CN103657135A - Internal heating type evaporative crystallization tank - Google Patents
Internal heating type evaporative crystallization tank Download PDFInfo
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- CN103657135A CN103657135A CN201210314055.0A CN201210314055A CN103657135A CN 103657135 A CN103657135 A CN 103657135A CN 201210314055 A CN201210314055 A CN 201210314055A CN 103657135 A CN103657135 A CN 103657135A
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Abstract
The invention belongs to the technical field of evaporative crystallization tanks, and discloses an internal heating type evaporative crystallization tank. The internal heating type evaporative crystallization tank comprises an upper head (10), a tank body (11), a lower head (14) and a support (2). The internal heating type evaporative crystallization tank is characterized in that the upper head (10) is arranged just above the tank body (11), the lower head (14) is arranged just below the tank body (11), the upper head (10), the tank body (11) and the lower head (14) form a closed space structure, the support (2) is arranged at two sides below the tank body (11), and a plurality of sight glasses (5) are uniformly arranged on the tank body (11). A cylindrical gas-liquid separator (7) is arranged above a cone body of the upper head (10), a lower spreading type discharging valve (1) is arranged on a cone body of the lower head (14), and a condensed water outlet (15) is arranged at one side, which is opposite to the side with the lower spreading type discharging valve, of the cone body. The internal heating type evaporative crystallization tank provided by the invention is large in heat exchange area, good in in-tank circulation and short in production period.
Description
Technical field
The technology of the present invention relates to the technical field of evaporation crystallization equipment, relates in particular to the evaporative crystallization tank of internal heat type.
Background technology
Evaporation crystallization equipment is widely used in the concentrated of the high viscosity feed liquids such as jam, preserved fruit, syrup, dairy products, bean milk crystal, edible glue, and is applied in the effects such as freezing, finished product crystallization that mix, lower the temperature of material stirring in the industries such as pharmacy, fine chemistry industry, bioengineering.Evaporative crystallization tank is generally comprised of pot body, pot cover, agitator, chuck, transmission device, gland seal device etc., and material and perforate can be formulated according to user's technological requirement.Heat form has electrical heating, oil heating, vapour heating, water heating (or cooling) etc.Chuck form is divided into: jacket type and outer coil-type.Whipped form generally has oar formula, anchor formula, frame, ribbon formula, scrapes wall type etc.High rotating speed stirs dispersion impeller formula, turbine type, high shear formula, propeller formula etc., and client can be according to process choice.Type of belt drive has common electric machine, fire-proof motor, electromagnetic adjustable speed motor, frequency converter etc.Seal form has common fillers sealing, the packing seal of combined type tetrafluoro, mechanical seal etc.Discharging form has ball valve, lower exhibition valve etc.
The product of equipment same composition, required final condition can reach by adjusting operation parameter.Stirring-type evaporimeter is for the material of high viscosity, paste body shape or pulpous state.Conventionally stirring-type evaporimeter, as highly enriched device, is arranged in the evaporimeter downstream of continued operation.The evaporation rate of stirring-type evaporimeter is lower.Can be more unfavorable when the size of evaporimeter is amplified.In the occasion allowing, heating surface can increase by heat(ing) coil is installed.In order to obtain satisfied evaporation rate, the temperature difference of vaporization chamber and boiling-house must be quite high.The impact of the common hand heating surface of existing crystallizing evaporator, heat exchange area is less, and thermal cycle is poor, tends to make the interior crystal structure of tank inhomogeneous, thereby affects crystalline rate and crystalline quality.
After crystallizing tank is mixing of materials reaction, the crystallizer of interlayer domestic demand chilled water or chilled water reduces heat, its key link is the size of interlayer area, the version of agitator and material outlet form, high accuracy polishing in crystallization tank body, and the requirement of cleaning without dead angle in tank body meets technique service condition.Different technological requirements, has abundant Design and manufacture experience, and the equipment of producing meets GMP checking requirement completely.Can produce the crystallization tank body of 0.3-5m3.
Current problem is to provide a kind of novel evaporative crystallization tank, can increase interlayer area, and in technique, adopt high-precision polishing, meets the needs of actual production.
Summary of the invention
The internal heat type evaporation crystallizing tank of features such as the object of the present invention is to provide that heat exchange area is large, circulate in tank, with short production cycle, single tank output is large, solves the technical deficiency of existing evaporative crystallization tank.
