CN212476784U - Device for accelerating convection of sugar mass in crystallizing tank - Google Patents
Device for accelerating convection of sugar mass in crystallizing tank Download PDFInfo
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- CN212476784U CN212476784U CN202021455143.9U CN202021455143U CN212476784U CN 212476784 U CN212476784 U CN 212476784U CN 202021455143 U CN202021455143 U CN 202021455143U CN 212476784 U CN212476784 U CN 212476784U
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- massecuite
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- crystallizer
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- 238000010438 heat treatment Methods 0.000 claims abstract description 33
- 210000003437 trachea Anatomy 0.000 claims abstract description 16
- 210000000621 bronchi Anatomy 0.000 claims abstract description 15
- 238000002425 crystallisation Methods 0.000 claims description 18
- 230000008025 crystallization Effects 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 230000001105 regulatory effect Effects 0.000 claims description 10
- 230000001954 sterilising effect Effects 0.000 claims description 5
- 238000009835 boiling Methods 0.000 abstract description 16
- 238000003756 stirring Methods 0.000 abstract description 8
- 238000004064 recycling Methods 0.000 abstract description 2
- 238000009923 sugaring Methods 0.000 abstract description 2
- 239000006071 cream Substances 0.000 abstract 3
- 239000007789 gas Substances 0.000 description 39
- 230000000694 effects Effects 0.000 description 11
- 238000000034 method Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000004659 sterilization and disinfection Methods 0.000 description 4
- 230000002349 favourable effect Effects 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000010907 mechanical stirring Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000001125 extrusion Methods 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 238000004887 air purification Methods 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The utility model belongs to industry sugaring field, concretely relates to a device that is used for crystallizer massecuite convection current with higher speed, characterized in that still is equipped with annular trachea in the crystallizer, annular trachea and heating member are concentric and the level sets up under the heating member, and annular trachea upper portion is equipped with the micropore that the aperture is 0.005-1mm, and the micropore quantity intensity that sets up on the tracheal pipeline direction of edge annular is not less than 2000/m, and annular trachea is equipped with the bronchus that communicates with the crystallizer outward, and noncondensable gas discharge pipe connects deareator, deareator's gas delivery outlet is connected to the bronchus. The device is used for boiling the strong convection gas of sugar and cream of the sugar crystallizing tank by recycling the non-condensable gas discharged by the heating body, can stir the sugar and cream, can heat the sugar and cream by using heat energy, and saves energy. When the non-condensable gas is insufficient, the treated air can be supplemented to blow the massecuite.
Description
Technical Field
The utility model belongs to industry sugaring field, concretely relates to a device that is used for crystallizer massecuite to convect with higher speed.
Background
In the sugar production process, sugar boiling and crystallization are a crucial link in the process flow. A traditional sugar boiling mode adopts a natural circulation crystallizing tank, sugar liquor is continuously heated and concentrated in a crystallizing tank with vacuum, crystals are formed after a certain saturated concentration is reached (or fine sugar particles are added), liquid must keep convection in the boiling process, the convection speed is higher, the concentration is higher, the crystallization is accelerated, the boiling time is shorter, and the convection of the sugar liquor in the existing crystallizing tank is formed by depending on vacuum, gravity and heating temperature difference.
In recent years, with the progress of sugar manufacturing technology, under the condition that the heating temperature of a crystallization tank is limited, mechanical forced stirring is added in the crystallization tank to accelerate sugar solution convection, a propeller principle is adopted to push down sugar paste, and referring to fig. 3, the sugar paste is accelerated in convection by external force, but the mechanical forced stirring has many defects, such as high power consumption (each set of forced stirring is provided with a 55kw/75kw motor), vacuum leakage of a dynamic and static mechanical connection part, mechanical faults (large resistance of a stirring blade, deformation and bending, and heating of the motor), and other safe operation and maintenance problems, and influences the normal use of the crystallization tank. In addition, the heating body in the existing sugar crystallizing tank discharges non-condensing gas (ammonia gas as the main component) in the working process, the condensing gas has certain pressure (more than or equal to 0.006 mPa) and temperature (more than or equal to 90 ℃), and the heat energy is wasted when the condensing gas is extracted and discharged.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a device that is used for crystallizer massecuite convection current with higher speed to solve and use the high technical problem of the high maintenance cost of mechanical stirring power consumption in the current sugar crystallization process of boiling.
