CN111820408A - Production system and production method for simultaneously producing calcium propionate particles and calcium propionate powder - Google Patents
Production system and production method for simultaneously producing calcium propionate particles and calcium propionate powder Download PDFInfo
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- CN111820408A CN111820408A CN201910308300.9A CN201910308300A CN111820408A CN 111820408 A CN111820408 A CN 111820408A CN 201910308300 A CN201910308300 A CN 201910308300A CN 111820408 A CN111820408 A CN 111820408A
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- BCZXFFBUYPCTSJ-UHFFFAOYSA-L Calcium propionate Chemical compound [Ca+2].CCC([O-])=O.CCC([O-])=O BCZXFFBUYPCTSJ-UHFFFAOYSA-L 0.000 title claims abstract description 41
- 235000010331 calcium propionate Nutrition 0.000 title claims abstract description 41
- 239000004330 calcium propionate Substances 0.000 title claims abstract description 41
- 239000000843 powder Substances 0.000 title claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 239000002245 particle Substances 0.000 title claims description 31
- 238000001035 drying Methods 0.000 claims abstract description 62
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 25
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 23
- 239000000428 dust Substances 0.000 claims abstract description 16
- 238000001694 spray drying Methods 0.000 claims abstract description 11
- 239000008187 granular material Substances 0.000 claims abstract 8
- 239000000463 material Substances 0.000 claims description 27
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 239000007788 liquid Substances 0.000 claims description 21
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 12
- 230000002829 reductive effect Effects 0.000 claims description 11
- 239000007787 solid Substances 0.000 claims description 11
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 claims description 10
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 8
- 239000000920 calcium hydroxide Substances 0.000 claims description 8
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 8
- 235000011116 calcium hydroxide Nutrition 0.000 claims description 8
- 239000011324 bead Substances 0.000 claims description 7
- 239000012153 distilled water Substances 0.000 claims description 7
- 238000001914 filtration Methods 0.000 claims description 7
- 238000002360 preparation method Methods 0.000 claims description 7
- 230000003472 neutralizing effect Effects 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 235000019260 propionic acid Nutrition 0.000 claims description 5
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 3
- 239000012295 chemical reaction liquid Substances 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 2
- 238000011017 operating method Methods 0.000 abstract 1
- 230000001276 controlling effect Effects 0.000 description 4
- 235000013305 food Nutrition 0.000 description 4
- 238000010924 continuous production Methods 0.000 description 3
- 239000013078 crystal Substances 0.000 description 3
- 244000144972 livestock Species 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 244000052616 bacterial pathogen Species 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000008520 organization Effects 0.000 description 2
- 230000003449 preventive effect Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 229930195730 Aflatoxin Natural products 0.000 description 1
- XWIYFDMXXLINPU-UHFFFAOYSA-N Aflatoxin G Chemical compound O=C1OCCC2=C1C(=O)OC1=C2C(OC)=CC2=C1C1C=COC1O2 XWIYFDMXXLINPU-UHFFFAOYSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 239000005409 aflatoxin Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003925 fat Substances 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 235000013373 food additive Nutrition 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 238000011085 pressure filtration Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L33/00—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof
- A23L33/10—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof using additives
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23K—FODDER
- A23K20/00—Accessory food factors for animal feeding-stuffs
- A23K20/10—Organic substances
- A23K20/105—Aliphatic or alicyclic compounds
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23K—FODDER
- A23K20/00—Accessory food factors for animal feeding-stuffs
- A23K20/20—Inorganic substances, e.g. oligoelements
- A23K20/24—Compounds of alkaline earth metals, e.g. magnesium
-
- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L3/00—Preservation of foods or foodstuffs, in general, e.g. pasteurising, sterilising, specially adapted for foods or foodstuffs
- A23L3/34—Preservation of foods or foodstuffs, in general, e.g. pasteurising, sterilising, specially adapted for foods or foodstuffs by treatment with chemicals
- A23L3/3454—Preservation of foods or foodstuffs, in general, e.g. pasteurising, sterilising, specially adapted for foods or foodstuffs by treatment with chemicals in the form of liquids or solids
- A23L3/3463—Organic compounds; Microorganisms; Enzymes
- A23L3/3481—Organic compounds containing oxygen
- A23L3/3508—Organic compounds containing oxygen containing carboxyl groups
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- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
- A23L33/00—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof
- A23L33/10—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof using additives
- A23L33/16—Inorganic salts, minerals or trace elements
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- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23P—SHAPING OR WORKING OF FOODSTUFFS, NOT FULLY COVERED BY A SINGLE OTHER SUBCLASS
