CN106946687B - A kind of calcium propionate continuous automatic production system and its production method - Google Patents
A kind of calcium propionate continuous automatic production system and its production method Download PDFInfo
- Publication number
- CN106946687B CN106946687B CN201710127934.5A CN201710127934A CN106946687B CN 106946687 B CN106946687 B CN 106946687B CN 201710127934 A CN201710127934 A CN 201710127934A CN 106946687 B CN106946687 B CN 106946687B
- Authority
- CN
- China
- Prior art keywords
- effect
- propionic acid
- calcium propionate
- evaporator
- reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- BCZXFFBUYPCTSJ-UHFFFAOYSA-L Calcium propionate Chemical compound [Ca+2].CCC([O-])=O.CCC([O-])=O BCZXFFBUYPCTSJ-UHFFFAOYSA-L 0.000 title claims abstract description 66
- 235000010331 calcium propionate Nutrition 0.000 title claims abstract description 43
- 239000004330 calcium propionate Substances 0.000 title claims abstract description 43
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 42
- 230000000694 effects Effects 0.000 claims abstract description 74
- 230000003472 neutralizing effect Effects 0.000 claims abstract description 37
- 238000000926 separation method Methods 0.000 claims abstract description 37
- 238000006243 chemical reaction Methods 0.000 claims abstract description 34
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims abstract description 15
- 235000011941 Tilia x europaea Nutrition 0.000 claims abstract description 15
- 239000004571 lime Substances 0.000 claims abstract description 15
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 14
- 235000019260 propionic acid Nutrition 0.000 claims abstract description 11
- 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 abstract description 11
- 239000012153 distilled water Substances 0.000 claims abstract description 10
- 238000004806 packaging method and process Methods 0.000 claims abstract description 8
- 239000000706 filtrate Substances 0.000 claims abstract description 7
- 230000004087 circulation Effects 0.000 claims abstract description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 4
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 4
- 239000000463 material Substances 0.000 claims description 34
- 238000001704 evaporation Methods 0.000 claims description 27
- 230000008020 evaporation Effects 0.000 claims description 20
- 239000007788 liquid Substances 0.000 claims description 18
- 239000000243 solution Substances 0.000 claims description 18
- 238000001035 drying Methods 0.000 claims description 13
- 238000000034 method Methods 0.000 claims description 11
- 238000005119 centrifugation Methods 0.000 claims description 7
- 239000012452 mother liquor Substances 0.000 claims description 7
- 238000001514 detection method Methods 0.000 claims description 6
- 238000001914 filtration Methods 0.000 claims description 4
- 230000009471 action Effects 0.000 claims description 2
- 230000008859 change Effects 0.000 claims description 2
- 239000011549 crystallization solution Substances 0.000 claims description 2
- 239000000047 product Substances 0.000 abstract description 14
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000003825 pressing Methods 0.000 abstract description 6
- 238000012864 cross contamination Methods 0.000 abstract description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 238000010924 continuous production Methods 0.000 abstract description 2
- 239000012467 final product Substances 0.000 abstract 1
- 238000003756 stirring Methods 0.000 description 7
- 238000001802 infusion Methods 0.000 description 6
- 238000005457 optimization Methods 0.000 description 6
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 4
- 239000000920 calcium hydroxide Substances 0.000 description 4
- 235000011116 calcium hydroxide Nutrition 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 235000013305 food Nutrition 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000000470 constituent Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000003112 inhibitor Substances 0.000 description 3
- 239000000155 melt Substances 0.000 description 3
- 238000012544 monitoring process Methods 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 230000035484 reaction time Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 241001465754 Metazoa Species 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000008520 organization Effects 0.000 description 2
- 238000012216 screening Methods 0.000 description 2
- TVEXGJYMHHTVKP-UHFFFAOYSA-N 6-oxabicyclo[3.2.1]oct-3-en-7-one Chemical compound C1C2C(=O)OC1C=CC2 TVEXGJYMHHTVKP-UHFFFAOYSA-N 0.000 description 1
- 229930195730 Aflatoxin Natural products 0.000 description 1