The technical proposal for realizing the purpose of the utility model is that,
the utility model provides a device for crystallizer massecuite convection with higher speed, including the heating member, be equipped with the noncondensable gas discharge pipe with the heating member intercommunication outside the crystallizer, different with prior art, still be equipped with annular trachea in the crystallizer, annular trachea and heating member concentric and the level setting is under the heating member, annular trachea upper portion is equipped with the micropore that the aperture is 0.005-1mm, the micropore quantity intensity that sets up on the tracheal pipeline direction of edge annular is not less than 2000/m, annular trachea is equipped with the bronchus with the crystallizer intercommunication outward, noncondensable gas discharge pipe connects the gas-water separator, the gas delivery outlet of gas-water separator is connected to the bronchus.
Furthermore, the device also comprises an air input pipeline, wherein a purification and sterilization device and a constant temperature heating device are arranged in the air pipeline along the air input direction, an air regulating valve is arranged on the air input pipeline, and the air input pipeline is communicated with the bronchus.
Furthermore, the distance between the annular air pipe and the heating body is 0-1000 mm.
Furthermore, 1-6 annular gas pipes with different diameters are arranged in the crystallizing tank.
Further, set up 2 annular trachea in the crystallizer, 2 annular trachea settings are on same horizontal plane, and 2 annular trachea's diameter is one-third and two-thirds of crystallizer internal diameter respectively, be equipped with the input governing valve in the bronchus.
Further, the micropores are taper micropores.
Further, the specification of the annular air pipe is DN15-DN 300.
When the device for the sugar mass accelerated convection of the crystallizing tank is used, the gas-water separator dries the non-condensable gas discharged by the heating body and then outputs the dry gas, the dry gas enters the annular gas pipe in the crystallizing tank and is discharged from the micropores on the wall of the annular gas pipe, the volume of the dry gas is continuously increased in the lifting process under the combined action of vacuum and self pressure at the upper part in the sugar boiling crystallizing tank, the sugar mass is driven to flow in extrusion and lifting, and the sugar mass is continuously stirred. When the non-condensing gas is insufficient, the annular air pipe can be mixed with input air, and the input air is firstly purified, sterilized and heated to the same temperature as the massecuite in the sugar boiling crystallizing tank. A plurality of annular air pipes with different diameters are arranged below the heating body, so that the action range of gas for accelerating the convection of massecuite is enlarged. The input regulating valve is arranged on the bronchus, which is favorable for accurately regulating the strength of convection of gas acceleration massecuite in each area. The micropore is set to be a taper hole, which is beneficial to preventing massecuite from entering the annular air pipe.
The device for accelerating the convection of the massecuite of the sugar boiling crystallizing tank is used for strong convection gas of the massecuite of the sugar boiling crystallizing tank by recycling the non-condensable gas discharged by the heating body, can be used for stirring the massecuite, can be used for heating the massecuite by using heat energy, does not waste the heat energy, accords with the food safety, and does not influence the quality of the massecuite. When the non-condensable gas is insufficient, the treated air can be supplemented to blow the massecuite. The use of the gas injection device utilizes the exhausted waste heat, thus saving energy.
The air consists of 78% nitrogen and 21% oxygen, 0.94% rare gas, 0.03% carbon dioxide, 0.03% water vapor, and impurities such as air. From the above composition of air it can be demonstrated that:
1. firstly, the air contains few impurities, and the impurities can be filtered and removed by adopting an air purification device, so that clean air can enter a sugar boiling tank;
2. the water content in the air is 0.03%, and the average water content in the air can be calculated according to the average air temperature of 25 ℃ and the average relative humidity of 80% in the Guangxi squeezing season: 80% × 20.356 × 1.185=0.019 kg/cubic meter, negligible;
3. after the air is purified, the air in a normal temperature state can be heated to more than 110 ℃ in an electric heating mode, so that the effects of disinfection and sterilization are achieved, and the food safety is ensured; keeping the air temperature the same as the massecuite temperature in the sugar boiling crystallizing tank to ensure input;
4. except nitrogen, oxygen, water vapor and carbon dioxide, the rest gases in the air belong to inert gases, and the quality of the massecuite is not influenced.