- A23P10/00—Shaping or working of foodstuffs characterised by the products
- A23P10/20—Agglomerating; Granulating; Tabletting
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- A—HUMAN NECESSITIES
- A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
- A23P—SHAPING OR WORKING OF FOODSTUFFS, NOT FULLY COVERED BY A SINGLE OTHER SUBCLASS
- A23P10/00—Shaping or working of foodstuffs characterised by the products
- A23P10/40—Shaping or working of foodstuffs characterised by the products free-flowing powder or instant powder, i.e. powder which is reconstituted rapidly when liquid is added
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- Life Sciences & Earth Sciences (AREA)
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- Inorganic Chemistry (AREA)
- Mycology (AREA)
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- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The utility model provides a production system and production method of coproduction calcium propionate granule and powder, includes heater, air-blower, spray drying tower and neutralization tank, the air intake connection air-blower of heater, spray drying tower are connected to the air outlet, and cyclone is connected to the drying tower, cyclone and water film dust remover, simultaneously cyclone's air inlet and air outlet are connected, cyclone's gas outlet is connected the water film dust remover, be connected through the draught fan between cyclone's gas outlet and the water film dust remover, can produce calcium propionate granule and powder respectively simultaneously bottom the drying tower and cyclone bottom, reduce artifical consumption and operating procedure.
Description
Technical Field
The invention relates to the technical field of food additives, in particular to a production system and a production method for simultaneously producing calcium propionate particles and powder.
Background
Calcium propionate is a safe and reliable food and feed mildew preventive approved by the World Health Organization (WHO) and the Food and Agriculture Organization (FAO) of the United nations. The calcium propionate can be absorbed by human and livestock through metabolism like other fats and supplies calcium necessary for human and livestock, which is superior to other mildewproof agents, has stronger inhibiting effect on various moulds, gram-negative bacilli or aerobic bacilli in an acid medium (starch, substances containing protein and grease), can inhibit the generation of aflatoxin, is harmless to yeast, is harmless to human and livestock, and has no toxic or side effect. Is a novel, safe and efficient mildew preventive for food and feed in the aspects of food, brewing, feed and traditional Chinese medicine preparation.
The current production process of calcium propionate: adding the screened lime powder and water into a reaction kettle, putting propionic acid into the reaction kettle from an acid head tank regularly and quantitatively under the stirring condition, reacting under the specified condition, filtering residues of the materials through a vacuum filter after complete reaction, putting the materials into a filtrate head tank for later use, continuously putting mother liquor into a concentration kettle through the head tank for evaporation, concentration and crystallization, continuously taking out crystals, putting the crystals into a rotary drum centrifuge for liquid removal treatment, sending wet materials after liquid removal into a dryer, and crushing, detecting, metering and packaging the dried materials to obtain the finished product.
The prior art can not realize continuous production in the production process, and has complicated working procedures, for example, the produced crystals need to be crushed and ground to produce corresponding powder and particles.
Disclosure of Invention
The technical problem to be solved by the invention is to provide a production system and a production method for simultaneously producing calcium propionate particles and powder, the process realizes continuous production, reduces labor consumption and complicated steps, simultaneously produces the calcium propionate powder and particles, and has high purity and stable quality.
The technical scheme of the invention is as follows:
the production system for simultaneously producing the calcium propionate particles and the calcium propionate powder is characterized by comprising a heater, an air blower, a spray drying tower and a neutralizing tank, wherein an air inlet of the heater is connected with the air blower, an air outlet of the heater is connected with the spray drying tower, the spray drying tower comprises a drying chamber, the drying chamber is barrel-shaped, the bottom of the drying chamber is conical, an air distributor is installed at the top of the drying chamber, a centrifugal atomizer is arranged at the center of the inner side of the top of the drying chamber and is connected with a feed pump, the feed pump is connected with the neutralizing tank, the air distributor is communicated with the drying chamber through hot air channels, the hot air channels are two groups and are symmetrically arranged at two sides of the centrifugal atomizer, the bottom of the drying chamber is provided with an air outlet, the air outlet is connected with a cyclone separator, the cyclone separator and a water film dust collector are arranged, and meanwhile, the air outlet of the cyclone separator is connected with the water film dust collector, and the air outlet of the cyclone separator is connected with the water film dust collector through an induced draft fan.
