CN114177855B - One-step production equipment and production method of acidity regulator lactic acid powder - Google Patents

One-step production equipment and production method of acidity regulator lactic acid powder Download PDF

Info

Publication number
CN114177855B
CN114177855B CN202111459321.4A CN202111459321A CN114177855B CN 114177855 B CN114177855 B CN 114177855B CN 202111459321 A CN202111459321 A CN 202111459321A CN 114177855 B CN114177855 B CN 114177855B
Authority
CN
China
Prior art keywords
lactic acid
tank
materials
content
hydrolysis
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
Application number
CN202111459321.4A
Other languages
Chinese (zh)
Other versions
CN114177855A (en
Inventor
周水明
郭慧颖
周力一
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mingfu Shanghai Health Technology Co ltd
Original Assignee
Mingfu Shanghai Health Technology Co ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Mingfu Shanghai Health Technology Co ltd filed Critical Mingfu Shanghai Health Technology Co ltd
Priority to CN202111459321.4A priority Critical patent/CN114177855B/en
Publication of CN114177855A publication Critical patent/CN114177855A/en
Application granted granted Critical
Publication of CN114177855B publication Critical patent/CN114177855B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • 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
    • A23L29/00—Foods or foodstuffs containing additives; Preparation or treatment thereof
    • A23L29/03—Organic compounds
    • A23L29/035—Organic compounds containing oxygen as heteroatom
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/02—Feed or outlet devices; Feed or outlet control devices for feeding measured, i.e. prescribed quantities of reagents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
    • B01J2204/002—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the feeding side being of particular interest
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
    • B01J2204/005—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the outlet side being of particular interest
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Nutrition Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention relates to one-step production equipment and a production method of an acidity regulator lactic acid powder. Firstly, calcium carbonate slurry and lactic acid are input into a reaction kettle for reaction, and the obtained mixture is input into a hydrolysis concentration device for reaction after rough filtration and fine filtration, so that the lactoyl lactic acid and the polylactic acid in the raw material lactic acid are ensured to be almost completely hydrolyzed, saponified and converted into free lactic acid and lactic acid molecules. Then the finished product is obtained through the procedures of evaporation, concentration, drying, mixing, packaging and the like. The invention has the advantages of more thorough reaction of raw materials, strict control of the content of free lactic acid by utilizing the hydrolysis concentration device, simpler whole process, contribution to industrialized mass production, shortening of production period, flexible and controllable lactic acid content within a certain range, great improvement of production efficiency, stable product quality, obvious reduction of production cost and the like.