- 241000193830 Bacillus <bacterium> Species 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 241000235342 Saccharomycetes Species 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 241001148470 aerobic bacillus Species 0.000 description 1
- 239000005409 aflatoxin Substances 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 238000004380 ashing Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000005034 decoration Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 238000001599 direct drying Methods 0.000 description 1
- 238000004945 emulsification Methods 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 235000013373 food additive Nutrition 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 150000002632 lipids Chemical class 0.000 description 1
- 239000002398 materia medica Substances 0.000 description 1
- 244000144977 poultry Species 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/41—Preparation of salts of carboxylic acids
- C07C51/412—Preparation of salts of carboxylic acids by conversion of the acids, their salts, esters or anhydrides with the same carboxylic acid part
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Crystallography & Structural Chemistry (AREA)
- Fertilizers (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a kind of calcium propionate continuous automatic production system and its production methods, after white lime is melted in distilled water in neutralizing tank, propionic acid calcium solution is obtained after propionic acid reaction is added dropwise, it neutralizes and active carbon is added into neutralizing tank after completing, and then propionic acid calcium solution is entered into filter press through gear pump pressurization, filtrate enters Lower tank after filters pressing, neutralization flow container is delivered to through pump, an effect separation chamber is pumped into through an effect conveying, two effect separation chambers are pumped into through two effect circulations again, into efficient centrifugal machine, final product is after drier is dry, it send through blast system to packaging system；The neutralizing tank is two, carries out neutralization reaction in turn.Compared with prior art, the present invention realizes consecutive production, reduce manpower consumption, it reduces environmental pollution, low energy consumption, because continuous production reduces personnel's cross contamination, is conducive to the raising of product quality, almost without " three wastes " generation in production process, calcium propionate purity is high, the stay in grade produced.
Description
Technical field
The present invention relates to technical field of food additives, are specifically exactly a kind of calcium propionate continuous automatic production system
And its production method.
Background technique
Calcium propionate is that the World Health Organization (WHO) and FAO (Food and Agriculture Organization of the United Nation) (FAO) ratify the safe and reliable food used
Product and feed mould inhibitor.Calcium propionate can equally be absorbed by being metabolized by people and animals with other fat, and be supplied necessary to people and animals
Calcium, this advantage are that other mould inhibitors can not be compared, to each in acid medium (starch contains protein and lipid phase)
Class mould, gram-Negative bacillus or aerobic bacillus have stronger inhibiting effect, can also inhibit the generation of aflatoxins,
And it is harmless to saccharomycete, to person poultry harmless, have no toxic side effect.It is that food, brewing, feed, one kind of Chinese materia medica preparation aspects are new
Type, safe and efficient food and feed mould inhibitor.
There are mainly two types of the production technologies of current calcium propionate:
One is using lime calcining by it is selected digestion, rinse emulsification made of milk of lime do raw material, it is straight using steam
The method for connecing heating.Its process flow are as follows: the master operation of calcium propionate production is reaction, filtering and drying, after screening
Lime is cleaned with clear water, crosses filter cake, and placement two days or more carry out aging, and it is spare to be made into milk of lime.Add in reaction kettle
Water simultaneously starts blender, while milk of lime is added, and obtains coarse fodder liquid at reaction conditions, fine fodder liquid is obtained after double-filtration
Drying is sent to, in the spray drying tower with heated high temperature air parallel flow contact, vaporizes the moisture in feed liquid, after dry
Product is through cyclonic separation collecting packing.Its processing disadvantages is: reaction process is discontinuous, and the degree of automation is low, does not evaporate link,
Direct drying, energy consumption are high.