Technical scheme of the present invention is that a kind of evaporative crystallization tank with following structure is provided:
Internal heat type evaporative crystallization tank, comprising: upper cover 10, tank body 11, low head 14, bearing 2; It is characterized in that: upper cover 10 be arranged on tank body 11 directly over, low head 14 be arranged on tank body 11 under, upper cover 10, tank body 11 and low head 14 form the space structure of a sealing; Bearing 2 is arranged on the both sides, below of tank body 11; Also evenly distributed on tank body 11 have some visors 5.
Described upper cover 10 is taper, and its cone top is provided with columned gas-liquid separator 7; Top one side of gas-liquid separation 7 is also provided with indirect steam outlet 8.
In the cone of described upper cover 10, a side is provided with blow-down pipe 6, and opposite side is also provided with hose entrance 9.
Described low head 14 is taper, is provided with bottom open type baiting valve 1 in its cone, and a relative side is also provided with condensate water outlet 15.
The middle part of described tank body 11 is also provided with reinforcement 4.
The tank body below of described reinforcement 4 is also provided with charging aperture 12.
The interior lower end of described tank body 11 is provided with the heater 13 of shell and tube, and middle part is provided with agitator 3.
One end of described agitator 3 is provided with transmission device 16.
Described upper cover 10, tank body 11, low head 14 all adopt SUS304 stainless steel.
The present invention is in the process of using, first from the charging aperture 12 of tank body 11, add a certain amount of solvent or diluent liquid, then start the transmission device 16 of tank body 11 belows, thereby drive the agitator 3 in tank body 11 to start working, open the row formula heating tube 13 in tank body 11 simultaneously, now feed liquid is stirred while being heated, and heating steam is conducted heat and condensation between pipe, transfers heat to feed liquid.Feed liquid is heated boiling vaporization, and the indirect steam of generation and feed liquid rise at a high speed in pipe, and the indirect steam that concentrate is risen at a high speed drives, and along tube wall, becomes membranaceous rising to be constantly heated evaporation.Feed liquid is concentrated to top exit gradually from heating clamber bottom, and concentrate enters gas-liquid separator 7, and indirect steam is discharged from the indirect steam outlet 8 at top, separation chamber, and condensed water is discharged from condensate water outlet 15.A concentrate part is by circulation pipe, then enters heating clamber bottom, continues concentratedly, and the exit that another part reaches the bottom open type baiting valve 1 that the concentrate of concentration requirement can be by tank body 11 bottoms emits.Can from visor 5, observe the whole process of crystallization, be convenient to add at any time enough feed liquids to supplement the deficiency after feed liquid crystallization.By adding the whole process of thermal agitation evaporation, solution is all crystallizations gradually, from the exit of bottom open type baiting valve, emit, and have completed a free of contamination evaporation and crystal process of totally enclosed type.
Compared with prior art, beneficial effect of the present invention is:
The whole tank body of internal heat type evaporative crystallization tank of the present invention all adopts SUS304 stainless steel, has guaranteed the stability of tank body and has met the requirement of evaporative crystallization tank to high accuracy technique; Upper cover 10, tank body 11, low head 14 have formed a fully closed space, totally enclosed design is guaranteed that material is under free of contamination state all the time and is operated, can guarantee that crystallization process in tank body is not subject to the impact of ambient temperature, humidity, pollution, the carrying out that is conducive to crystallization process, and the pollution on source in food technology, safety and environmental protection have been stopped; Arranging of tube still heater 13 and agitator 3 guaranteed that feed liquid is heated evenly, and crystallization forms also more even; The setting of visor 5 can be operator a visual window is provided in the process of evaporative crystallization tank work, observes at any time feed liquid crystallization situation, is convenient to add in time supplementary feed liquid, thereby increases work efficiency.Internal heat type evaporative crystallization tank heat exchange area of the present invention is large, circulate in tank, with short production cycle, single tank output is large, is applicable to the crystallization of food engineering feed liquid.
Accompanying drawing explanation
Accompanying drawing 1 is the half sectional view of internal heat type evaporative crystallization tank of the present invention.
Accompanying drawing 2 is the top view of internal heat type evaporative crystallization tank of the present invention.
As shown in the figure: 1, bottom open type baiting valve, 2, bearing, 3, agitator, 4, reinforcement, 5, visor, 6, blow-down pipe, 7, gas-liquid separator, 8, indirect steam outlet, 9, soft water entrance, 10, upper cover, 11, tank body, 12, charging aperture, 13, tube still heater, 14, low head, 15, condensate water outlet, 16, transmission device.