Description

One-step production equipment and production method of acidity regulator lactic acid powder
Technical Field
The invention relates to the technical field of food additives, in particular to one-step production equipment and a one-step production method of an acidity regulator lactic acid powder.
Background
Lactic acid is a hydroxy organic acid (structural formula: CH) with relatively simple molecular structure and relatively small molecular weight 3 CH (OH) COOH, formula C 3 H 6 O 3 ). After lactic acid is added into water, the carboxyl group releases a proton H + Simultaneously generates a lactate ion CH 3 CH(OH)COO - Lactic acid in this state is called free lactic acid. The study shows that the content of free lactic acid in lactic acid solutions with different concentrations at normal temperature and normal pressure is different: lactic acid molecules are substantially in a free state when the lactic acid content (m/m) is below about 30%; when the lactic acid content is more than 30%, lactoyl lactic acid (intermolecular dehydrate of lactic acid) starts to be generated; when the lactic acid content is further increased to about 60% -100%, the lactic acid content in a free state is not more than 30%, and most of lactic acid in the system is converted into lactoyl lactic acid and polylactic acid, and at the moment, the lactic acid coexists in a plurality of forms of free lactic acid, lactoyl lactic acid and polylactic acid. The ratio of lactoyl lactic acid to polylactic acid in the lactic acid solution changes with the time or temperature. The lactic acid content we generally refer to is the total content of lactic acid, i.e. free lactic acid and lactoyl lactic acid in the systemThe total content of the polylactic acid after all the polylactic acid is converted into free lactic acid can be measured by adding excessive caustic alkali into a lactic acid sample to be measured for full saponification and then back-titrating with sulfuric acid standard solution, and the measurement of the content of the free lactic acid can be directly titrated by adopting sodium hydroxide standard solution.
The commercial lactic acid powder has main components of lactic acid (53% -62%) and calcium lactate (38% -45%), and is allowed to contain not more than 2% of water and about 2% of anti-caking agent (such as silica, etc.) in order to prevent the product from being hardened during the storage. The acidity regulator lactic acid powder has unique fruit acid flavor and the characteristic of promoting formation of cheese flavor during compound application, can be used as a compound food additive for wrapping powder of soft sweets in candy production and functional ingredients of hard milk sweets, and can also be used as flour modifier (such as leavening agent, shaping agent and preservative of baked foods), sour agent of solid beverage (endowing beverage products with unique fruit sour), flavoring agent of flavoring, feed acidifier in the breeding industry and the like. Lactic acid powder used as acidity regulator requires that almost all lactic acid exists in free, directly titratable form, which puts higher demands on the preparation process.
There are many documents relating to lactic acid powder and a preparation method thereof. Chinese patent CN104661539B discloses a method for preparing lactic acid powder, the lactic acid powder prepared by this method is a mixed lactate product with neutral or near neutral pH, wherein the ratio of two components of calcium lactate and sodium lactate is up to more than 80%, in order to maintain the use function of lactate product mainly comprising calcium lactate, and increase the dissolution rate. That is, the lactic acid powder (which can be regarded as lactate powder) has low free lactic acid content, and is not a product with the acidity regulator lactic acid powder provided by the invention.
Chinese patent CN104117327A, CN111850056a produced lactic acid powder products by spray granulation of high concentration lactic acid solution and grinding and pressing of solid lactic acid, respectively. Analysis shows that the two methods can only be used as theoretical assumption put forward for the preparation method of the lactic acid powder, and the actual process or large-scale production is difficult to form. This is because 99% of lactic acid, which is one of the raw materials in the former technical proposal, cannot be completely converted into calcium lactate by chemical reaction with the ratio of calcium oxide under the environment, and a large amount of lactic acid is converted into lactoyl lactic acid, polylactic acid during the reaction, and finally remains in the lactic acid powder. The method and the equipment are very difficult to prepare lactic acid powder products used as acidity regulators in reality, and mainly have the following two reasons: firstly, the scheme still adopts the conventional thought of mixing powder calcium lactate and finished lactic acid, does not relate to evaluation of mixing effect, and lacks evaluation standard and method; secondly, the scheme only refers to a method for preparing solid lactic acid into lactic acid particles or powder by using a twisting screen machine, and the key method and process for converting the lactic acid and calcium lactate liquid mixture into the solid lactic acid after distillation and concentration are omitted or avoided.
The Chinese patent CN108157932A prepares the compound food additive lactic acid powder through a double screw extruder, the product of the scheme is consistent with the principle and the aim of the invention, but the process of crystallization rearrangement of the solid mixture exists in the process, which objectively leads to the problems of large occupied area of a production field (semi-finished product area), long production period (1-4 weeks), large risk of biological pollution, large workload of personnel, low production efficiency and the like.
Disclosure of Invention
The invention aims to provide one-step production equipment and a one-step production process of a whole set of acidity regulator lactic acid powder. The equipment comprises a metering tank, a slurry mixing tank, a reaction kettle, a transfer tank, a filter, a hydrolysis concentration device, a conveyor, a dryer (comprising a separator connected with the conveyor and matched with the dryer), and a mixer. Wherein the feed inlet of reation kettle links to each other with the discharge gate of metering tank, size mixing tank respectively, and the discharge gate of reation kettle links to each other with the feed inlet of transfer jar, and the transfer jar links to each other with filter, hydrolysis concentration device, conveyer, desiccator, separator, mixer in proper order through the pipeline. Raw materials of lactic acid and calcium carbonate respectively enter a reaction kettle through a metering tank and a slurry mixing tank, obtained reaction liquid enters a hydrolysis concentration device after passing through a transfer tank and a filter, materials which are hydrolyzed and concentrated to a certain concentration are sent to a dryer and a separator by a conveyor to be sequentially dried and separated, and finally enter a mixer to be homogenized, packaged and put in storage.
Further, the number of the transfer tanks and the filters is two, and the two groups are respectively marked as a transfer tank I, a transfer tank II, a filter I and a filter II; wherein transfer jar I's feed inlet links to each other with reation kettle's discharge gate, and transfer jar I's discharge gate links to each other with filter I's feed inlet, and filter I's discharge gate links to each other with transfer jar I's feed inlet (backward flow), transfer jar II's feed inlet respectively, and transfer jar II's discharge gate links to each other with filter II's feed inlet, and filter II's discharge gate links to each other with transfer jar II's feed inlet (backward flow), hydrolysis concentration device's feed inlet respectively. The transfer tank plays a role of temporarily storing materials, and ensures continuous production; the two filters respectively play roles of rough filtration and fine filtration, and ensure that the materials entering the hydrolysis concentration device meet the quality index requirements of the lactic acid powder product of the acidity regulator with the target specification.