Another kind be by through screening pulverized limestone and water ashing pond adjust to scale milk of lime be added reaction kettle in,
It is put into reaction kettle, is reacted under prescribed conditions, fully reacting from sour head tank by propionic acid at regular time and quantity under stirring condition
Afterwards, material enters spare in filtrate head tank after vacuumfilter filters off residue, and mother liquor is continuously put into concentration kettle through head tank
In be evaporated condensing crystallizing, and constantly crystallization is pulled out to put and carries out de- liquid processing in drum centrifuge, the wet object after de- liquid is sent
Enter drier, the material after drying is got product through crushing, detection, metering packing.Its processing disadvantages is that reaction is discontinuous, technique
Complexity, the degree of automation are low.
Traditional calcium propionate production is discontinuous, and energy consumption is high, process manual control, and yield is polluted environment by limit value.
Summary of the invention
It is an object of the invention to overcome disadvantage of the existing technology, a kind of calcium propionate continuous automatic production system is provided
System and its production method, technique realize consecutive production, reduce manpower consumption, reduce environmental pollution, and low energy consumption, because continuous
Production reduces personnel's cross contamination, is conducive to the raising of product quality, generates in production process almost without " three wastes ", production
Calcium propionate purity is high, stay in grade out.
To achieve the goals above, the technical scheme adopted by the invention to solve the technical problem is that: a kind of calcium propionate connects
Continuous mechanized production system, which is characterized in that including neutralizing tank, filter press, vapo(u)rization system, centrifuge, drier, the evaporation
System includes several groups separation chamber and evaporator combinations, and the neutralizing tank is connected by pump with filter press, and the filter press is in
Be connected with liquid bath, neutralize liquid bath and run well for temporarily storing feed liquid, guarantee system, the neutralizations liquid bath by delivery pump and
Vapo(u)rization system is connected, and the vapo(u)rization system is connected by pump with centrifuge, and the centrifuge is connected with drier.
As an optimization, the evaporator is connected with separation chamber, material is under the action of circulating pump in evaporator and separation
Indoor circulation.
The detection device for being able to detect the concentration variation of material in separation chamber is equipped with as optimization, in the separation chamber.
As optimization, the centrifuge centrifugation post mother liquor enters vapo(u)rization system and is evaporated again.
As optimization, the drier is pan dryer, and the pan dryer is four.
It is a kind of to utilize calcium propionate continuous automatic production system production calcium propionate method, which is characterized in that the steps include:
(1) stage of reaction: white lime is mixed well in neutralizing tank with distilled water, and being heated to 50~80 DEG C keeps it complete
Portion is dissolved, and propionic acid is added dropwise and carries out neutralization reaction, and control reaction end pH is 7.0~9.0, obtains propionic acid calcium solution；
(2) filtration stage: being added active carbon into neutralizing tank after the reaction was completed, propionic acid calcium solution is filtered, filtrate
It is delivered to neutralization flow container；
(3) two effect evaporation separation phases: the propionic acid calcium solution that step (2) obtains is delivered to an effect separation chamber, through an effect
Separation chamber enters 1st effective evaporator, and propionic acid calcium solution recycles in an effect separation chamber and 1st effective evaporator, and propionic acid calcium concentration reaches
When 40~50%, into two effect separation chambers, enter 2nd effect evaporator through two effect separation chambers, propionic acid calcium solution in two effect separation chambers and
Circulation, propionic acid calcium concentration reach 70~80% in 2nd effect evaporator.
(4) eccentric phase: the concentration calcium propionate crystallization solution that step (3) is obtained carries out centrifugal treating；
(5) drying stage: calcium propionate is sent through blast system to packaging system after drying after centrifugation.
As optimization, the 1st effective evaporator, evaporating temperature is 150~200 DEG C.
As optimization, the 2nd effect evaporator, evaporating temperature is 130~180 DEG C.
Compared with prior art the beneficial effects of the present invention are: a kind of calcium propionate continuous automatic production system of the invention
And its production method, guarantee that production technology can be continuous, reduces manpower consumption, reduce environmental pollution, low energy consumption, reduces personnel
Cross contamination is conducive to the raising of product quality, generates in production process almost without " three wastes ", the calcium propionate produced is pure
Degree height, stay in grade, superior product quality.
