.09 ± 0.005MPa, solvent vapo(u)r with point
The cooling water of 25 DEG C in the cooling coil of sub- distillation center carries out heat exchange, the solvent vapo(u)r not being condensed Jing -4 DEG C of chilled water again
Empty after depth cooling.
At 80 ± 1 DEG C, extract Jing films bottom drains into by flow container thin film evaporator gaseous phase outlet temperature control, and solvent steams
Vapour goes condensation to reclaim to recycle by gas phase pipeline, and the condensed device of molecular clock heavy phase is cooled to 20-30 DEG C of placement finished product
Tank.
Per hour can output 548.08kg product, molten residual 19ppm, colour value 154.20, colour value yield 99.00%.
Embodiment of above is merely to illustrate the present invention, and not limitation of the present invention, about the common of technical field
Technical staff, without departing from the spirit and scope of the present invention, can also make a variety of changes and modification, therefore all
The technical scheme of equivalent falls within scope of the invention, and the scope of patent protection of the present invention should be defined by the claims.
Claims (10)
1. a kind of capsanthin solvent extraction liquid method of evaporating, it is characterised in that it is rapid with 102 times 00 steps .0 that KH bag P1 include 411：
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 evaporimeter tube side, with liter putamina journey；Extract Jing enters flash tank, in flash tank
Evaporation, solvent vapo(u)r removes condensate recycling device by pipeline, to recycle；
2) step 1) liquid phase after flash distillation enters falling film evaporator, in falling film evaporator tube side, inside flows from the top down, with falling liquid film
70～80 DEG C of hot water carries out heat exchange in evaporimeter shell side；
3) liquid phase that falling film evaporator is discharged enters rotary film evaporator, is evaporated in vacuo；
4) liquid phase of rotary film evaporator bottom enters molecular clock evaporimeter, distills under vacuum.
2. the capsanthin solvent extraction liquid method of evaporating according to claim, it is characterised in that the capsanthin solvent is carried
Take liquid be capsicum particle organic solvent extraction after extract, the organic solvent be the alkane of C1～C8, the two of C2～C8
One or more in first alcohol, acetone, butanone, capsicum particle is 1kg with the solid-liquid ratio of organic solvent：2～5L.
3. capsanthin solvent extraction liquid method of evaporating according to claim 2, it is characterised in that the solvent is volume ratio
2～8:1 alkane and the mixed solvent of acetone.
4. capsanthin solvent extraction liquid method of evaporating according to claim 1, it is characterised in that the climbing film evaporator
Gas phase temperature is 54～58 DEG C, and the vacuum of flash tank is -0.02～-0.06MPa, the gas phase temperature 58 of the falling film evaporator
～63 DEG C, vacuum is -0.05～-0.07MPa in falling film evaporator tube side.
5. the capsanthin solvent extraction liquid method of evaporating according to any one of Claims 1 to 4, it is characterised in that the rotation
Turn thin film evaporator outlet gas phase temperature be controlled to 72～76 DEG C, the vacuum in rotary film evaporator be -0.06～-
0.009MPa,
6. according to any one of Claims 1 to 4 described capsanthin solvent extraction liquid method of evaporating, it is characterised in that it is described
78～82 DEG C of the gas phase temperature of molecular clock evaporimeter, vacuum is -0.08-0.1MPa.Solvent vapo(u)r and molecular clock center
The cooling water of 20～28 DEG C in cooling coil carries out heat exchange, the solvent vapo(u)r not being condensed Jing -5～-2 DEG C chilled brine again
Empty after depth cooling.
7. according to any one of Claims 1 to 4 described capsanthin solvent extraction liquid method of evaporating, it is characterised in that it is described
Rotary film evaporator is heated with 80～90 DEG C of hot water, and the molecular clock evaporimeter is carried out with 80～90 DEG C of hot water
Heating.
8. a kind of capsanthin solvent extraction liquid evaporation equipment, it is characterised in that steam including the climbing film evaporator, falling liquid film being sequentially connected with
Device, rotary film evaporator and molecular clock evaporimeter are sent out, the climbing film evaporator top is connected with liter by gas equalizing line
Film flash vaporization case, climbing-film evaporation flash tank bottom arranges liquid outlet；
The falling film evaporator bottom is connected with falling film evaporation flash tank by gas equalizing line, and falling film evaporation flash tank bottom sets
Put liquid outlet；
The rotation film evaporator top is connected with rotation film flash vaporization case by gas equalizing line, rotates film flash vaporization case
Bottom arranges liquid outlet；
It is connected with the discharge pipe of rotary film evaporator at the top of discharging pump, discharge pipe connection molecule evaporator for distillation, with
Gas equalizing line is connected between the vacuum pump set of molecular clock evaporimeter connection.
9. capsanthin solvent extraction liquid evaporation equipment according to claim 8, it is characterised in that the rotating thin film evaporation
Flowing plus thermal medium in chuck, chuck are provided with outside the wall of device and the molecular clock evaporimeter, described plus thermal medium is
Hot water.
10. capsanthin solvent extraction liquid evaporation equipment according to claim 8 or claim 9, it is characterised in that the molecular clock
Gear pump is provided with the drain pipe road of evaporimeter, drain pipe road connection inlet is higher than molecular clock evaporimeter top, has
The supporting fluid reservoir of identical vacuum condition, the supporting liquid storage pot bottom is connected to atmospheric storage tank by pipeline and excavationg pump.
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| CN201611267256.4A CN106634037B (en) | 2016-12-31 | 2016-12-31 | A kind of capsanthin solvent extraction liquid method of evaporating and evaporation equipment |
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| CN201611267256.4A CN106634037B (en) | 2016-12-31 | 2016-12-31 | A kind of capsanthin solvent extraction liquid method of evaporating and evaporation equipment |
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| CN106634037B CN106634037B (en) | 2019-03-22 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253348A (en) * | 2022-07-11 | 2022-11-01 | 山东凯斯达机械制造有限公司 | Evaporation device and process for mixed oil of leaching system |
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| CN102604732A (en) * | 2012-02-14 | 2012-07-25 | 安徽国孚润滑油工业有限公司 | Static mixed rotational flow separation and extraction process of regenerative base oil N-methyl pyrrolidone |
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| CN101205194A (en) * | 2007-12-10 | 2008-06-25 | 吴贵岚 | Three-stage continuous separation and purification technique of fatty primary amide |
| CN102504947A (en) * | 2011-11-07 | 2012-06-20 | 晨光生物科技集团股份有限公司 | Method for refining cottonseed mixed oil |
| CN102516802A (en) * | 2011-12-12 | 2012-06-27 | 山东凯斯达机械制造有限公司 | Method for extracting capsicum red pigment and capsaicin |
| CN102604732A (en) * | 2012-02-14 | 2012-07-25 | 安徽国孚润滑油工业有限公司 | Static mixed rotational flow separation and extraction process of regenerative base oil N-methyl pyrrolidone |
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| CN115253348A (en) * | 2022-07-11 | 2022-11-01 | 山东凯斯达机械制造有限公司 | Evaporation device and process for mixed oil of leaching system |
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