Further, the hydrolysis concentration device comprises a tank body, a heating device, a stirring device (eccentrically arranged), a material circulating pump (submerged pump), a heat exchanger and a pressure reducing device; a heating device is arranged on the surface of the tank body and is used for heating materials in the tank; the top of the tank body is provided with a stirring port (eccentric), an evaporation concentration port (center), a reflux port, a material circulating pump port and a manhole, and the stirring device, the pressure reducing device, the material circulating pump and the heat exchanger are respectively connected with the stirring port, the evaporation concentration port, the material circulating pump port and the reflux port; the material circulating pump conveys the materials in the tank to the heat exchanger for concentration through a submerged pump discharging pipe arranged in the tank body, and returns to the tank again through a backflow port; and a discharge port is arranged on the circulating reflux pipeline of the material and is connected with the conveyor.
Further, the heating device on the hydrolysis concentration device comprises a heating jacket fixed at the bottom of the tank body and a heating winding pipe surrounding the tank body, and the heating jacket, the heating winding pipe and the heat exchanger are all communicated with the heating medium conveying pipeline.
Further, the conveyor is specifically a double-screw conveyor, the dryer is specifically a spin flash dryer, and the separator is specifically a cyclone separator.
Another object of the present invention is to provide a process for producing lactic acid powder as an acidity regulator by the one-step method using the above apparatus, comprising the steps of: (a) Adding calcium carbonate and water into a size mixing tank, uniformly mixing to obtain calcium carbonate slurry, and adding lactic acid into a metering tank; (b) The calcium carbonate slurry and the lactic acid are proportionally input into a reaction kettle for reaction, the mixed materials are conveyed to a transfer tank for temporary storage after being sampled and detected to be qualified in the period, and then are input into a filter for filtration; (c) Delivering the filtered material reaching the standard to a hydrolysis concentration device, stirring while keeping the material circulating reflux, continuously circulating the hydrolyzed material to a heat exchanger for heating and concentrating under a reduced pressure state; (d) And (3) after the concentrated materials are detected to be qualified, conveying the materials into a dryer for drying, separating the obtained powder solids by a separator, homogenizing the powder solids in a mixer, and finally packaging and warehousing the powder solids.
Further, the feeding ratio (mass ratio) of calcium carbonate, lactic acid and water in the size mixing tank and the metering tank in the step (a) is 400-900:3000-4500:800-1500, wherein the free lactic acid content and the total lactic acid content in the acidity regulator lactic acid powder prepared in the step (d) are controlled to be 55-62%, and the difference between the free lactic acid content and the total lactic acid content is not more than 1%.
Further, in the step (b), a small amount of lactic acid is added to fill the bottom of the reaction kettle, then calcium carbonate slurry is added at one time, and lactic acid is slowly added to react.
Further, the temperature of the materials in the reaction kettle in the step (b) is maintained at 60-80 ℃, sampling and detection are continuously carried out in the reaction process, and lactic acid is added into the reaction kettle according to the situation; and after the pH value of the materials in the reaction kettle is maintained at 4.8-5.2, the reaction is considered to be completed, and lactic acid which is equivalent to 5% of the theoretical feeding amount is fed again, so that the pH value of the mixed materials is less than 4.5. The purpose of the addition of the lactic acid is to make the lactic acid excessive, which is favorable for the thorough reaction and the filtration operation after the reaction.
Further, the temperature of the materials in the transfer tank I in the step (b) is maintained at 75-85 ℃, the temperature of the materials in the transfer tank II is maintained at 85-95 ℃, and the materials are subjected to rough filtration by the filter I and fine filtration by the filter II in sequence and then enter a hydrolysis concentration heating device.
Further, the content of calcium lactate in the material input into the hydrolysis concentration device in the step (c) is controlled within the range of 45% -55% (m/m), the temperature of the material is controlled to be 85-95 ℃ in the stirring reflux (i.e. circulation) process, the content of free lactic acid and the total content of lactic acid are continuously sampled and detected, and the lactic acid is optionally added to match with a target value of the product, and the hydrolysis is completed when the total content of lactic acid and the content of free lactic acid are less than or equal to 1%.
Further, after the hydrolysis in the step (c), stirring and refluxing are maintained, the vacuum degree in the hydrolysis concentration device is pumped to-0.09 MPa to-0.05 MPa, the materials are heated to 100-115 ℃ by a heat exchanger for concentration, and when the total content of calcium lactate and free lactic acid in the materials reaches 88% -92%, the reflux, stirring and heating are stopped, and the materials are cooled to 90-110 ℃.
Further, in the step (d), the air inlet temperature of the dryer is 115-125 ℃, the air outlet temperature is 75-85 ℃, the moisture content of the material output from the dryer is less than or equal to 2%, and the fineness is randomly regulated and controlled within the range of 25-100 meshes.
The invention gets rid of the public report and the conventional thinking and process method that the powder-like calcium lactate finished product is firstly prepared, then the raw material lactic acid is mixed with the prepared powder-like calcium lactate finished product, and then the lactic acid powder product is produced. The hydrolysis process of the invention can be completed in a period of time ranging from instant to hours (influenced by the content of the lactoyl lactic acid and the polylactic acid in the raw material lactic acid), and the content of free lactic acid is not concerned in the prior process for producing the lactic acid powder by mixing the raw material lactic acid and the powdery calcium lactate, so that the free lactic acid, the lactoyl lactic acid and the polylactic acid exist simultaneously in the prepared lactic acid powder product. Even the most effective twin screw extrusion mixing in CN108157932a is difficult to achieve the conditions and effects of the materials of the present invention on lactoyl lactic acid and polylactic acid with sufficient contact and free water and calcium ions, so that the hydrolysis process called crystallization rearrangement is objectively relatively slow, taking weeks to months.
Compared with the prior art, the invention has the following beneficial effects: (1) Lactic acid and calcium carbonate are utilized to prepare lactic acid powder for acidity regulator, calcium carbonate is converted into calcium lactate through mixing reaction, and excessive lactic acid is added after the reaction is balanced, so that the reaction is more thorough; (2) The content of free lactic acid is strictly controlled by utilizing a hydrolysis concentration device, so that the lactoyl lactic acid and the polylactic acid are completely converted into the free lactic acid as far as possible, the content of the lactoyl lactic acid and the polylactic acid in the obtained lactic acid powder product is negligible, and the previous process or the lactic acid powder product does not pay attention to the point; (3) The whole process is simple, can realize industrialized mass production, shortens the production period to the maximum extent, has flexible and controllable lactic acid content in a certain range, and can better meet the demands of customers.
Drawings
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a flow diagram of the apparatus of the present invention;
FIG. 3 is a front view of the hydrolysis concentration device;
fig. 4 is a top view of the hydrolysis concentration device.
The device comprises a slurry mixing tank 1, a slurry mixing tank 2, a metering tank 3, a reaction kettle 4, a candle type filter 5, a transfer tank I, a transfer tank 6, a transfer tank II, a precise filter 7, a spiral pipe heat exchanger 8, a hydrolysis concentration device 9, a hydrolysis concentration device 10, a double-screw conveyor 11, a spin flash dryer 12 and a mixer; 9-1 parts of evaporation concentration pipes, 9-2 parts of stirrers, 9-3 parts of heating winding pipes, 9-4 parts of heating jackets, 9-5 parts of material circulating pumps, 9-6 parts of stirring ports, 9-7 parts of evaporation ports, 9-8 parts of reflux ports, 9-9 parts of material circulating pump ports and 9-10 parts of manholes.
Detailed Description
In order to make the technical scheme and the beneficial effects of the present invention fully understood by those skilled in the art, the following description is further made with reference to specific embodiments and drawings.