Further, the air outlet is arranged at the conical part 1/2 at the bottom of the drying chamber.
Further, the hot air channel air inlet angle is 30 degrees.
Furthermore, a plurality of groups of oscillators are arranged on the outer side of the bottom of the drying chamber.
Further, the heater is a transverse heater.
A production method for simultaneously producing calcium propionate particles and powder is characterized by comprising a reaction liquid preparation stage, a centrifugal drying stage and a material collection stage, and comprises the following specific operation steps:
firstly, a preparation reaction stage:
(1) a reaction stage: fully and uniformly mixing slaked lime and distilled water in a neutralization tank, heating to 50-80 ℃ to completely dissolve the slaked lime and the distilled water, dropwise adding propionic acid to perform a neutralization reaction, and controlling the pH value of a reaction end point to be 7.0-9.0 to obtain a calcium propionate solution, wherein the solid content of the calcium propionate solution is 30-35%;
(2) and (3) a filtering stage: after the reaction is finished, adding activated carbon into a neutralization tank, filtering the calcium propionate solution, adding 2-4 kg of activated carbon into the neutralization tank, stopping stirring after 20min, pumping the materials in the neutralization tank into a filter press by a gear pump after the reaction is finished, and conveying the filtered calcium propionate solution into the neutralization tank by the pump;
II, centrifugal drying:
(1) a preheating stage: a valve at the feed opening of the cyclone separator is closed, a heater and a blower are turned on to enable the temperature of inlet air in an air inlet channel at the top of the drying chamber to reach 180-220 ℃, the air inlet speed is kept at 10.8-13.8 m/s, and hot air uniformly circles around the drying chamber in a spiral shape;
(2) a feeding stage: starting a centrifugal atomizer, starting a feeding pump when the centrifugal atomizer reaches the highest rotation speed of 1000r/min, adding feed liquid, gradually increasing the feeding amount from small to large, adjusting to 3-5 m/h, wherein the feeding temperature is 50 ℃, and meanwhile, starting an induced draft fan, an oscillator and valves at a feed opening to keep the air outlet temperature at the bottom of a drying chamber at 60-80 ℃ and the air outlet speed at 3.6-5 m/s;
thirdly, material collection stage:
(1) particle receiving stage: the feed liquid is sprayed out through a centrifugal atomizer to form vaporous liquid beads, the vaporous liquid beads are dried in a drying chamber under the action of hot air to form solid particles, and the solid particles are sprayed to the bottom of the drying chamber and discharged from the bottom of the drying chamber;
(2) and (3) a powder receiving stage: the air outlet sucks materials smaller than 5mm into the cyclone separator, and the cyclone separator deposits solid particles with the particle diameter of 0.5mm-0.1mm to the bottom for discharge.
Furthermore, the air outlet temperature and the feeding amount are in inverse proportion in the material collecting stage, the feeding amount is reduced, the outlet temperature can be increased, the feeding amount is increased, and the outlet temperature can be reduced.
Furthermore, after the use is finished, the heater is firstly closed, the feed liquid is replaced by water to wash residual materials in the pipeline, then the feed pump is closed, when the temperature of inlet air is reduced to be below 100 ℃, the operation of the air feeder and the exhaust fan can be stopped, the residual materials in the drying chamber and the cyclone separator are treated, the dust remover and the oscillator are closed, and finally the main power supply is closed, so that the production operation is finished.
The invention has the beneficial effects that: the reaction process is continuous, the evaporation link of the traditional process is reduced, direct heating and drying are realized, the consumption is low, the continuous production of the calcium propionate is realized, particles and powder can be produced simultaneously, and the labor consumption can be reduced.
Drawings
FIG. 1 is a schematic view of the structure of the present invention.
In the figure:
the drying device comprises a heater 1, an air blower 2, a drying chamber 3, an air distributor 4, a centrifugal atomizer 5, a hot air channel 6, a cyclone separator 7, an induced draft fan 8, a water film dust collector 9, an oscillator 10, a feeding pump 11 and an air outlet 12.
Detailed Description
The invention is further described with reference to the following description and embodiments in conjunction with the accompanying drawings.