Detailed description of the invention
Fig. 1 is present invention process equipment schematic diagram；
Wherein: 1 neutralizing tank, 2 gear pumps, 3 filter presses, in 4 and flow container, 5 one effect delivery pumps, 6 one effect separation chambers, 7 one effects
Evaporator, 8 one effect circulating pumps, 9 two effect separation chambers, 10 2nd effect evaporators, 11 2 effect circulating pumps, 12 discharging pumps, 13 mother liquors pump, 14
Condenser, 15 are containing batch can, 16 centrifuges, 17 mother liquor tanks, 18 pan dryer A, 19 pan dryer B, 20 pulverizers, 21 packagings
System.
Specific embodiment
To enable the above objects, features and advantages of the present invention to be clearer and more comprehensible, preferred embodiment is cited below particularly, and combine
Detailed description are as follows for attached drawing:
The production technology that the present invention devises a set of new calcium propionate is produced calcium propionate by cleverly process step design
Line is connected into a whole set of complete automatic production line, greatly improves production efficiency, reduces human factor to product product
The influence of matter, reduces production energy consumption, has very high economy and society value.
Embodiment 1, referring to Fig.1, a kind of calcium propionate continuous automatic production system and its production method, process are as follows:
Propionic acid and white lime and distilled water are reacted in neutralizing tank 1, enter pressure by gear pump 2 after the reaction was completed
3 filters pressing of filter, the propionic acid calcium solution after filters pressing flow to Lower tank, are stored in and neutralize in flow container 4, and one imitates delivery pump 5 for calcium propionate
Solution is delivered to an effect separation chamber 6, from one effect separation chamber 6 in the middle part of feed, through one effect 6 lower part of separation chamber by one effect circulating pump 8 into
Enter 1st effective evaporator 7, after calcium propionate material concentration is up to standard, material by one effect 6 lower part outlet of separation chamber through two effect circulating pumps 11 into
Enter two effect separation chambers, 9 bottom, enters 2nd effect evaporator 10 from discharging in the middle part of two effect separation chambers 9 and recycle, concentration is up to standard through discharging pump
12 enter centrifuge 16, and centrifugal material passes through pan dryer 18,19, and centrifuge mother liquor enters mother liquor tank 17, send through mother liquor pump 13
To two effect separation chambers 9.Go out thermal energy of the neutralizer steam as 2nd effect evaporator 10 at the top of one effect separation chamber 6, through 2nd effect evaporator
10 enter condenser 14 condensation be sent into contain batch can 15, two effect 9 top material vapor liquids of separation chamber also enter condenser 10 condense into
Enter to contain batch can 14, participates in neutralization reaction containing liquid in batch can 14.Calcium propionate after pan dryer 18,19 is dry enters crushing
Machine 20 is crushed, and then is entered packaging system 21 and carried out finished product packing.
Specific reaction condition and reaction time are as follows:
1. the stage of reaction: distilled water is added into neutralizing tank, starts agitating paddle, puts into 1600 kg of white lime while stirring,
The mass ratio of white lime and distilled water is 1:10.Temperature control valve (TCV) is opened, the temperature controlled in neutralizing tank is maintained at 50 DEG C, until
White lime in neutralizing tank all melts, and stops heating.The propionic acid 3000 that mass fraction is 99% is added dropwise into neutralizing tank at this time
Kg, propionic acid drip off in 0.5 hour, and at 50 DEG C, the terminal pH of reaction mass is 7.5 for reaction temperature control, react 1 hour.To
6 kg active carbons are added in neutralizing tank, stop stirring after 20min, two neutralizing tanks successively carry out above-mentioned neutralization reaction, so that instead
It should be able to be carried out continuously, increase equipment capacity.