The process flow shown in fig. 1 is as follows:
1. feeding: the lactic acid and the calcium carbonate raw materials meeting the requirements are prepared before production. The theoretical amount of lactic acid, the amount of calcium carbonate and the amount of distilled water for pulping are calculated by taking 50+/-5% of the content of calcium lactate (anhydrous substance) in the clarified liquid entering the hydrolysis concentration device 9 as targets according to the single batch plan reaction liquid production amount of the reaction kettle 3 and combining the content (80% -100%) of the lactic acid serving as the raw material. Raw material lactic acid and distilled water with 120 percent of theoretical amount are respectively pumped into a metering tank 2 and a size mixing tank 1. And starting the slurry mixing tank 1 to stir, slowly adding theoretical amount of calcium carbonate into the slurry mixing tank 1 to finish slurry mixing, and putting the obtained slurry into the reaction kettle 3 at one time.
2. The reaction: and starting a heating system of the reaction kettle 3, and maintaining the temperature of materials in the reaction kettle at 60-80 ℃. Starting a stirrer in the reaction kettle, opening a discharge valve of the metering tank to a feed inlet of the reaction kettle, observing a reaction phenomenon through a sight glass at the upper part of the reaction kettle, and accordingly adjusting the feed rate of raw material lactic acid and keeping in mind the consumption of lactic acid in the metering tank. The reaction vessel was sampled to measure the pH of the reaction solution, and the addition of lactic acid as a raw material was stopped when the pH was set to ph=5±0.5. After stirring was continued for a period of time, the measurement was sampled again and the reaction was deemed complete when ph=5±0.2. And (3) keeping a stirring state, slightly opening a discharge valve of the metering tank 2 to a feed inlet of the reaction kettle, and dropwise adding lactic acid with the amount which is about 5% of the theoretical feeding amount, so that the pH value of the reaction solution is less than 4.5. Finally, the materials in the reaction kettle are conveyed to the transfer tank I at one time.
3. And (3) filtering: the heating system of the transfer pot I5 is started, so that the temperature of the materials in the transfer pot II 6 is maintained at 80+/-2 ℃, and then the materials are pumped into the candle filter 4 for primary filtration, and filtrate synchronously enters the transfer pot II 6. The heating system of the transfer tank II 6 is started, so that the temperature of the materials in the transfer tank II 6 is maintained at 90+/-5 ℃, then the materials are pumped into the precise filter 7 for further filtration, and the clarified liquid synchronously enters the hydrolysis concentration device 9.
4. And (3) hydrolyzing and concentrating: and (3) starting a heating system on the tank body of the hydrolysis concentration device 9, so that the temperature of materials in the tank is maintained at 90+/-5 ℃, and sampling and measuring the content of calcium lactate and lactic acid in the feed liquid after circularly stirring for a period of time. According to the measurement result, the addition amount of the lactic acid is calculated according to the proportion of the target formula (generally, the lactic acid is 53-62 percent and the calcium lactate is 38-45 percent), and the circulation stirring is continued for a period of time after one accurate addition. And sampling again to measure the content of calcium lactate and lactic acid in the feed liquid, and repeatedly adjusting and confirming the proportion conforming to the target formula. And (3) preserving the heat of the mixed material with the calcium lactate and the lactic acid content conforming to the target formula proportion in the hydrolysis concentration device 9 at 90+/-5 ℃, continuously stirring and maintaining a reflux circulation state, sampling once every 30min, and respectively measuring the free lactic acid content and the total lactic acid content until the total lactic acid content-the free lactic acid content is less than or equal to 1 percent, wherein the hydrolysis is completed. After the hydrolysis is confirmed, under the condition that the materials are kept under stirring and circulated and reflowed, a vacuum device connected with an evaporation concentration port is started, the vacuum degree in the tank body is pumped to minus 0.07+/-0.02 MPa, and a spiral tube heat exchanger 8 connected with a material circulating pump at the upper part of the hydrolysis concentration device 9 is started for heating. And (3) maintaining the vacuum degree in the tank at-0.07+/-0.02 MPa and the material temperature at 110+/-2 ℃ in the evaporation concentration process, repeatedly sampling and measuring the content of calcium lactate and lactic acid in the concentrated solution during the concentration process, stopping heating, vacuumizing and material circulation when the total content of the calcium lactate and the lactic acid reaches 88% -92%, and maintaining the material temperature at 90-110 ℃.
5. Post-treatment: the circulating cooling water of the jacket of the cylinder of the double-screw conveyor 10 is opened, the double-screw conveyor 10 is started, the screw rod of the double-screw conveyor is in a normal rotary conveying state, and the rotary flash dryer 11 is started. And opening a material conveying valve of the circulating pump to the double-screw conveyor 10, and starting the material circulating pump 9-5 to discharge. The liquid material entering the double-screw conveyor 10 is maintained to be completely output in a powder particle shape at the tail end and directly enters the spin flash dryer 11 by slowly closing a material conveying valve (adjusting the reflux quantity) which flows back to the tank body through the spiral tube heat exchanger. The method aims at controlling the moisture content of the dried product to be less than or equal to 2 percent, and the temperature of hot air is set within the range of 115-125 ℃, or the feeding speed is regulated at the set fixed temperature (within the range of 115-125 ℃) so that the temperature of air outlet is within the range of 75-85 ℃ (combined with the corresponding spin flash dryer 11). Meanwhile, the fineness of the output product is arbitrarily controlled and regulated within the range of 25-100 meshes by regulating the rotation speed of the main machine of the rotary flash dryer 11. The output product enters the mixer 12, is uniformly mixed by a verified program, is sampled and detected, and is packaged and put in storage after being judged to be qualified.
The equipment involved in the whole production process is shown in fig. 2-4: the size mixing tank 1 is made of stainless steel material with mechanical stirring; the metering tank 2 is made of dual-phase steel; the reaction kettle 3 is a stainless steel or glass lining reactor which is made of lactic acid corrosion resistant materials, provided with a screw belt or a jacket, can be communicated with steam or can be heated by heat conducting oil, provided with a paddle or an anchor stirring device, and has a volume matched with the whole production scale; . The material requirements of the transfer tank I5 and the transfer tank II 6 are the same as those of the reaction kettle 3, and the volume and the whole yield are matched in scale; the candle filter 4 and the precision filter 7 are preferably metal plate filters or candle filters which are made of lactic acid corrosion resistant materials and have a sufficient filtering area (filtering amount); the hydrolysis concentration device 9 is core equipment of the invention, the material of the hydrolysis concentration device is preferably stainless steel with lactic acid corrosion resistance, and the effective volume is matched with the yield scale; the double-screw conveyor 10 is a semicircular cylinder and is provided with a water cooling jacket, and the material of the part contacted with the material is lactic acid corrosion resistant; the material of the contact part of the spin flash dryer 11 and the material is lactic acid corrosion resistant, and the drying capacity is matched with the set yield scale; the mixer 12 is a one-dimensional mixer, and the material of the part contacted with the material is lactic acid corrosion resistant, and the volume is matched with the set output scale; the packing machine is a powder packing machine, and the material of the part contacted with the material is lactic acid corrosion resistant, and the using capacity is matched with the set output scale and the production organization.
Example 1
1 preparation of materials