The production system for simultaneously producing the calcium propionate particles and the calcium propionate powder is characterized by comprising a heater 1, an air blower 2, a spray drying tower and a neutralizing tank, wherein an air inlet of the heater 1 is connected with the air blower 2, an air outlet of the heater is connected with the spray drying tower, the spray drying tower comprises a drying chamber 3, the drying chamber 3 is barrel-shaped, the bottom of the drying chamber is conical, an air distributor 4 is installed at the top of the drying chamber 3, a centrifugal atomizer 5 is arranged at the center of the inner side of the top of the drying chamber 3, the centrifugal atomizer 5 is connected with a feed pump 11, the feed pump is connected with the neutralizing tank, the air distributor 5 is communicated with the drying chamber through hot air channels 6, the hot air inlet angles of the hot air channels are 30 degrees, the hot air channels 6 are two groups and are symmetrically arranged at two sides of the centrifugal atomizer 5, an air outlet 12 is arranged at the bottom, cyclone 7 and water film dust collector 9, simultaneously the air inlet and the air outlet 11 of cyclone 7 are connected, cyclone's gas outlet is connected water film dust collector 9, cyclone's gas outlet and water film dust collector 9 are connected through draught fan 8 between are connected.
Further, the air outlet 12 is arranged at the conical part 1/2 at the bottom of the drying chamber.
Further, a plurality of groups of oscillators 10 are arranged on the outer side of the bottom of the drying chamber 3.
Further, the heater 1 is a lateral heater.
When the device is used, propionic acid, hydrated lime and distilled water react in a neutralization tank, the reaction is carried out, the calcium propionate solution after pressure filtration flows to a low-level tank and is stored in a neutralization tank, a feed pump 11 sends feed liquid into a centrifugal atomizer 5, an air heater 1 is used for heating and enters an air distributor at the top of a drying chamber 3, hot air uniformly enters the drying chamber in a spiral shape, the centrifugal atomizer 5 at the top of the feed liquid drying chamber 3 sprays the feed liquid into superfine atomized liquid beads (in a rotating mode) and can be dried into a finished product in a short time in parallel flow contact with the hot air, the finished product is particles and powder, the particles are continuously discharged from the bottom of the drying chamber 3, the powder is output from a cyclone separator 7, and waste gas is discharged by an induced draft fan 8.
A production method for simultaneously producing calcium propionate particles and powder is characterized by comprising a reaction liquid preparation stage, a centrifugal drying stage and a material collection stage, wherein the specific operation steps, specific reaction conditions and specific reaction time are as follows:
firstly, a preparation reaction stage:
(1) a reaction stage: adding distilled water into a neutralization tank, starting a stirring paddle, adding 1600 kg of hydrated lime while stirring, wherein the mass ratio of the hydrated lime to the distilled water is 1: and 8, opening a temperature regulating valve, controlling the temperature in the neutralization tank to be kept at 50 ℃ until the slaked lime in the neutralization tank is completely melted, stopping heating, dropwise adding 3000 kg of propionic acid with the mass fraction of 99% into the neutralization tank at the moment, controlling the reaction temperature to be 50-80 ℃, controlling the end point pH of the reaction material to be 7-9, and keeping the temperature for 1 hour.
(2) And (3) a filtering stage: and after the reaction is finished, adding activated carbon into the neutralization tank, filtering the calcium propionate solution, adding 4kg of activated carbon into the neutralization tank, stopping stirring after 20min, pumping the materials in the neutralization tank into a filter press by a gear pump after the reaction is finished, and conveying the filtered calcium propionate solution to the neutralization tank by the pump.
II, centrifugal drying:
(1) a preheating stage: the valve at the feed opening of the cyclone separator is closed, the heater and the blower are turned on to ensure that the inlet air temperature in the inlet air channel at the top of the drying chamber reaches 200 ℃, the inlet air speed is kept at 12m/s, and the hot air uniformly circles around in the drying chamber in a spiral shape.
(2) A feeding stage: starting a centrifugal atomizer, starting a feeding pump when the centrifugal atomizer reaches the highest rotation speed of 1000r/min, adding feed liquid, gradually increasing the feeding amount from small to large, adjusting to 4 m/h, wherein the feeding temperature is 50 ℃, and meanwhile, starting an induced draft fan, an oscillator and valves at a blanking opening to keep the air outlet temperature at 60 ℃ and the air outlet speed at 4m/s at the bottom of a drying chamber;
thirdly, material collection stage:
(1) particle receiving stage: the feed liquid is sprayed out through a centrifugal atomizer to form vaporous liquid beads, the vaporous liquid beads are dried in a drying chamber under the action of hot air to form solid particles, and the solid particles are sprayed to the bottom of the drying chamber and discharged from the bottom of the drying chamber;
(2) and (3) a powder receiving stage: the air outlet sucks materials smaller than 5mm into the cyclone separator, and the cyclone separator deposits solid particles with the particle diameter of 0.5mm-0.1mm to the bottom for discharge.
Furthermore, the air outlet temperature and the feeding amount are in inverse proportion in the material collecting stage, the feeding amount is reduced, the outlet temperature can be increased, the feeding amount is increased, and the outlet temperature can be reduced.
Furthermore, after the use is finished, the heater is firstly closed, the feed liquid is replaced by water to wash residual materials in the pipeline, then the feed pump is closed, when the temperature of inlet air is reduced to be below 100 ℃, the operation of the air feeder and the exhaust fan can be stopped, the residual materials in the drying chamber and the cyclone separator are treated, the dust remover and the oscillator are closed, and finally the main power supply is closed, so that the production operation is finished.
The water content of the calcium propionate is less than or equal to 9.5 percent and the content of the effective components is more than or equal to 99.0 percent.
Finally, it should be noted that the above-mentioned embodiments are only for illustrating the technical solutions of the present invention and not for limiting, and although the present invention has been described in detail with reference to the preferred embodiments, it should be understood by those skilled in the art that modifications or equivalent substitutions may be made to the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention, which should be covered by the claims of the present invention.
Claims (8)
1. The production system for simultaneously producing the calcium propionate particles and the calcium propionate powder is characterized by comprising a heater, an air blower, a spray drying tower and a neutralizing tank, wherein an air inlet of the heater is connected with the air blower, an air outlet of the heater is connected with the spray drying tower, the spray drying tower comprises a drying chamber, the drying chamber is barrel-shaped, the bottom of the drying chamber is conical, an air distributor is installed at the top of the drying chamber, a centrifugal atomizer is arranged at the center of the inner side of the top of the drying chamber and is connected with a feed pump, the feed pump is connected with the neutralizing tank, the air distributor is communicated with the drying chamber through hot air channels, the hot air channels are two groups and are symmetrically arranged at two sides of the centrifugal atomizer, the bottom of the drying chamber is provided with an air outlet, the air outlet is connected with a cyclone separator, the cyclone separator and a water film dust collector are arranged, and meanwhile, the air outlet of the cyclone separator is connected with the water film dust collector, and the air outlet of the cyclone separator is connected with the water film dust collector through an induced draft fan.
2. The system of claim 1, wherein the air outlet is disposed at the bottom of the drying chamber at the taper 1/2.
3. The system for simultaneously producing granules and powder of calcium propionate as claimed in claim 1, wherein the air inlet angle of said hot air channel is 30 °.
4. The system for simultaneously producing granules and powder of calcium propionate according to claim 1, wherein the bottom of said drying chamber is provided with a plurality of sets of oscillators.
5. The system of claim 1, wherein the heater is a lateral heater.
6. The method for producing the calcium propionate particles and the powder by the production system for simultaneously producing the calcium propionate particles and the powder according to any one of claims 1 to 5, which is characterized by comprising a reaction liquid preparation stage, a centrifugal drying stage and a material collection stage, and comprises the following specific operation steps:
firstly, a preparation reaction stage:
(1) a reaction stage: fully and uniformly mixing slaked lime and distilled water in a neutralization tank, heating to 50-80 ℃ to completely dissolve the slaked lime and the distilled water, dropwise adding propionic acid to perform a neutralization reaction, and controlling the pH value of a reaction end point to be 7.0-9.0 to obtain a calcium propionate solution, wherein the solid content of the calcium propionate solution is 30-35%;
(2) and (3) a filtering stage: after the reaction is finished, adding activated carbon into a neutralization tank, filtering the calcium propionate solution, adding 2-4 kg of activated carbon into the neutralization tank, stopping stirring after 20min, pumping the materials in the neutralization tank into a filter press by a gear pump after the reaction is finished, and conveying the filtered calcium propionate solution into the neutralization tank by the pump;
II, centrifugal drying:
(1) a preheating stage: a valve at the feed opening of the cyclone separator is closed, a heater and a blower are turned on to enable the temperature of inlet air in an air inlet channel at the top of the drying chamber to reach 180-220 ℃, the air inlet speed is kept at 10.8-13.8 m/s, and hot air uniformly circles around the drying chamber in a spiral shape;
(2) a feeding stage: starting a centrifugal atomizer, starting a feeding pump when the centrifugal atomizer reaches the highest rotation speed of 1000r/min, adding feed liquid, gradually increasing the feeding amount from small to large, adjusting to 3-5 m/h, wherein the feeding temperature is 50 ℃, and meanwhile, starting an induced draft fan, an oscillator and valves at a feed opening to keep the air outlet temperature at the bottom of a drying chamber at 60-80 ℃ and the air outlet speed at 3.6-5 m/s;
thirdly, material collection stage:
(1) particle receiving stage: the feed liquid is sprayed out through a centrifugal atomizer to form vaporous liquid beads, the vaporous liquid beads are dried in a drying chamber under the action of hot air to form solid particles, and the solid particles are sprayed to the bottom of the drying chamber and discharged from the bottom of the drying chamber;
(2) and (3) a powder receiving stage: the air outlet sucks materials smaller than 5mm into the cyclone separator, and the cyclone separator deposits solid particles with the particle diameter of 0.5mm-0.1mm to the bottom for discharge.
7. The method for producing calcium propionate granules and powder by using the production system for simultaneously producing calcium propionate granules and powder as claimed in claim 6, wherein the outlet temperature is inversely proportional to the feeding amount in the material collection stage, the feeding amount is reduced, the outlet temperature is increased, the feeding amount is increased, and the outlet temperature is reduced.
8. The method for producing calcium propionate granules and powder by using the production system for simultaneously producing calcium propionate granules and powder as claimed in claim 6, wherein after the material collection stage is finished, the heater is first turned off, the feed liquid is replaced by water to flush the residual materials in the pipeline, then the feed pump is turned off, the operation of the air blower and the air exhaust fan can be stopped when the temperature of the inlet air is reduced to below 100 ℃, the residual materials in the drying chamber and the cyclone separator are treated, the dust collector and the oscillator are turned off, and finally the main power supply is turned off, so that the production operation is completed.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117018649A (en) * | 2023-10-09 | 2023-11-10 | 山西旺龙药业集团有限公司 | Medicinal hericium erinaceus mycelium spray drying tower and application method thereof |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101665425A (en) * | 2009-09-25 | 2010-03-10 | 如皋市江北添加剂有限公司 | Production process of calcium propionate and drying tower thereof |
| CN202770142U (en) * | 2012-08-09 | 2013-03-06 | 南京扬子精细化工有限责任公司 | Calcium propionate drying device |
| CN106946687A (en) * | 2017-03-06 | 2017-07-14 | 山东省同泰维润食品科技有限公司 | A kind of calcium propionate continuous automatic production system and its production method |
| CN107754360A (en) * | 2017-11-29 | 2018-03-06 | 慈溪市舒润卫浴实业有限公司 | A kind of drying process with atomizing |
| CN207871566U (en) * | 2018-01-17 | 2018-09-18 | 张丽娴 | A kind of centrifugal spray drying device |
| CN208136128U (en) * | 2018-02-06 | 2018-11-23 | 山东省同泰维润食品科技有限公司 | A kind of calcium propionate production recovery tower |
-
2019
- 2019-04-17 CN CN201910308300.9A patent/CN111820408A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101665425A (en) * | 2009-09-25 | 2010-03-10 | 如皋市江北添加剂有限公司 | Production process of calcium propionate and drying tower thereof |
| CN202770142U (en) * | 2012-08-09 | 2013-03-06 | 南京扬子精细化工有限责任公司 | Calcium propionate drying device |
| CN106946687A (en) * | 2017-03-06 | 2017-07-14 | 山东省同泰维润食品科技有限公司 | A kind of calcium propionate continuous automatic production system and its production method |
| CN107754360A (en) * | 2017-11-29 | 2018-03-06 | 慈溪市舒润卫浴实业有限公司 | A kind of drying process with atomizing |
| CN207871566U (en) * | 2018-01-17 | 2018-09-18 | 张丽娴 | A kind of centrifugal spray drying device |
| CN208136128U (en) * | 2018-02-06 | 2018-11-23 | 山东省同泰维润食品科技有限公司 | A kind of calcium propionate production recovery tower |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117018649A (en) * | 2023-10-09 | 2023-11-10 | 山西旺龙药业集团有限公司 | Medicinal hericium erinaceus mycelium spray drying tower and application method thereof |
| CN117018649B (en) * | 2023-10-09 | 2023-12-15 | 山西旺龙药业集团有限公司 | Medicinal hericium erinaceus mycelium spray drying tower and application method thereof |
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