2. the filters pressing stage: after the reaction was completed, the material in neutralizing tank being squeezed into filter press through gear pump pressurization, to generation
Filter mud is recycled, and filtrate flows into Lower tank, and the effect of Lower tank is to collect filtered fluid, and the propionic acid calcium solution in Lower tank is through pumping
It is delivered to neutralization flow container, effect is to guarantee continuous feeding.
3. evaporation stage: propionic acid calcium solution is delivered to 1st effective evaporator, the evaporation temperature of 1st effective evaporator by an effect infusion pump
Degree is 160 DEG C, and material recycles continuous evaporation in 1st effective evaporator, controls material evaporation material concentration 45% in 1st effective evaporator.
Enter 2nd effect evaporator through two effect infusion pumps, the evaporating temperature of 2nd effect evaporator is 140 DEG C, and material recycles in 2nd effect evaporator
Continuous evaporation controls material concentration 70% in 2nd effect evaporator.
4. the eccentric phase: after material is evaporated in 2nd effect evaporator, into efficient centrifugal machine, controlling centrifuge speed
Be 3000 revs/min, the liquid after centrifugation enter accumulator tank then return to neutralizing tank continue participate in reaction, solid is automatically into defeated
Flood dragon is sent, is sent dry to drier.
5. drying stage: drying process is carried out continuously in four pan dryers, the material in real-time monitoring drier,
After detection is qualified, enter finished product conveying hinge cage through drain hole, then send through blast system to packaging system and packed automatically.
Through detecting water content≤3% of obtained calcium propionate, calcium propionate active constituent content >=99.99%
Embodiment 2, referring to Fig.1, the present embodiment are identical as 1 calcium propionate continuous automatic production process of embodiment, it is identical it
Place repeats no more, the difference is that, specific reaction condition and reaction time are as follows:
1. the stage of reaction: distilled water is added into neutralizing tank, starts agitating paddle, puts into 1700 kg of white lime while stirring,
The mass ratio of white lime and distilled water is 1:10.Temperature control valve (TCV) is opened, the temperature controlled in neutralizing tank is maintained at 60 DEG C, until
White lime in neutralizing tank all melts, and stops heating.The propionic acid 3000 that mass fraction is 99% is added dropwise into neutralizing tank at this time
Kg, propionic acid drip off in 0.5 hour, and at 60 DEG C, the terminal pH of reaction mass is 8.0 for reaction temperature control, react 1 hour.To
7 kg active carbons are added in neutralizing tank, stop stirring after 20min, two neutralizing tanks successively carry out above-mentioned neutralization reaction, so that instead
It should be able to be carried out continuously, increase equipment capacity.
2. the filters pressing stage: after the reaction was completed, the material in neutralizing tank being squeezed into filter press through gear pump pressurization, to generation
Filter mud is recycled, and filtrate flows into Lower tank, and the effect of Lower tank is to collect filtered fluid, and the propionic acid calcium solution in Lower tank is through pumping
It is delivered to neutralization flow container, effect is to guarantee continuous feeding.
3. evaporation stage: propionic acid calcium solution is delivered to 1st effective evaporator, the evaporation temperature of 1st effective evaporator by an effect infusion pump
Degree is 150 DEG C, and material recycles continuous evaporation in 1st effective evaporator, controls material evaporation material concentration 45% in 1st effective evaporator.
Enter 2nd effect evaporator through two effect infusion pumps, the evaporating temperature of 2nd effect evaporator is 130 DEG C, and material recycles in 2nd effect evaporator
Continuous evaporation controls material concentration 70% in 2nd effect evaporator.
4. the eccentric phase: after material is evaporated in 2nd effect evaporator, into efficient centrifugal machine, controlling centrifuge speed
Be 3000 revs/min, the liquid after centrifugation enter accumulator tank then return to neutralizing tank continue participate in reaction, solid is automatically into defeated
Flood dragon is sent, is sent dry to drier.
5. drying stage: drying process is carried out continuously in four pan dryers, the material in real-time monitoring drier,
After detection is qualified, enter finished product conveying hinge cage through drain hole, then send through blast system to packaging system and packed automatically.