Mixing calcium carbonate: 900kg of distilled water is injected into the size mixing tank, 600kg of food-grade calcium carbonate is added under stirring and is prepared into slurry, and stirring is kept until discharging is finished. Lactic acid feed: 3200kg of raw lactic acid having a nominal content of 80.2% was pumped into the metering tank at a time.
2 reaction
Firstly, about 5kg of raw material lactic acid is input into the reaction kettle, and the feeding is stopped immediately after the bottom of the reaction kettle is filled and sealed. Then the calcium carbonate slurry is input into a reaction kettle once, a stirring and heating device of the reaction kettle is started, and the temperature of the materials is set to be 60-80 ℃.Slowly opening a lactic acid feeding valve, adding raw material lactic acid into the reaction kettle, and reacting with calcium carbonate under stirring. Bubble (CO) is released during the reaction 2 ) And the reflux quantity of the metering tank is regulated under the condition of keeping the small opening degree of the feed valve and not frequently changing. The lactic acid feed valve was closed when the reaction solution pH was measured to be approximately 4.5, and about 1280Kg of the raw material lactic acid was consumed. After stirring for 20 minutes, the reaction solution was sampled again to measure the pH of about 4.8, and the feed valve was opened to add about 50 kg of lactic acid as a raw material and stirred for 10 minutes, and the reaction solution was observed as clear from the sight glass at the upper part of the reaction vessel.
And opening and setting a heating and heat-preserving system of the transfer tank I, and inputting the clarified reaction liquid in the reaction kettle into the transfer tank I at one time, wherein the temperature of materials in the tank is maintained to be 80+/-2 ℃. And starting and setting a heating and heat-preserving system of the candle filter, inputting the reaction liquid in the transfer tank I into the candle filter for rough filtration, and maintaining the temperature of the material flowing out of the candle filter to be 90+/-5 ℃. And (3) starting and setting a heating and heat-preserving system of the transfer tank II, inputting clarified filtrate into the transfer tank II, and maintaining the temperature of materials in the tank to be 90+/-5 ℃. And starting and setting a heating and heat-preserving system of the precise filter, inputting the reaction liquid in the transfer tank II into the precise filter for continuous precise filtration, and inputting the filtered liquid after the precise filtration into the hydrolysis concentration device.
3 hydrolysis
Materials entering the hydrolysis concentration device are stirred and hydrolyzed at the temperature of 90+/-5 ℃, and the materials are circulated and refluxed in the tank by using a material circulating pump. And sampling and measuring the content of calcium lactate (converted into anhydrous substance) in the feed liquid to be 51.2% and the content of lactic acid to be 1.65% when the circulating reflux is carried out for 5 min. The stirring and the normal operation of a circulating pump are kept, the residual raw material lactic acid in a metering tank is fed into a hydrolysis concentration device once (3200 Kg of raw material lactic acid is consumed up to the moment), and the temperature of the materials in the tank is kept at 90+/-5 ℃. And then sampling and detecting every 30min, and respectively measuring the free lactic acid content and the total lactic acid content. When the free lactic acid content was measured to be 42.8% and the total lactic acid content was measured to be 43.3% (difference < 1%), the completion of the hydrolysis was judged.
And (3) maintaining normal operation of the stirring and circulating pump, starting a vacuum device connected with an evaporation concentration port at the upper part of the hydrolysis concentration device to carry out vacuumizing, and starting a spiral tube heat exchanger connected with the circulating pump at the upper part of the hydrolysis concentration device to carry out evaporation concentration when the vacuum degree in the tank reaches-0.07+/-0.02 MPa, so as to maintain the vacuum degree of the system to-0.07+/-0.02 MPa. Sampling and measuring when the temperature of the material rises to 110+/-2 ℃, stopping concentrating and maintaining the temperature of the material at 90-110 ℃ when the content of calcium lactate is 35.6%, the content of free lactic acid is 53.2% and the total content of lactic acid is 53.4% (the difference between the two is less than 1%).
4 post-treatment
Starting the double-screw conveyor and the spin flash dryer, opening a material conveying valve of a circulating pump to the double-screw conveyor, and conveying the materials in the hydrolysis concentration device to the spin flash dryer for drying. The liquid material entering the double screw conveyor is maintained and enters the spin flash dryer at the end in a powder particle form. The inlet air temperature of the spin flash dryer is set to be 120+/-5 ℃, the feeding speed is adjusted to enable the outlet air temperature to be within the range of 80+/-5 ℃, the rotating speed of a host machine of the spin flash dryer is adjusted, and the proportion of the fineness of the product within the range of 25-100 meshes is not less than 98%.
The materials output from the spin flash dryer enter a mixer (meanwhile, an anti-caking agent is added in a proper amount), and after being uniformly mixed by a verification program, the materials are sampled and detected, wherein the calcium lactate content is 38.86%, the free lactic acid content is 58.00%, the total lactic acid content is 58.33%, the water content is 1.36% and the silicon dioxide content is 1.50%. And packaging and warehousing the mixed materials to obtain 3100 kg of finished lactic acid powder sour agent, wherein the total yield is about 94.3%.
Example 2
1 preparation of materials
Mixing calcium carbonate: 1000kg of distilled water is injected into the size mixing tank, 700kg of food-grade calcium carbonate is added under stirring and is prepared into slurry, and stirring is kept until discharging is finished. Lactic acid feed: 3700kg of lactic acid with a nominal content of 88.2% was pumped once into the metering tank.
2 reaction
Firstly, about 5kg of raw material lactic acid is input into the reaction kettle, and the feeding is stopped immediately after the bottom of the reaction kettle is filled and sealed. Then the calcium carbonate slurry is input into the reaction kettle for one time, and stirring of the reaction kettle is startedMixing and heating the mixture to 60-80 deg.c. Slowly opening a lactic acid feeding valve, adding raw material lactic acid into the reaction kettle, and reacting with calcium carbonate under stirring. Bubble (CO) is released during the reaction 2 ) And the reflux quantity of the metering tank is regulated under the condition of keeping the small opening degree of the feed valve and not frequently changing. The lactic acid feed valve was closed when the reaction solution pH was measured to be approximately 4.5, and about 1420Kg of lactic acid was consumed as a raw material. After stirring for 20 minutes, the reaction solution was sampled again to measure about pH 4.7, and the feed valve was opened to add about 60 kg of lactic acid as a raw material and stirred for 10 minutes, and the reaction solution was observed as clear from the sight glass at the upper portion of the reaction vessel.
And opening and setting a heating and heat-preserving system of the transfer tank I, and inputting the clarified reaction liquid in the reaction kettle into the transfer tank I at one time, wherein the temperature of materials in the tank is maintained to be 80+/-2 ℃. And starting and setting a heating and heat-preserving system of the candle filter, inputting the reaction liquid in the transfer tank I into the candle filter for rough filtration, and maintaining the temperature of the material flowing out of the candle filter to be 90+/-5 ℃. And (3) starting and setting a heating and heat-preserving system of the transfer tank II, inputting clarified filtrate into the transfer tank II, and maintaining the temperature of materials in the tank to be 90+/-5 ℃. And starting and setting a heating and heat-preserving system of the precise filter, inputting the reaction liquid in the transfer tank II into the precise filter for continuous precise filtration, and inputting the filtered liquid after the precise filtration into the hydrolysis concentration device.
3 hydrolysis