The specific embodiment
Below in conjunction with the drawings and specific embodiments, the present invention will be further described.
The evaporative crystallization tank of internal heat type of the present invention comprises: bottom open type baiting valve 1, bearing 2, agitator 3, reinforcement 4, visor 5, blow-down pipe 6, gas-liquid separator 7, indirect steam outlet 8, soft water entrance 9, upper cover 10, tank body 11, charging aperture 12, tube still heater 13, low head 14, condensate water outlet 15, transmission device 16.The evaporative crystallization tank of internal heat type is comprised of upper cover 10, tank body 11, low head 14, bearing 2, and tapered upper cover 10 and low head 14 lay respectively at top and the bottom of tank body 11, has formed an enclosed tank structure.The inside of tank body 11 is disposed with gas-liquid separator 7, tube still heater 13, agitator 3 from top to bottom, and the end of agitator 3 is connected with transmission device 16.
When feed liquid enters from the bottom of tank body 11, heating steam is conducted heat and condensation between pipe, transfers heat to feed liquid.Feed liquid is heated boiling vaporization, and the indirect steam of generation and feed liquid rise at a high speed in pipe, and the indirect steam that the feed liquid after evaporation and concentration is risen at a high speed drives, and along tube wall, becomes membranaceous rising to be constantly heated evaporation.Feed liquid is concentrated to top exit gradually from heating clamber bottom, and concentrate enters gas-liquid separator 7, and indirect steam is discharged from the indirect steam outlet 8 of upper cover 10.A concentrate part is passed through circulation pipe, then enters heating clamber bottom, continues to concentrate, and another part reaches the concentrate of concentration requirement can emit from the bottom of low head 14, thereby realizes the process of whole evaporative crystallization.
The concentration that adds a certain amount of solvent or diluent liquid product extremely final needs of heating evaporation under the effect of stirring.For keeping quantitative liquid, by regularly adding the mode of feed liquid can reach semicontinuous operation in evaporation process.
Evaporative crystallization tank body of the present invention adopts sanitation-grade to open soon interface outward.Several visors 5 are equipped with, the interfaces such as rotating wash bowl and nitrogen inlet.And, evaporative crystallization tank of the present invention adopts SUS304 stainless steel, and crystallizing tank inwall is processed through mirror finish, and totally enclosed design is guaranteed that material is under free of contamination state all the time and operated, equipment sealing adopts special sanitation-grade mechanical seal, guarantees that material is not contaminated.
The present invention selects hollow helix(ribbon type) agitator 3 structures can increase heat exchange area, improves heat exchange efficiency, promotes crystallization production capacity, and charging discharging is convenient; In equipment chuck, can pass into steam or refrigerant so that the advantage such as material, under optimum temperature, has efficiency high, easy to operate.
In operating process, should control charging liquid measure, the amount of moisture through once concentration evaporation, can not be greater than 80% of inlet amount, if charging is too much, pipe bottom hydrops is too much; Very little, can there is tube wall coking phenomenon in charging.Material adds after crystallizer, starts agitator, passes into cooling water, and crystallization control temperature is slowly grown up crystal, after crystal grain reaches requirement, emits magma.
Internal heat type evaporative crystallization tank of the present invention has advantages of that heat exchange area is large, circulate in tank, with short production cycle, single tank output is large etc.
Claims (9)
1. internal heat type evaporative crystallization tank, comprising: upper cover (10), tank body (11), low head (14), bearing (2); It is characterized in that: upper cover (10) be arranged on tank body (11) directly over, low head (14) be arranged on tank body (11) under, upper cover (10), tank body (11) and low head (14) form the space structure of a sealing; Bearing (2) is arranged on the both sides, below of tank body (11); Tank body (11) is upper also evenly distributedly has some visors (5).
2. internal heat type evaporative crystallization tank as claimed in claim 1, is characterized in that: described upper cover (10) is taper, and its cone top is provided with columned gas-liquid separator (7); Top one side of gas-liquid separator (7) is also provided with indirect steam outlet (8).
3. internal heat type evaporative crystallization tank as claimed in claim 1, is characterized in that: in the cone of described upper cover (10), a side is provided with blow-down pipe (6), and opposite side is also provided with hose entrance (9).
4. internal heat type evaporative crystallization tank as claimed in claim 1, is characterized in that: described low head (14) is taper, is provided with bottom open type baiting valve (1) in its cone, and a relative side is also provided with condensate water outlet (15).
5. internal heat type evaporative crystallization tank as claimed in claim 1, is characterized in that: the middle part of described tank body (11) is also provided with reinforcement (4).
6. the internal heat type evaporative crystallization tank as described in claim 1 or 5, is characterized in that: the tank body below of described reinforcement (4) is also provided with charging aperture (12).
7. internal heat type evaporative crystallization tank as claimed in claim 1, is characterized in that: the interior lower end of described tank body (11) is provided with the heater (13) of shell and tube, and middle part is provided with agitator (3).
8. the internal heat type evaporative crystallization tank as described in claim 1 or 7, is characterized in that: one end of described agitator (3) is provided with transmission device (16).
9. internal heat type evaporative crystallization tank as claimed in claim 1, is characterized in that: described upper cover (10), tank body (11), low head (14) all adopt SUS304 stainless steel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210314055.0A CN103657135A (en) | 2012-08-28 | 2012-08-28 | Internal heating type evaporative crystallization tank |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210314055.0A CN103657135A (en) | 2012-08-28 | 2012-08-28 | Internal heating type evaporative crystallization tank |
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| CN103657135A true CN103657135A (en) | 2014-03-26 |
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| CN201210314055.0A Pending CN103657135A (en) | 2012-08-28 | 2012-08-28 | Internal heating type evaporative crystallization tank |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105885914A (en) * | 2015-01-07 | 2016-08-24 | 中石化洛阳工程有限公司 | Method for recycling light hydrocarbon through atmosphere-vacuum distillation device |
| CN105885916A (en) * | 2015-01-07 | 2016-08-24 | 中石化洛阳工程有限公司 | Technology for recycling light hydrocarbon with atmospheric and vacuum distillation device |
| CN105885932A (en) * | 2015-01-07 | 2016-08-24 | 中石化洛阳工程有限公司 | Process of recycling atmospheric and vacuum distillation unit light dydrocarbon |
| CN106964169A (en) * | 2017-05-11 | 2017-07-21 | 刘向东 | Suitable for high-salt concentrated degree and have crystal separate out MVR crystallizing evaporators and its production technology |
| CN109011682A (en) * | 2018-08-31 | 2018-12-18 | 长沙点金节能环保科技有限公司 | Manganese sulfate, zinc sulfate class material MVR system-specific crystallizing evaporator and method |
| US20190055134A1 (en) * | 2016-05-26 | 2019-02-21 | Binyuan Zhu | Method and system for rapidly preparing lithium carbonate or concentrated brine using high-temperature steam |
| CN113277955A (en) * | 2021-06-21 | 2021-08-20 | 通辽梅花生物科技有限公司 | Method for extracting L-isoleucine |
-
2012
- 2012-08-28 CN CN201210314055.0A patent/CN103657135A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105885914A (en) * | 2015-01-07 | 2016-08-24 | 中石化洛阳工程有限公司 | Method for recycling light hydrocarbon through atmosphere-vacuum distillation device |
| CN105885916A (en) * | 2015-01-07 | 2016-08-24 | 中石化洛阳工程有限公司 | Technology for recycling light hydrocarbon with atmospheric and vacuum distillation device |
| CN105885932A (en) * | 2015-01-07 | 2016-08-24 | 中石化洛阳工程有限公司 | Process of recycling atmospheric and vacuum distillation unit light dydrocarbon |
| US20190055134A1 (en) * | 2016-05-26 | 2019-02-21 | Binyuan Zhu | Method and system for rapidly preparing lithium carbonate or concentrated brine using high-temperature steam |
| US10981798B2 (en) * | 2016-05-26 | 2021-04-20 | Guangzhou Ruishi Tianqi Energy Technology Co., Ltd. | Method and system for rapidly preparing lithium carbonate or concentrated brine using high-temperature steam |
| CN106964169A (en) * | 2017-05-11 | 2017-07-21 | 刘向东 | Suitable for high-salt concentrated degree and have crystal separate out MVR crystallizing evaporators and its production technology |
| CN109011682A (en) * | 2018-08-31 | 2018-12-18 | 长沙点金节能环保科技有限公司 | Manganese sulfate, zinc sulfate class material MVR system-specific crystallizing evaporator and method |
| CN113277955A (en) * | 2021-06-21 | 2021-08-20 | 通辽梅花生物科技有限公司 | Method for extracting L-isoleucine |
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Application publication date: 20140326 |