Through detecting water content≤4% of obtained calcium propionate, calcium propionate active constituent content >=99.99%
Embodiment 3, referring to Fig.1, the present embodiment are identical as 1 calcium propionate continuous automatic production process of embodiment, it is identical it
Place repeats no more, the difference is that, specific reaction condition and reaction time are as follows:
1. the stage of reaction: distilled water is added into neutralizing tank, starts agitating paddle, puts into white lime 1800kg while stirring,
The mass ratio of white lime and distilled water is 1:10.Temperature control valve (TCV) is opened, the temperature controlled in neutralizing tank is maintained at 80 DEG C, until
White lime in neutralizing tank all melts, and stops heating.The propionic acid 3000 that mass fraction is 99% is added dropwise into neutralizing tank at this time
Kg, propionic acid drip off in 0.5 hour, and at 80 DEG C, the terminal pH of reaction mass is 8.0 for reaction temperature control, react 1 hour.To
8kg active carbon is added in neutralizing tank, stops stirring after 20min, two neutralizing tanks successively carry out above-mentioned neutralization reaction, so that reaction
It can be carried out continuously, increase equipment capacity.
2. the filters pressing stage: after the reaction was completed, the material in neutralizing tank being squeezed into filter press through gear pump pressurization, to generation
Filter mud is recycled, and filtrate flows into Lower tank, and the effect of Lower tank is to collect filtered fluid, and the propionic acid calcium solution in Lower tank is through pumping
It is delivered to neutralization flow container, effect is to guarantee continuous feeding.
3. evaporation stage: propionic acid calcium solution is delivered to 1st effective evaporator, the evaporation temperature of 1st effective evaporator by an effect infusion pump
Degree is 180 DEG C, and material recycles continuous evaporation in 1st effective evaporator, controls material evaporation material concentration 45% in 1st effective evaporator.
Enter 2nd effect evaporator through two effect infusion pumps, the evaporating temperature of 2nd effect evaporator is 160 DEG C, and material recycles in 2nd effect evaporator
Continuous evaporation controls material concentration 70% in 2nd effect evaporator.
4. the eccentric phase: after material is evaporated in 2nd effect evaporator, into efficient centrifugal machine, controlling centrifuge speed
Be 3000 revs/min, the liquid after centrifugation enter accumulator tank then return to neutralizing tank continue participate in reaction, solid is automatically into defeated
Flood dragon is sent, is sent dry to drier.
5. drying stage: drying process is carried out continuously in four pan dryers, the material in real-time monitoring drier,
After detection is qualified, enter finished product conveying hinge cage through drain hole, then send through blast system to packaging system and packed automatically.
Through detecting water content≤4% of obtained calcium propionate, calcium propionate active constituent content >=99.99%.
Above-mentioned specific embodiment is only specific case of the invention, and scope of patent protection of the invention includes but is not limited to
The product form and style of above-mentioned specific embodiment, a kind of any calcium propionate for meeting claims of the present invention are continuously automatic
Change production system and its production method and what any person of an ordinary skill in the technical field did it suitably changes or repair
Decorations, all shall fall within the protection scope of the present invention.
Claims (6)
1. a kind of calcium propionate continuous automatic production system, which is characterized in that including neutralizing tank, filter press, vapo(u)rization system, centrifugation
Machine, drier, the vapo(u)rization system include several groups separation chamber and evaporator combinations, and the neutralizing tank passes through pump and filter press phase
Even, the filter press with neutralize liquid bath be connected, neutralize liquid bath for temporarily storage feed liquid, guarantee system normal operation, it is described in
Be connected by delivery pump with vapo(u)rization system with liquid bath, the vapo(u)rization system by pump is connected with centrifuge, the centrifuge with do
Dry device is connected；The evaporator is connected with separation chamber, and material is under the action of circulating pump in evaporator and separation indoor circulation；Institute
State the detection device that the concentration variation for being able to detect material in separation chamber is equipped in separation chamber.