Materials entering the hydrolysis concentration device are stirred and hydrolyzed at the temperature of 90+/-5 ℃, and the materials are circulated and refluxed in the tank by using a material circulating pump. And sampling and measuring the calcium lactate (converted into anhydrous substance) content in the feed liquid to be 52.8% and the lactic acid content to be 1.58% when the circulating reflux is carried out for 5 min. The stirring and circulating pump were kept in normal operation, and the raw material lactic acid remaining in the metering tank was fed once into the hydrolysis concentration apparatus (3720 Kg of raw material lactic acid was consumed up to this point) and the temperature of the material in the tank was maintained at 90±5 ℃. And then sampling and detecting every 30min, and respectively measuring the free lactic acid content and the total lactic acid content. When the free lactic acid content was 38.3% and the total lactic acid content was 39.1% (difference < 1%) in the fifth measurement, the hydrolysis was judged to be completed.
And (3) maintaining normal operation of the stirring and circulating pump, starting a vacuum device connected with an evaporation concentration port at the upper part of the hydrolysis concentration device to carry out vacuumizing, and starting a spiral tube heat exchanger connected with the circulating pump at the upper part of the hydrolysis concentration device to carry out evaporation concentration when the vacuum degree in the tank reaches-0.07+/-0.02 MPa, so as to maintain the vacuum degree of the system to-0.07+/-0.02 MPa. Sampling and measuring when the temperature of the material rises to 110+/-2 ℃, stopping concentrating and maintaining the temperature of the material at 90-110 ℃ when the calcium lactate content is 34.2%, the free lactic acid content is 51.8% and the total lactic acid content is 52.6% (the difference between the two is less than 1%).
4 post-treatment
Starting the double-screw conveyor and the spin flash dryer, opening a material conveying valve of a circulating pump to the double-screw conveyor, and conveying the materials in the hydrolysis concentration device to the spin flash dryer for drying. The liquid material entering the double screw conveyor is maintained and enters the spin flash dryer at the end in a powder particle form. The inlet air temperature of the spin flash dryer is set to be 120+/-5 ℃, the feeding speed is adjusted to enable the outlet air temperature to be within the range of 80+/-5 ℃, the rotating speed of a host machine of the spin flash dryer is adjusted, and the proportion of the fineness of the product within the range of 25-40 meshes is not less than 98%.
The materials output from the spin flash dryer enter a mixer (meanwhile, an anti-caking agent is added in a proper amount), and after being uniformly mixed by a verification program, the materials are sampled and detected, wherein the content of calcium lactate is 41.88%, the content of free lactic acid is 55.01%, the content of total lactic acid is 55.32%, the content of water is 1.86%, and the content of silicon dioxide is 1.50%. Packaging and warehousing the mixed materials to obtain 3500 kg of finished lactic acid powder sour agent, wherein the total yield is about 96.3%.
Example 3
1 preparation of materials
Mixing calcium carbonate: 1300kg of distilled water is injected into the size mixing tank, 740kg of food-grade calcium carbonate is added under stirring and is prepared into slurry, and stirring is kept until discharging is finished. Lactic acid feed: 4220kg of lactic acid having a content of 100.2% was pumped into the metering tank at a time.
2 reaction
Firstly, about 5kg of raw material lactic acid is input into the reaction kettle, and the feeding is stopped immediately after the bottom of the reaction kettle is filled and sealed. Then carbonic acid is addedThe calcium slurry is fed into the reaction kettle once, the stirring and heating device of the reaction kettle is started, and the temperature of the materials is set to be 60-80 ℃. Slowly opening a lactic acid feeding valve, adding raw material lactic acid into the reaction kettle, and reacting with calcium carbonate under stirring. Bubble (CO) is released during the reaction 2 ) And the reflux quantity of the metering tank is regulated under the condition of keeping the small opening degree of the feed valve and not frequently changing. The lactic acid feed valve was closed when the reaction solution pH was measured to be approximately 4.5, and about 1320Kg of lactic acid as a raw material was consumed. After stirring for 20 minutes, the reaction solution was sampled again to measure the pH of about 4.7, and the feed valve was opened to add about 40kg of lactic acid as a raw material and stirred for 10 minutes, and the reaction solution was observed as clear from the sight glass at the upper part of the reaction vessel.
And opening and setting a heating and heat-preserving system of the transfer tank I, and inputting the clarified reaction liquid in the reaction kettle into the transfer tank I at one time, wherein the temperature of materials in the tank is maintained to be 80+/-2 ℃. And starting and setting a heating and heat-preserving system of the candle filter, inputting the reaction liquid in the transfer tank I into the candle filter for rough filtration, and maintaining the temperature of the material flowing out of the candle filter to be 90+/-5 ℃. And (3) starting and setting a heating and heat-preserving system of the transfer tank II, inputting clarified filtrate into the transfer tank II, and maintaining the temperature of materials in the tank to be 90+/-5 ℃. And starting and setting a heating and heat-preserving system of the precise filter, inputting the reaction liquid in the transfer tank II into the precise filter for continuous precise filtration, and inputting the filtered liquid after the precise filtration into the hydrolysis concentration device.
3 hydrolysis
Materials entering the hydrolysis concentration device are stirred and hydrolyzed at the temperature of 90+/-5 ℃, and the materials are circulated and refluxed in the tank by using a material circulating pump. And sampling and measuring the calcium lactate (converted into anhydrous substance) content in the feed liquid to be 53.00% and the lactic acid content to be 1.68% when the circulating reflux is carried out for 5 min. The stirring and circulating pump were kept in normal operation, and the raw material lactic acid remaining in the metering tank was fed once into the hydrolysis concentration apparatus (4220 Kg of raw material lactic acid was consumed so far in total) and the temperature of the material in the tank was maintained at 90±5 ℃. And then sampling and detecting every 30min, and respectively measuring the free lactic acid content and the total lactic acid content. When the free lactic acid content was 48.3% and the total lactic acid content was 49.1% (difference < 1%) in the sixth measurement, the hydrolysis was judged to be completed.
And (3) maintaining normal operation of the stirring and circulating pump, starting a vacuum device connected with an evaporation concentration port at the upper part of the hydrolysis concentration device to carry out vacuumizing, and starting a spiral tube heat exchanger connected with the circulating pump at the upper part of the hydrolysis concentration device to carry out evaporation concentration when the vacuum degree in the tank reaches-0.07+/-0.02 MPa, so as to maintain the vacuum degree of the system to-0.07+/-0.02 MPa. Sampling and measuring when the temperature of the material is raised to 110+/-2 ℃, stopping concentrating and maintaining the temperature of the material at 90-110 ℃ when the content of calcium lactate is 33.12%, the content of free lactic acid is 56.79% and the total content of lactic acid is 56.90% (the difference between the two is less than 1%).
4 post-treatment
Starting the double-screw conveyor and the spin flash dryer, opening a material conveying valve of a circulating pump to the double-screw conveyor, and conveying the materials in the hydrolysis concentration device to the spin flash dryer for drying. The liquid material entering the double screw conveyor is maintained and enters the spin flash dryer at the end in a powder particle form. The inlet air temperature of the spin flash dryer is set to be 120+/-5 ℃, the feeding speed is adjusted to enable the outlet air temperature to be within the range of 80+/-5 ℃, and the rotating speed of a main machine of the spin flash dryer is adjusted to enable the fineness of the product to be more than or equal to 98% within the range of 40 meshes.
The materials output from the spin flash dryer enter a mixer (meanwhile, an anti-caking agent is added in a proper amount), and after being uniformly mixed by a verification program, the materials are sampled and detected, wherein the calcium lactate content is 36.00%, the free lactic acid content is 61.73%, the total lactic acid content is 61.88%, the moisture content is 0.86%, and the silicon dioxide content is 1.50%. And packaging and warehousing the mixed materials to obtain 4300 kg of finished lactic acid powder sour agent, wherein the total yield is about 95.2%.

Claims (8)

1. A one-step production device of an acidity regulator lactic acid powder is characterized in that: the equipment comprises a metering tank, a slurry mixing tank, a reaction kettle, a transfer tank, a filter, a hydrolysis concentration device, a conveyor, a dryer and a mixer; wherein the feed inlet of the reaction kettle is respectively connected with the feed inlets of the metering tank and the slurry mixing tank, the feed inlet of the reaction kettle is connected with the feed inlet of the transfer tank, and the transfer tank is sequentially connected with the filter, the hydrolysis concentration device, the conveyor, the dryer and the mixer through pipelines; the number of the transfer tanks and the number of the filters are two, namely a transfer tank I, a transfer tank II, a filter I and a filter II, wherein the feed inlet of the transfer tank I is connected with the feed inlet of the reaction kettle, the feed outlet of the transfer tank I is connected with the feed inlet of the filter I, the feed inlet of the filter I is connected with the feed inlet of the transfer tank I and the feed inlet of the transfer tank II, the feed inlet of the transfer tank II is connected with the feed inlet of the filter II, and the feed outlet of the filter II is connected with the feed inlet of the transfer tank II and the feed inlet of the hydrolysis concentration device; the hydrolysis concentration device comprises a tank body, a heating device, a stirring device, a material circulating pump, a heat exchanger and a pressure reducing device, wherein the heating device is arranged on the surface of the tank body and is used for heating materials in the tank; the top of the tank body is provided with a stirring port, an evaporation concentration port, a reflux port, a material circulating pump port and a manhole, and the stirring device, the pressure reducing device, the material circulating pump and the heat exchanger are respectively connected with the stirring port, the evaporation concentration port, the material circulating pump port and the reflux port; the material circulating pump conveys the material in the tank to the heat exchanger through a submerged pump discharging pipe arranged in the tank body and returns to the tank again through a backflow port; a discharge port is arranged on the circulating reflux pipeline of the material and is connected with a conveyor; raw materials of lactic acid and calcium carbonate respectively enter a reaction kettle through a metering tank and a slurry mixing tank, obtained reaction liquid enters a hydrolysis concentration device after passing through a transfer tank and a filter, materials which are hydrolyzed and concentrated to a certain concentration are sent to a dryer to be dried by the conveyor, and finally enter a mixer to be homogenized, packaged and put in storage.
2. The production facility of claim 1, wherein: the heating device on the hydrolysis concentration device comprises a heating jacket fixed at the bottom of the tank body and a heating winding pipe surrounding the tank body, and the heating jacket, the heating winding pipe and the heat exchanger are all communicated with a heat source medium.
3. The production facility of claim 1, wherein: the conveyor is specifically a double-screw conveyor, the dryer is specifically a spin flash dryer, and the separator matched with the spin flash dryer is a cyclone separator.
4. A process for the production of lactic acid powder as claimed in any one of claims 1 to 3, characterised in that it comprises the steps of: (a) Adding calcium carbonate and water into a size mixing tank, uniformly mixing to obtain calcium carbonate slurry, and adding lactic acid into a metering tank; (b) The calcium carbonate slurry and the lactic acid are proportionally input into a reaction kettle for reaction, the mixed materials are conveyed to a transfer tank for temporary storage after being sampled and detected to be qualified in the period, and then are input into a filter for filtration; (c) Delivering the filtered material reaching the standard to a hydrolysis concentration device, stirring while keeping the material circulating reflux, and concentrating the hydrolyzed material by circulating reflux to a heat exchanger of the hydrolysis concentration device; (d) After the concentrated materials are detected to be qualified, the materials are input into a dryer for drying by a conveyor, the obtained solids are separated by a separator and then enter a mixer for homogenization, and finally the materials are packaged; wherein the feed inlet of reation kettle links to each other with the discharge gate of metering tank, size mixing tank respectively, and the discharge gate of reation kettle links to each other with the feed inlet of transfer jar, and the transfer jar passes through the pipeline and links to each other with filter, hydrolysis concentration device, conveyer, desiccator, separator, mixer in proper order, and the heat exchanger links to each other with the backward flow mouth at hydrolysis concentration device jar body top.
5. The process of claim 4, wherein: the mass feed ratio of calcium carbonate, lactic acid and water in the size mixing tank and the metering tank in the step (a) is 400-900:3000-4500:800-1500, wherein the content of free lactic acid and the total content of lactic acid in the acidity regulator lactic acid powder prepared in the step (d) are controlled to be 55-62%, and the difference between the free lactic acid and the total content of lactic acid is not more than 1%; and (b) adding a small amount of lactic acid to fill the bottom of the reaction kettle, adding calcium carbonate slurry at one time, and slowly adding lactic acid to react.
6. The process of claim 4, wherein: the temperature of the materials in the reaction kettle in the step (b) is maintained at 60-80 ℃, sampling and detection are continuously carried out in the reaction process, and lactic acid is added into the reaction kettle according to the situation; after the pH value of the materials in the reaction kettle is maintained at 4.8-5.2, the reaction is considered to be completed, and lactic acid which is equivalent to 5% of the theoretical feeding amount is fed again, so that the pH value of the mixed materials is less than 4.5; the temperature of the materials in the transfer tank I is maintained at 75-85 ℃, the temperature of the materials in the transfer tank II is maintained at 85-95 ℃, and the materials are subjected to rough filtration by the filter I and fine filtration by the filter II and then enter the hydrolysis concentration heating device.
7. The process of claim 4, wherein: the content of calcium lactate in the material input into the hydrolysis concentration device is controlled to be 45% -55%, the temperature of the material is controlled to be 85-95 ℃ in the stirring and reflux process, the free lactic acid content and the total lactic acid content are continuously sampled and detected, and the lactic acid is optionally added to match a product target value, and the hydrolysis is considered to be completed when the total lactic acid content-free lactic acid content is less than or equal to 1%; after hydrolysis, stirring and refluxing are maintained, the vacuum degree in the hydrolysis concentration device is pumped to-0.09 MPa to-0.05 MPa, the materials are heated to 100-115 ℃ by a heat exchanger for concentration, and when the total content of calcium lactate and free lactic acid in the materials reaches 88% -92%, the reflux, stirring and heating are stopped, and the materials are cooled to 90-110 ℃.
8. The process of claim 4, wherein: in the step (d), the air inlet temperature of the dryer is 115-125 ℃, the air outlet temperature is 75-85 ℃, the moisture content of the material output from the dryer is less than or equal to 2%, and the fineness is randomly regulated and controlled within the range of 25-100 meshes.
CN202111459321.4A 2021-12-02 2021-12-02 One-step production equipment and production method of acidity regulator lactic acid powder Active CN114177855B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202111459321.4A CN114177855B (en) 2021-12-02 2021-12-02 One-step production equipment and production method of acidity regulator lactic acid powder