Because the effect that can also reach the energy saving simultaneously as the strong convection gas of massecuite of noncondensable gas in the steam of adoption, can preferentially use noncondensable gas in the scheme, not enough part air of resupplying again, with the mode of the mechanical stirring massecuite among the prior art, this technical scheme energy-conserving effect is obvious, uses gaseous jetting massecuite, promotes the massecuite convection current effect better.
It should be noted that, the most commonly used cylindrical crystallization tank in the field correspondingly adopts a cylindrical heating body, and the technical solutions of non-invasive property made by the skilled person according to the disclosure of the present invention for crystallization tanks of other shapes all belong to the present invention.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention;
FIG. 2 is a schematic cross-sectional view of a crystallization tank according to an embodiment of the present invention;
FIG. 3 is a schematic structural view of a prior art sugar boiling crystallizer;
in the figure, 1, a crystallizing tank; 2. a heating body; 3. an annular air pipe; 3-1, bronchi; 3-10, inputting a regulating valve; 4. a gas-water separator; 5. an air regulating valve; 6. a purification and sterilization device; 7. a constant temperature heating device.
Detailed Description
The present invention will be described in detail with reference to examples.
Referring to fig. 1 to 3, the boiled sugar of the present embodiment is 55m3The crystallization tank (1) is provided with a crystallization tank,
a device for accelerating convection of massecuite in a crystallizing tank comprises a heating body 2, a noncondensable gas discharge pipe communicated with the heating body 2 is arranged outside the crystallizing tank 1, 2 annular air pipes 3 of DN76 are arranged in the crystallizing tank 1, the diameters of the 2 annular air pipes 3 are respectively one third and two thirds of the inner diameter of the crystallizing tank 1, the 2 annular air pipes 3 and the heating body 2 are concentric and horizontally arranged under the heating body 2, the diameters of the 2 annular air pipes are reasonably arranged to ensure that the annular air pipes are uniformly distributed in the crystallizing tank, the upper part of the annular air pipe 3 is provided with taper micropores with the aperture of 0.02mm, the reasonable arrangement of the pore diameter and the shape of the micropores is favorable for ensuring proper spray intensity and effectively preventing the massecuite from flowing into the annular air pipes, the number concentration of the taper micropores is 50000 per meter in the pipeline direction, the number of the micropores with high density is favorable for improving the uniformity of acting force for accelerating convection of the massecu, so that the convection effect of massecuite is better, 2 annular gas pipes 3 are respectively provided with a bronchus 3-1 communicated with the outside of the crystallizing tank 1, an input adjusting valve 3-10 is arranged in the bronchus 3-1, a non-condensable gas discharge pipeline is connected with a gas-water separator 4, the bronchus 3-1 is connected with a gas output port of the gas-water separator 4,
the branch air pipe 3-1 is also communicated with an air input pipeline, a purifying and sterilizing device 6 and a constant temperature heating device 7 are arranged in the air pipeline along the air input direction, an air regulating valve 5 is arranged on the air input pipeline,
the annular gas tube 3 is spaced from the heating body 2 by a distance of 250mm, which is the best distance for accelerating the convection of massecuite through the heating body 2.
When the device for accelerating convection of the massecuite in the crystallizing tank is used, the gas-water separator 4 performs gas-water separation and drying on input non-condensable gas and outputs dry gas, the dry gas enters the annular gas pipe 3 and is discharged from the taper micropores, and under the combined action of the self pressure of the gas and the vacuum on the upper part of the crystallizing tank 1, the volume of the gas is continuously increased in the rising process, the massecuite is driven to flow in extrusion and lifting, and the massecuite is continuously stirred. The boiling intensity of the massecuite and the vacuum degree in the crystallization tank 1 can be observed through a sight glass to judge that the gas amount in the tank is proper, and when the non-condensed gas is not enough, the air regulating valve 5 can be opened simultaneously, and proper amount of treated air is mixed and input into the bronchus 3-1 to ensure the boiling intensity of the massecuite. The input regulating valve 3-10 in the bronchus 3-1 can be regulated to respectively regulate the boiling degree of the massecuite at the center and the periphery in the crystallizing tank 1, so as to improve the crystallization effect of the massecuite and be beneficial to improving the product quality. The device replaces mechanical stirring, can effectively improve the maintainability of the sugar crystallizing tank, has better effect of accelerating the convection of massecuite and has obvious effect of saving energy. With one 55m3For example, the power distribution machine of the gas strong convection device of the crystallization tank is about 3-5 kw, which is 50kw less than that of the forced stirring 55kw motor, and the power consumption is 50 every day60 percent x 20 hours x 0.65 yuan/degree =390 yuan, the squeezing season is about 39000 yuan per 100 days, and the electricity-saving effect is obvious. The device can replace a forced stirring device, reduce the power consumption, has remarkable energy-saving effect and considerable economic benefit, and is an energy-saving reconstruction project with less investment and quick effect for sugar manufacturing enterprises.
Claims (7)
1. The utility model provides a device for crystallizer massecuite convection with higher speed, including the heating member, be equipped with the noncondensable gas discharge pipe with the heating member intercommunication outside the crystallizer, characterized in that, still be equipped with annular trachea in the crystallizer, annular trachea and heating member concentric and the level setting is under the heating member, annular trachea upper portion is equipped with the micropore that the aperture is 0.005-1mm, the micropore quantity concentration that sets up in annular trachea's pipeline direction is not less than 2000/m, annular trachea is equipped with the bronchus with the crystallizer intercommunication outward, noncondensable gas discharge pipe connects the gas-water separator, the gas delivery outlet of gas-water separator is connected to the bronchus.
2. The apparatus as set forth in claim 1, further comprising an air supply line, said air supply line being provided with a sterilizing unit and a constant temperature heating unit along an air supply direction, said air supply line being provided with an air control valve, said air supply line being communicated with said branch pipe.
3. The apparatus for accelerated convection of massecuite for crystallization pots as claimed in claim 1 or 2, wherein said circular air tube is spaced from the heating body by 0 to 1000 mm.
4. The apparatus as claimed in claim 1 or 2, wherein 2-6 circular air tubes with different diameters are provided in the crystallization tank.
5. The apparatus as claimed in claim 1 or 2, wherein 2 annular air pipes are provided in the crystallization tank, the 2 annular air pipes are provided on the same horizontal plane, the diameters of the 2 annular air pipes are one third and two thirds of the inner diameter of the crystallization tank, respectively, and the inlet regulating valve is provided in the branch air pipe.
6. The apparatus for accelerated convection in crystallizer massecuite as claimed in claim 1 or 2, wherein said micropores are tapered micropores.
7. The apparatus for accelerated convection in massecuite crystallizers according to claim 1 or 2, wherein said annular air tube has a size of DN15-DN 300.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021455143.9U CN212476784U (en) | 2020-07-22 | 2020-07-22 | Device for accelerating convection of sugar mass in crystallizing tank |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202021455143.9U CN212476784U (en) | 2020-07-22 | 2020-07-22 | Device for accelerating convection of sugar mass in crystallizing tank |
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| CN212476784U true CN212476784U (en) | 2021-02-05 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111733299A (en) * | 2020-07-22 | 2020-10-02 | 广西飞鹏节能环保科技有限公司 | Apparatus and method for accelerated convection of massecuite in crystallization tank |
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- 2020-07-22 CN CN202021455143.9U patent/CN212476784U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111733299A (en) * | 2020-07-22 | 2020-10-02 | 广西飞鹏节能环保科技有限公司 | Apparatus and method for accelerated convection of massecuite in crystallization tank |
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