2. a kind of calcium propionate continuous automatic production system according to claim 1, which is characterized in that the centrifuge from
Heart post mother liquor enters vapo(u)rization system and is evaporated again.
3. a kind of calcium propionate continuous automatic production system according to claim 1, which is characterized in that the drier is
Pan dryer, the pan dryer are four.
4. utilizing calcium propionate continuous automatic production system production calcium propionate method, spy as any in claim 1-3
Sign is, the steps include:
(1) stage of reaction: white lime is mixed well in neutralizing tank with distilled water, and being heated to 50~80 DEG C keeps it all molten
Change, propionic acid is added dropwise and carries out neutralization reaction, control reaction end pH is 7.0~9.0, obtains propionic acid calcium solution；
(2) filtration stage: being added active carbon into neutralizing tank after the reaction was completed, and propionic acid calcium solution is filtered, filtrate conveying
To neutralization flow container；
(3) two effect evaporation separation phases: the propionic acid calcium solution that step (2) obtains is delivered to an effect separation chamber, is separated through an effect
Room enters 1st effective evaporator, and propionic acid calcium solution recycles in an effect separation chamber and 1st effective evaporator, and propionic acid calcium concentration reaches 40~
When 50%, into two effect separation chambers, enter 2nd effect evaporator through two effect separation chambers, propionic acid calcium solution is in two effect separation chambers and two effects
Circulation, propionic acid calcium concentration reach 70~80% in evaporator；
(4) eccentric phase: the concentration calcium propionate crystallization solution that step (3) is obtained carries out centrifugal treating；
(5) drying stage: calcium propionate is sent through blast system to packaging system after drying after centrifugation.
5. a kind of calcium propionate continuous automatic production method according to claim 4, which is characterized in that the effect evaporation
Device, evaporating temperature are 150~200 DEG C.
6. a kind of calcium propionate continuous automatic production method according to claim 4, which is characterized in that the two effects evaporation
Device, evaporating temperature are 130~180 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710127934.5A CN106946687B (en) | 2017-03-06 | 2017-03-06 | A kind of calcium propionate continuous automatic production system and its production method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710127934.5A CN106946687B (en) | 2017-03-06 | 2017-03-06 | A kind of calcium propionate continuous automatic production system and its production method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106946687A CN106946687A (en) | 2017-07-14 |
| CN106946687B true CN106946687B (en) | 2019-01-18 |
Family
ID=59467804
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710127934.5A Active CN106946687B (en) | 2017-03-06 | 2017-03-06 | A kind of calcium propionate continuous automatic production system and its production method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106946687B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111820408A (en) * | 2019-04-17 | 2020-10-27 | 山东雨田食品科技有限公司 | Production system and production method for simultaneously producing calcium propionate particles and calcium propionate powder |
| WO2022058401A1 (en) | 2020-09-17 | 2022-03-24 | Niacet Corporation | Direct conversion of esters to carboxylates |
| CN113976054A (en) * | 2021-10-25 | 2022-01-28 | 聊城鲁西甲酸化工有限公司 | Production system and process for continuously and automatically producing calcium formate |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201301235Y (en) * | 2008-06-30 | 2009-09-02 | 浙江商达环保有限公司 | Triple-effect continuous evaporative condenser |
| CN101747174B (en) * | 2010-01-15 | 2013-04-17 | 连云港树人科创食品添加剂有限公司 | Preparation method of calcium propionate and second-effect flash distillation plant |
-
2017
- 2017-03-06 CN CN201710127934.5A patent/CN106946687B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN106946687A (en) | 2017-07-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106517626B (en) | A kind for the treatment of process of sodium sulfate wastewater | |
| CN106946687B (en) | A kind of calcium propionate continuous automatic production system and its production method | |