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202111459321.4A CN114177855B (en) 2021-12-02 2021-12-02 One-step production equipment and production method of acidity regulator lactic acid powder

Publications (2)

Publication Number Publication Date
CN114177855A CN114177855A (en) 2022-03-15
CN114177855B true CN114177855B (en) 2023-06-13

Family

ID=80603235

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202111459321.4A Active CN114177855B (en) 2021-12-02 2021-12-02 One-step production equipment and production method of acidity regulator lactic acid powder

Country Status (1)

Country Link
CN (1) CN114177855B (en)

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BRPI0513256A (en) * 2004-07-15 2008-04-29 Purac Biochem Bv Method for the preparation of a stable powdered metal lactate salt and stable metal lactate salt
JP2015531754A (en) * 2012-08-01 2015-11-05 ピュラック バイオケム ビー． ブイ． Lactate powder and method for producing the same
DE102012016284A1 (en) * 2012-08-19 2014-02-20 Dr. Jung Willi Method for manufacturing lactates e.g. calcium lactates, in fermentation process for manufacturing amino acid compounds in e.g. food market, involves pumping lactate to container, and drying lactate in drier to form end product as powder
CN104117327B (en) * 2014-07-11 2016-08-24 武汉三江航天固德生物科技有限公司 A kind of low temperature method of granulating of powder lactic acid
CN107960637B (en) * 2017-12-28 2021-03-23 河南金丹乳酸科技股份有限公司 Process for preparing sodium lactate powder
CN108157932B (en) * 2017-12-30 2021-03-30 湖北壮美生物科技有限公司 Double-screw extrusion mixing and drying-free preparation method of compound food additive lactic acid powder
CN110368886A (en) * 2019-07-26 2019-10-25 许正 A kind of preparation method of solid lactic acid
CN110642702B (en) * 2019-09-10 2023-02-10 湖北壮美生物科技有限公司 Industrial preparation device of sodium lactate powder with high purity and low water content and corresponding preparation method
CN111850056A (en) * 2020-07-15 2020-10-30 望江县同心农业专业合作社 Production method of lactic acid powder

Also Published As

Publication number Publication date
CN114177855A (en) 2022-03-15

Similar Documents

Publication Publication Date Title
CN203123863U (en) Automatic dry powder medicament preparing and adding device
CN204865825U (en) Automatic throw polymeric kettle of material stirring
CN104028129A (en) Automatic dissolving apparatus for production of casein and automatic dissolving method
CN114177855B (en) One-step production equipment and production method of acidity regulator lactic acid powder
CA2864023C (en) Process for preparing animal feed
CN101032264A (en) Producing method of novel soybean milk powder and manufacturing line
CN203417608U (en) Liquid powder mixing machine
CN104719484B (en) A kind of production method of milk tablet base stock powder and the direct tablet compressing method of milk tablet
CN202246515U (en) Caramel color boiling device
CN214680164U (en) Automatic washing device for chloralkane
CN215873350U (en) Online steamed system of point of efflux
CN207355408U (en) A kind of honey Finish Machining System
CN105418414B (en) A kind of production method of single, double tristerin
CN104542990A (en) Processing technique of milk powder
CN107583482A (en) Sugar refinery molasses serial dilution intelligence control system
CN219580552U (en) Calcium phosphate continuous reaction device
CN207667576U (en) A kind of sodium alginate expanding apparatus
CN215234042U (en) Automatic batching device for producing furfural
CN215028408U (en) Automatic accurate batching device for black garlic fermentation production
CN205653182U (en) Improve device of carbonization sodium bicarbonate granularity
CN208639511U (en) One Yeasts beverage agitating heater
CN220496043U (en) Automatic lime milk preparing system in sugar refining and clarifying process
CN204583192U (en) A kind of reaction unit for making calcium propionate
CN117923447B (en) Method and device for continuously producing calcium hydrophosphate by cascade reaction kettles
CN220867358U (en) Brewing and separating system for deep processing of grains

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