| CN108568135B (en) | Manganese sulfate evaporation crystallization equipment and process | |
| CN104473120B (en) | A kind of production technology of monosodium glutamate | |
| CN107510026A (en) | Salt and preparation method thereof and system | |
| CN101747174B (en) | Preparation method of calcium propionate and second-effect flash distillation plant | |
| CN106191328A (en) | A kind of xylose production process | |
| CN101896241A (en) | Be used for making the method and apparatus of sugared crystallization by the control cooling | |
| CN104805224B (en) | A kind of processing unit (plant) of ecosystem brown sugar | |
| CN108741078A (en) | The processing method for preparing the method and linseed of flaxseed gum, flax lignan, flax dietary fiber and flax protein powder | |
| CN110436513A (en) | The continuous evaporative crystallization production technology and its power-economizing method of monohydrate zinc sulphate | |
| CN206384871U (en) | A kind of processing system of sodium sulfate wastewater | |
| CN106698562A (en) | MVR evaporation crystallization drying integrated apparatus and evaporation crystallization drying method | |
| US4083732A (en) | Sugar juice treatment | |
| KR100698899B1 (en) | Method for preparing liquid salt | |
| CN107383116A (en) | A kind of method for efficiently preparing L arabinoses | |
| CN108557894A (en) | A kind of manganese sulfate solution crystallization apparatus and method | |
| EA015362B1 (en) | Process for the production of liquid sugar | |
| CN109232772A (en) | A kind of method that animal cartilage extracts chondroitin sulfate and collagen | |
| CN205627163U (en) | Monosodium glutamate no. 2 is imitated and is evaporated crystal system against current | |
| CN1284586A (en) | Method for treatment of biological base filamentary material | |
| CN206368049U (en) | A kind of device for handling organic brine waste | |
| CN207957789U (en) | A kind of manganese sulfate solution crystallization apparatus | |
| CN106472816A (en) | Alcohol method removes the method and apparatus that aflatoxin produces peanut concentrated protein | |
| CN108559797A (en) | A kind of method and apparatus that xylose is extracted in the waste material from viscose fiber |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Continuous automatic production system for calcium propionate and production method for same Effective date of registration: 20190627 Granted publication date: 20190118 Pledgee: Zaozhuang rural commercial bank Limited by Share Ltd. Shanting branch Pledgor: SHANDONG PROVINCE AND TAI WEI RUN FOOD TECHNOLOGY Co.,Ltd. Registration number: 2019370000143 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 277200 No.1, Yinshan Industrial Park, economic development zone, Shanting District, Zaozhuang City, Shandong Province Patentee after: Shandong tongtaiweirun Food Technology Co.,Ltd. Address before: 277200 Shandong city of Zaozhuang province Shanting District City Town waterlogging Stephen East Village Patentee before: SHANDONG PROVINCE AND TAI WEI RUN FOOD TECHNOLOGY Co.,Ltd. |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20210906 Granted publication date: 20190118 Pledgee: Zaozhuang rural commercial bank Limited by Share Ltd. Shanting branch Pledgor: SHANDONG PROVINCE AND TAI WEI RUN FOOD TECHNOLOGY Co.,Ltd. Registration number: 2019370000143 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: Calcium propionate continuous automatic production system and production method thereof Effective date of registration: 20210909 Granted publication date: 20190118 Pledgee: Zaozhuang Rural Commercial Bank Co.,Ltd. Shanting sub branch Pledgor: Shandong tongtaiweirun Food Technology Co.,Ltd. Registration number: Y2021980009162 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20220829 Granted publication date: 20190118 Pledgee: Zaozhuang Rural Commercial Bank Co.,Ltd. Shanting sub branch Pledgor: Shandong tongtaiweirun Food Technology Co.,Ltd. Registration number: Y2021980009162 |
|
| PC01 | Cancellation of the registration of the contract for pledge of patent right | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: A kind of calcium propionate continuous automatic production system and production method thereof Effective date of registration: 20220831 Granted publication date: 20190118 Pledgee: Zaozhuang rural commercial bank Limited by Share Ltd. Shanting branch Pledgor: Shandong tongtaiweirun Food Technology Co.,Ltd. Registration number: Y2022980014232 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |