WO2018102835A1 - Apparatus and method for evaporation to concentrate sensitive substances in solutions - Google Patents

Apparatus and method for evaporation to concentrate sensitive substances in solutions Download PDF

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Publication number
WO2018102835A1
WO2018102835A1 PCT/VN2017/000011 VN2017000011W WO2018102835A1 WO 2018102835 A1 WO2018102835 A1 WO 2018102835A1 VN 2017000011 W VN2017000011 W VN 2017000011W WO 2018102835 A1 WO2018102835 A1 WO 2018102835A1
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WO
WIPO (PCT)
Prior art keywords
heat
contact surface
liquid contact
vapor
enhanced structure
Prior art date
Application number
PCT/VN2017/000011
Other languages
French (fr)
Inventor
Minh Tan NGUYEN
M. Samhaber WOLFGANG
Original Assignee
Nmt Technology Co., Ltd
Gvt Verfahrenstechnik Gmbh
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 Nmt Technology Co., Ltd, Gvt Verfahrenstechnik Gmbh filed Critical Nmt Technology Co., Ltd
Publication of WO2018102835A1 publication Critical patent/WO2018102835A1/en

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Classifications

    • 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
    • A23L2/00—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation
    • A23L2/02—Non-alcoholic beverages; Dry compositions or concentrates therefor; Their preparation containing fruit or vegetable juices
    • A23L2/08—Concentrating or drying of juices
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23C—DAIRY PRODUCTS, e.g. MILK, BUTTER OR CHEESE; MILK OR CHEESE SUBSTITUTES; MAKING THEREOF
    • A23C1/00—Concentration, evaporation or drying
    • A23C1/12—Concentration by evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating

Definitions

  • the present invention relates to the evaporation of heat-sensitive fluids at moderate temperature and ambient pressure, and more particularly to an apparatus for removal of the solvent of heat-sensitive fluids and the method applied in this apparatus.
  • This is especially suitable for evaporating of solvents of heat-sensitive solutions, for example fruit juice, vegetable juice, milk, liquid food, post-fermentation broth, crude enzyme, herbal extracts, solvent extracts.
  • the conventional thermal process of evaporation to concentrate solutions is often carried out at the by boiling temperature of the solution.
  • the solutions have been normally heated to the respective boiling temperature while at temperatures above 60°C, colour change, flavour loss and decreased sensory quality of heat-sensitive substances take place already.
  • membrane processes can also be not efficiently applied for the concentration if the feed is viscous, heavy cloudy and exhibit high osmotic pressures.
  • Vacuum evaporation can be applied to concentrate the solution at temperatures lower than 60°C.
  • vacuum evaporator has a high investment cost and requires complex operation and improper operation, which is not suited to be applied at small and medium enterprises in developing countries like Vietnam.
  • US4472450 refers to equipment that reduces the water amount in honey from high levels (e.g. 20% to 35% water) to less than 18%.
  • This device uses a rotating wing partially embedded in the bulk feed kept in the container, forming a film that is attached to the rotating wing. Hot air (from 45° C to 75°C) is blown into the rotating part above the fluid level in the container, thereby gradually reduce the water content of the solution.
  • Hot air above 60°C can cause local colour change and reduction of sensorial quality of the product.
  • FR2672473A refers to a device for reducing the water content of grape juice before fermentation.
  • the grape juice is dispersed continuously in the form of droplets onto a heat exchange surface in a wet tower through which a gas stream, for example ambient air, preheated or dehumidified.
  • the corresponding device comprises a wet tower and has a heater and circulating said inserted gas stream.
  • the wet tower there is dry air flow at low temperature and at ambient pressure which is usually circulated. The continuous process is carried out until the desired concentration of sugar is reached.
  • the purpose of the invention is to increase the evaporation efficiency of heat-sensitive substances in solutions at moderate temperature and ambient pressure.
  • the invention provides an evaporation apparatus concept that can increase the concentration of heat-sensitive solutions at low temperature and ambient pressure.
  • the apparatus consists of: working unit is a closed chamber divided into two adjacent compartments, the evaporating and the condensing compartment, which are separated by a baffle at lower position and connected to each other at the top position;
  • the evaporating compartment consists of an underneath space which filled with the vapor/liquid contact surface enhanced structure, right above is a fluid irrigation unit, the upper space is free and connected with the condensing compartment;
  • the primary heat exchanger is arranged within the vapor/liquid contact surface enhanced structure in order to implement first heating up of the feed;
  • the condensing compartment consists of indirect heat exchangers arranged parallel to each other to perform a condensation process whereby the thermal sensitive solution is traveling upward, and the heat transfer surface of the indirect heat exchangers can be varied by increasing or decreasing the number of indirect heat exchangers;
  • a blower is arranged between the condensing compartment and the evaporating compartment in order to ensure the air circulation within the working unit; fluid circulation reservoir; circulation pump;
  • condensate collecting container heat pump connected with cooling and heating loop; switch cabinet connected with measurement devices to monitor and control the operating parameters.
  • the vapor/liquid contact surface enhanced structure is selected from a group comprising random or structured packings with specific surface area ranges from 100 to 2500 m 2 / m 3 , preferably from 300 to 2000 m 2 /m 3 , more preferably from 500 to 1600 m 2 /m 3 and most preferably 600 to 1200 m 2 /m 3 .
  • the indirect heat exchanger is selected from the group comprising of tube heat transfer exchanger or plate heat exchanger.
  • the first heating is implemented by primary heat exchanger selected from the group comprising of tube heat transfer, plate heat transfer and pipe-in-pipe heat exchanger.
  • the indirect heat exchanger is selected from the group comprising of plate heat exchangers with a heat transfer surface ranges from 100 to 1800 m 2 /m 3 , preferably from 300 to 1400 m 2 /m 3 , most preferably from 500 to 1000 m 2 /m 3 .
  • the indirect heat exchangers are arranged in parallel and form an angle of -15° to 60° from the vertical, preferably from -5° to 45°, most preferably from 0° to 30°.
  • the heat transfer surface can be varied by increasing or decreasing the number of indirect heat exchangers.
  • air circulation unit is a fan or blower.
  • heat-sensitive solutions were selected from the group comprising of juices, vegetable juices, milk, liquid foods, fermentation broths, crude enzymes, herbal extracts, solvent extracts.
  • heat-sensitive solutions with or without fibres and pulp.
  • this apparatus is multi-feed compatible, which can be used for processing of different feeds.
  • this apparatus can be controlled and monitored on-site or remotely over IP.
  • this invention relates to evaporation method for concentrating of heat- sensitive solutions at moderate temperature and ambient pressure comprising steps:
  • temperature of the fluid contributed within the vapor/liquid contact surface enhanced structure is kept within the rage from 20°C to 60°C, preferably from 25°C to 55°C, most preferably from 35°C to 50°C.
  • loading of the vapor/liquid contact surface enhanced structure is kept within the rage from 0,1 m 3 /m 2 h to 10 m 3 /m 2 h, preferably from 0,5 m 3 /m 2 h to 9 m 3 /m 2 h, most preferably from 1 m 3 /m 2 h to 7 m 3 /m 2 h.
  • the primary and secondary heat exchanger use heat carrier, which is hot water from heating unit of the heat pump.
  • the indirect heat exchange use heat carrier from cold unit of the heat pump kept from the range from- 25 °C to +18°C, preferably from - 20 °C to +15°C.
  • heat pump is used for taking the heat from the condensation to supply to the evaporation in order to maximize the heat usage efficiency.
  • inert gas introduced into the fluid circulation reservoir is selected from the group comprises of C0 2 , N 2 and its mixture.
  • air is circulated in the space of the working unit between the evaporating compartment and the condensing chamber to maximize the retention of aromas and volatile compounds in the product.
  • Fig. 1 is schematic diagram of the apparatus for evaporation to concentrate heat-sensitive solutions at moderate temperature and ambient pressure
  • the present invention refers to an apparatus for evaporation to concentrate heat- sensitive solutions at moderate temperature and ambient pressure
  • working unit is a closed chamber divided into two adjacent compartments, the evaporating 1.1 and the condensing compartment 1.2, which are separated by a baffle at lower position and connected to each other at the top position
  • the evaporating compartment 1.1 consists of an underneath space which filled with the vapor/liquid contact surface enhanced structure 1.1.1, right above is a fluid irrigation unit 1.1.2, the upper space is free and connected with the condensing compartment 1.2
  • the primary heat exchanger 1.1.1.1 is arranged within the vapor/liquid contact surface enhanced structure in order to implement first heating up of the feed;
  • the condensing compartment 1.2 consists of indirect heat exchangers 1.2.1 arranged parallel to each other to perform a condensation process whereby the thermal sensitive solution is traveling upward, and the heat transfer surface of the indirect heat exchangers 1.2. lean be varied by increasing or decreasing the number of indirect heat exchangers 1.2.1;
  • a blower 1.3 is arranged between the condensing compartment 1.2 and the evaporating compartment 1.1 in order to ensure the air circulation within the working unit 1 ; fluid circulation reservoir 2;
  • secondary heat exchanger 4 condensate collecting container 5; heat pump connected with cooling 6.2 and heating loop 6.1 ; switch cabinet 7 connected with measurement devices to monitor and control the operating parameters.
  • the vapor/liquid contact surface enhanced structure 1.1.1 is selected from a group comprising random or structured packings with specific surface area ranges from 100 to 2500 m 2 / m 3 , preferably from 300 to 2000 m 2 /m 3 , more preferably from 500 to 1600 m 2 /m 3 and most preferably 600 to 1200 m 2 /m 3 .
  • the indirect heat exchanger 1.1.1.1. is selected from the group comprising of tube heat transfer exchanger or plate heat exchanger.
  • the first heating is implemented by primary heat exchanger 4 selected from the group comprising of tube heat transfer, plate heat transfer and pipe-in-pipe heat exchanger.
  • the indirect heat exchanger 1.2.1 is selected from the group comprising of plate heat exchangers with a heat transfer surface ranges from 100 to 1800 m 2 /m 3 , preferably from 300 to 1400 m 2 /m 3 , most preferably from 500 to 1000 m 2 /m 3 .
  • the indirect heat exchangers 1.2.1 are arranged in parallel and form an angle of -15° to 60° from the vertical, preferably from -5° to 45°, most preferably from 0° to 30°.
  • the heat transfer surface can be varied by increasing or decreasing the number of indirect heat exchangers 1.2.1.
  • air circulation unit 1.3 is a fan or blower.
  • heat-sensitive solutions were selected from the group comprising of juices, vegetable juices, milk, liquid foods, fermentation broths, crude enzymes, herbal extracts, solvent extracts.
  • heat-sensitive solutions with or without fibres and pulp.
  • this apparatus is multi-feed compatible, which can be used for processing of different feeds.
  • this apparatus can be controlled and monitored on-site or remotely over IP.
  • temperature of the fluid contributed within the vapour/liquid contact surface enhanced structure 1.1.1 is kept within the rage from 20°C to 60°C, preferably from 25°C to 55°C, most preferably from 35°C to 50°C.
  • loading of the vapour/liquid contact surface enhanced structure 1.1.1 is kept within the rage from 0,1 m 3 /m 2 h to 10 m 3 /m 2 h, preferably from 0,5 m 3 /m 2 h to 9 m 3 /m 2 h, most preferably from 1 m 3 /m 2 h to 7 m 3 /m 2 h.
  • the primary 4 and secondary heat exchanger 1.1.1.1 use heat carrier, which is hot water from heating unit 6.1 of the heat pump 6.
  • the indirect heat exchange 1.2.1 use heat carrier from cold unit 6.2 of the heat pump 6 kept from the range from -25 °C to +18°C, preferably from -20 °C to +15°C.
  • heat pump 6 is used for taking the heat from the condensation to supply to the evaporation in order to maximize the heat usage efficiency.
  • inert gas introduced into the fluid circulation reservoir 2 is selected from the group comprises of C0 2 , N 2 and its mixture.
  • air is circulated in the space of the working unit between the evaporating compartment 1.1 and the condensing chamber 1.2 to maximize the retention of aromas and volatile compounds in the product.
  • Examples 2 producing lychee fruit concentrate leading 12.5kg lychee fruit juice 16.6 °Brix into circulation reservoir 2; pumping heat sensitive solutions with circulation pump 3 to the first heat exchanger 4; irrigating heat sensitive solutions on the vapor/liquid contact surface enhanced structure 1.1.1 with a flux of 1.4L/min, fluids is then be equally distributed within the above mentioned vapor/liquid contact surface enhanced structure 1.1.1 in form of droplets and flow top down, the solution is simultaneously be heated up by the primary heat exchanger located within the vapor/liquid contact surface enhanced structure 1.1.1; Fruit juice temperature is kept from 42 °C den 45°C; heat carrier from cold unit 6.2 is kept from -20°C d8n -8°C; heat carrier from hot unit 6.1 is kept from 75°C den 60°C blowing air 1.3 through the vapor/liquid contact surface enhanced structure 1.1.1 in opposite direction of the fluid flow; circulating air in order to entrain solvent vapour from evaporating compartment 1.1 to condensing compartment 1.2 through the connected space between these 2 compartments;
  • lychee fruit concentrate containes 88% ester, 78% acohol, 88% ankane in comparision with the fresh fruit juice.
  • Examples 5 concentration of Protease solution leading 8.3kg onion extract 2°Brix/0.4U/mL into circulation reservoir 2; pumping heat sensitive solutions with circulation pump 3 to the first heat exchanger 4;
  • Fruit juices apple juice, water melone juice, coconut water, lychee juice, lime juice, nuoc tao, dragon fruit juice, guave juice,
  • Apparatus of this invention can also be used for evaporation of heat-stable solutions

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Health & Medical Sciences (AREA)
  • Nutrition Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

The invention relates to the apparatus and method for evaporation to concentrate heat- sensitive solutions at moderate temperature and ambient pressure by irrigating heat- sensitive solutions on the vapor/liquid contact surface enhanced structure (1.1.1), fluids is then be equally distributed within the vapor/liquid contact surface enhanced structure (1.1.1) in form of droplets and flow top down, the solution is simultaneously heated up by the primary heat exchanger located within the vapor/liquid contact surface enhanced structure (1.1.1). Air is blown through the vapor/liquid contact surface enhanced structure (1.1) in opposite direction of the fluid flow and circulated to entrain solvent vapour from evaporating compartment (1.1) to condensing compartment (1.2) through the connected space between these 2 compartments. Condensation of solvent vapour takes place on the surface of the indirect heat exchanger (1.2.1). Inert gas is introduced into the fluid circulation reservoir (2) in order to minimize the effect of oxidation processes to achieve high quality of concentrated product.

Description

Title
APPARATUS AND METHOD FOR EVAPORATION TO CONCENTRATE SENSITIVE SUBSTANCES IN SOLUTIONS
Technical field of the invention
The present invention relates to the evaporation of heat-sensitive fluids at moderate temperature and ambient pressure, and more particularly to an apparatus for removal of the solvent of heat-sensitive fluids and the method applied in this apparatus. This is especially suitable for evaporating of solvents of heat-sensitive solutions, for example fruit juice, vegetable juice, milk, liquid food, post-fermentation broth, crude enzyme, herbal extracts, solvent extracts.
Background of the invention
The conventional thermal process of evaporation to concentrate solutions is often carried out at the by boiling temperature of the solution. The solutions have been normally heated to the respective boiling temperature while at temperatures above 60°C, colour change, flavour loss and decreased sensory quality of heat-sensitive substances take place already. On the other hands, membrane processes can also be not efficiently applied for the concentration if the feed is viscous, heavy cloudy and exhibit high osmotic pressures. Vacuum evaporation can be applied to concentrate the solution at temperatures lower than 60°C. However, vacuum evaporator has a high investment cost and requires complex operation and improper operation, which is not suited to be applied at small and medium enterprises in developing countries like Vietnam.
US4472450 refers to equipment that reduces the water amount in honey from high levels (e.g. 20% to 35% water) to less than 18%. This device uses a rotating wing partially embedded in the bulk feed kept in the container, forming a film that is attached to the rotating wing. Hot air (from 45° C to 75°C) is blown into the rotating part above the fluid level in the container, thereby gradually reduce the water content of the solution.
This device has following disadvantages:
• The rotating vane in the fluid will create bubbles. This foam layer reduces the diffusion of vapors and moisture from the solution. This layer is hardly destructed while the solution is highly viscous.
• Uneven air flow reaching to the surface of the rotary wing, short contact time and low efficiency of vapor and moisture removal by the air flow, which is reflected in the small vapor pressure gradient. Low vapor and moisture removal results in longer retention time, which increases the required hot air flow, moreover it is not recirculated. This increases energy cost in particular and the production cost. Bulky equipment, low productivity
• Hot air above 60°C, can cause local colour change and reduction of sensorial quality of the product.
FR2672473A refers to a device for reducing the water content of grape juice before fermentation. For this, the grape juice is dispersed continuously in the form of droplets onto a heat exchange surface in a wet tower through which a gas stream, for example ambient air, preheated or dehumidified. The corresponding device comprises a wet tower and has a heater and circulating said inserted gas stream. In the wet tower, there is dry air flow at low temperature and at ambient pressure which is usually circulated. The continuous process is carried out until the desired concentration of sugar is reached.
This device has following disadvantages:
• Due to the fact that in the tower are heat transfer surfaces that increase the tower's resistance and decrease the velocity of the air flow, leading to a decrease of moisture or vapor removal yield. Therefore, a high air flow is required. A curtain part of the juice is entrained" by the outgoing air flow. Three should be a fluid recovery unit. High pressure in the tower also causes a decrease in the moisture or vapor transfer from the fluid to the air flow.
• Fluid fall from the top plate to the bottom plate with the free fall speed so that the amount of transferred moisture from the fluid to the gas is not much, which also means that the reduction of the water content in one circulation cycle is not large. Therefore, the number of cycles should be increased. The energy cost to circulate the fluid to the top sieve is significant. Thus, in a cycle of air movement, the moisture or vapor amount transferred to the air flow is quite small. The amount of air for remove 1 kg of moisture or vapor from the solution is big and cause high investment cost as well as operating costs.
Disclosure of invention
The purpose of the invention is to increase the evaporation efficiency of heat-sensitive substances in solutions at moderate temperature and ambient pressure.
To achieve the above purpose, the invention provides an evaporation apparatus concept that can increase the concentration of heat-sensitive solutions at low temperature and ambient pressure. The apparatus consists of: working unit is a closed chamber divided into two adjacent compartments, the evaporating and the condensing compartment, which are separated by a baffle at lower position and connected to each other at the top position;
the evaporating compartment consists of an underneath space which filled with the vapor/liquid contact surface enhanced structure, right above is a fluid irrigation unit, the upper space is free and connected with the condensing compartment; the primary heat exchanger is arranged within the vapor/liquid contact surface enhanced structure in order to implement first heating up of the feed; the condensing compartment consists of indirect heat exchangers arranged parallel to each other to perform a condensation process whereby the thermal sensitive solution is traveling upward, and the heat transfer surface of the indirect heat exchangers can be varied by increasing or decreasing the number of indirect heat exchangers; a blower is arranged between the condensing compartment and the evaporating compartment in order to ensure the air circulation within the working unit; fluid circulation reservoir; circulation pump;
secondary heat exchanger;
condensate collecting container; heat pump connected with cooling and heating loop; switch cabinet connected with measurement devices to monitor and control the operating parameters.
In one embodiment, the vapor/liquid contact surface enhanced structure is selected from a group comprising random or structured packings with specific surface area ranges from 100 to 2500 m2/ m3, preferably from 300 to 2000 m2/m3, more preferably from 500 to 1600 m2/m3 and most preferably 600 to 1200 m2/m3.
In other embodiment, the indirect heat exchanger is selected from the group comprising of tube heat transfer exchanger or plate heat exchanger.
In another embodiment, the first heating is implemented by primary heat exchanger selected from the group comprising of tube heat transfer, plate heat transfer and pipe-in-pipe heat exchanger.
In another embodiment, the indirect heat exchanger is selected from the group comprising of plate heat exchangers with a heat transfer surface ranges from 100 to 1800 m2/m3, preferably from 300 to 1400 m2/m3, most preferably from 500 to 1000 m2/m3.
In another embodiment, the indirect heat exchangers are arranged in parallel and form an angle of -15° to 60° from the vertical, preferably from -5° to 45°, most preferably from 0° to 30°.
In another embodiment, the heat transfer surface can be varied by increasing or decreasing the number of indirect heat exchangers. In another embodiment, air circulation unit is a fan or blower.
In another embodiment, heat-sensitive solutions were selected from the group comprising of juices, vegetable juices, milk, liquid foods, fermentation broths, crude enzymes, herbal extracts, solvent extracts.
In another embodiment, heat-sensitive solutions with or without fibres and pulp.
In another embodiment, this apparatus is multi-feed compatible, which can be used for processing of different feeds.
In another embodiment, this apparatus can be controlled and monitored on-site or remotely over IP.
In other embodiment, this invention relates to evaporation method for concentrating of heat- sensitive solutions at moderate temperature and ambient pressure comprising steps:
leading feed into circulation reservoir; pumping heat sensitive solutions to the first heat exchanger; irrigating heat sensitive solutions on the vapor/liquid contact surface enhanced structure, fluids is then equally distributed within the above mentioned vapor/liquid contact surface enhanced structure in form of droplets and flow top down, the solution is simultaneously be heated up by the primary heat exchanger located within the vapor/liquid contact surface enhanced structure;
blowing air through the vapor/liquid contact surface enhanced structure in opposite direction of the fluid flow; circulating air in order to entrain solvent vapour from evaporating compartment to condensing compartment through the connected space between these 2 compartments;
.condensing solvent vapour on the surface of the indirect heat exchanger;
sucking of dry air into the circulation unit order to supply air flow for the next circulation; collecting concentrated solution at the bottom of the evaporating compartment and leading to the fluid circulation reservoir; collecting concentrated products through a valve on the side of fluid circulation reservoir; introducing inert gas to the fluid circulation reservoir in order to minimize the effect of oxidation processes to achieve high quality of concentrated product; collecting condensed solvent at the bottom of the condensing compartment and leading to the condensation reservoir. In one embodiment, temperature of the fluid contributed within the vapor/liquid contact surface enhanced structure is kept within the rage from 20°C to 60°C, preferably from 25°C to 55°C, most preferably from 35°C to 50°C.
In another embodiment, loading of the vapor/liquid contact surface enhanced structure is kept within the rage from 0,1 m3/m2h to 10 m3/m2h, preferably from 0,5 m3/m2h to 9 m3/m2h, most preferably from 1 m3/m2h to 7 m3/m2h.
In another embodiment, the primary and secondary heat exchanger use heat carrier, which is hot water from heating unit of the heat pump.
In another embodiment, the indirect heat exchange use heat carrier from cold unit of the heat pump kept from the range from- 25 °C to +18°C, preferably from - 20 °C to +15°C.
In another embodiment, heat pump is used for taking the heat from the condensation to supply to the evaporation in order to maximize the heat usage efficiency.
In another embodiment, inert gas introduced into the fluid circulation reservoir is selected from the group comprises of C02, N2 and its mixture.
In another embodiment, air is circulated in the space of the working unit between the evaporating compartment and the condensing chamber to maximize the retention of aromas and volatile compounds in the product.
Brief description of the drawings
Fig. 1 is schematic diagram of the apparatus for evaporation to concentrate heat-sensitive solutions at moderate temperature and ambient pressure
Detailed description of the invention
The details of one or more embodiments of the invention are set forth in the description below. The description is just for illustrative purpose, but not meant to be construed in a limiting sense. Various modifications of the disclosed embodiments, as well as alternative embodiments, will be apparent to persons skilled in the art. It is, therefore, contemplated that the appended claims will cover all modifications that fall within the true scope of the invention.
In one aspect, the present invention refers to an apparatus for evaporation to concentrate heat- sensitive solutions at moderate temperature and ambient pressure comprising: working unit is a closed chamber divided into two adjacent compartments, the evaporating 1.1 and the condensing compartment 1.2, which are separated by a baffle at lower position and connected to each other at the top position; the evaporating compartment 1.1 consists of an underneath space which filled with the vapor/liquid contact surface enhanced structure 1.1.1, right above is a fluid irrigation unit 1.1.2, the upper space is free and connected with the condensing compartment 1.2; the primary heat exchanger 1.1.1.1 is arranged within the vapor/liquid contact surface enhanced structure in order to implement first heating up of the feed;
the condensing compartment 1.2 consists of indirect heat exchangers 1.2.1 arranged parallel to each other to perform a condensation process whereby the thermal sensitive solution is traveling upward, and the heat transfer surface of the indirect heat exchangers 1.2. lean be varied by increasing or decreasing the number of indirect heat exchangers 1.2.1;
a blower 1.3 is arranged between the condensing compartment 1.2 and the evaporating compartment 1.1 in order to ensure the air circulation within the working unit 1 ; fluid circulation reservoir 2;
circulation pump 3;
secondary heat exchanger 4; condensate collecting container 5; heat pump connected with cooling 6.2 and heating loop 6.1 ; switch cabinet 7 connected with measurement devices to monitor and control the operating parameters.
In one embodiment, the vapor/liquid contact surface enhanced structure 1.1.1 is selected from a group comprising random or structured packings with specific surface area ranges from 100 to 2500 m2/ m3, preferably from 300 to 2000 m2/m3, more preferably from 500 to 1600 m2/m3 and most preferably 600 to 1200 m2/m3.
In other embodiment, the indirect heat exchanger 1.1.1.1. is selected from the group comprising of tube heat transfer exchanger or plate heat exchanger.
In another embodiment, the first heating is implemented by primary heat exchanger 4 selected from the group comprising of tube heat transfer, plate heat transfer and pipe-in-pipe heat exchanger.
In another embodiment, the indirect heat exchanger 1.2.1 is selected from the group comprising of plate heat exchangers with a heat transfer surface ranges from 100 to 1800 m2/m3, preferably from 300 to 1400 m2/m3, most preferably from 500 to 1000 m2/m3.
In another embodiment, the indirect heat exchangers 1.2.1 are arranged in parallel and form an angle of -15° to 60° from the vertical, preferably from -5° to 45°, most preferably from 0° to 30°. In another embodiment, the heat transfer surface can be varied by increasing or decreasing the number of indirect heat exchangers 1.2.1.
In another embodiment, air circulation unit 1.3 is a fan or blower.
In another embodiment, heat-sensitive solutions were selected from the group comprising of juices, vegetable juices, milk, liquid foods, fermentation broths, crude enzymes, herbal extracts, solvent extracts.
In another embodiment, heat-sensitive solutions with or without fibres and pulp.
In another embodiment, this apparatus is multi-feed compatible, which can be used for processing of different feeds.
In another embodiment, this apparatus can be controlled and monitored on-site or remotely over IP.
leading feed into circulation reservoir 2; pumping heat sensitive solutions with circulation pump 3 to the first heat exchanger 4; irrigating heat sensitive solutions on the vapor/li uid contact surface enhanced structure 1.1.1, fluids is then equally distributed within the above mentioned vapor/liquid contact surface enhanced structure 1.1.1 in form of droplets and flow top down, the solution is simultaneously heated up by the primary heat exchanger located within the vapor/liquid contact surface enhanced structure 1.1.1;
blowing air 1.3 through the vapor/liquid contact surface enhanced structure 1.1.1 in opposite direction of the fluid flow; circulating air in order to entrain solvent vapour from evaporating compartment 1.1 to condensing compartment 1.2 through the connected space between these 2 compartments; condensing solvent vapour on the surface of the indirect heat exchanger 1.2.1 ;
sucking of dry air into the circulation unit 1.3 order to supply air flow for the next circulation; collecting concentrated solution at the bottom of the evaporating compartment 1.1 and leading to the fluid circulation reservoir 2; collecting concentrated products through a valve on the side of fluid circulation reservoir 2; introducing inert gas to the fluid circulation reservoir 2 in order to minimize the effect of oxidation processes to achieve high quality of concentrated product; collecting condensed solvent at the bottom of the condensing compartment 1.2 and leading to the condensation reservoir 5. In one embodiment, temperature of the fluid contributed within the vapour/liquid contact surface enhanced structure 1.1.1 is kept within the rage from 20°C to 60°C, preferably from 25°C to 55°C, most preferably from 35°C to 50°C.
In another embodiment, loading of the vapour/liquid contact surface enhanced structure 1.1.1 is kept within the rage from 0,1 m3/m2h to 10 m3/m2h, preferably from 0,5 m3/m2h to 9 m3/m2h, most preferably from 1 m3/m2h to 7 m3/m2h.
In another embodiment, the primary 4 and secondary heat exchanger 1.1.1.1 use heat carrier, which is hot water from heating unit 6.1 of the heat pump 6.
In another embodiment, the indirect heat exchange 1.2.1 use heat carrier from cold unit 6.2 of the heat pump 6 kept from the range from -25 °C to +18°C, preferably from -20 °C to +15°C.
In another embodiment, heat pump 6 is used for taking the heat from the condensation to supply to the evaporation in order to maximize the heat usage efficiency.
In another embodiment, inert gas introduced into the fluid circulation reservoir 2 is selected from the group comprises of C02, N2 and its mixture.
In another embodiment, air is circulated in the space of the working unit between the evaporating compartment 1.1 and the condensing chamber 1.2 to maximize the retention of aromas and volatile compounds in the product.
Examples
Examples 1: producing passion fruit concentrate
leading 11.2kg passion fruit juice 15.6 °Brix into circulation reservoir 2; pumping heat sensitive solutions with circulation pump 3 to the first heat exchanger 4; irrigating heat sensitive solutions on the vapor/liquid contact surface enhanced structure 1.1.1 with a flux of 1.8L/min, fluids is then be equally distributed within the above mentioned vapor/liquid contact surface enhanced structure 1.1.1 in form of droplets and flow top down, the solution is simultaneously be heated up by the primary heat exchanger located within the vapor/liquid contact surface enhanced structure 1.1.1 ; Fruit juice temperature is kept from 40 °C den 52°C; heat carrier from cold unit 6.2 is kept from -25°C din -20°C; heat carrier from hot unit 6.1 is kept from 60°C den 65°C blowing air 1.3 through the vapor/liquid contact surface enhanced structure 1.1.1 in opposite direction of the fluid flow; circulating air in order to entrain solvent vapour from evaporating compartment 1.1 to condensing compartment 1.2 through the connected space between these 2 compartments; condensing solvent vapour on the surface of the indirect heat exchanger 1.2.1; sucking of dry air into the circulation unit 1.3 order to supply air flow for the next circulation; collecting concentrated solution at the bottom of the evaporating compartment 1.1 and leading to the fluid circulation reservoir 2;
collecting 1.8 L passion fruit concentrate 67.5°Brix through a valve on the side of fluid circulation reservoir 2; introducing inert gas to the fluid circulation reservoir 2 in order to minimize the effect of oxidation processes to achieve high quality of concentrated product; collecting condensed solvent at the bottom of the condensing compartment 1.2 and leading to the condensation reservoir.
In the passion fruit concentrate containes 86% ester, 82% alcohol, 95% ankane in comparision with the fresh passion fruit juice.
Examples 2: producing lychee fruit concentrate leading 12.5kg lychee fruit juice 16.6 °Brix into circulation reservoir 2; pumping heat sensitive solutions with circulation pump 3 to the first heat exchanger 4; irrigating heat sensitive solutions on the vapor/liquid contact surface enhanced structure 1.1.1 with a flux of 1.4L/min, fluids is then be equally distributed within the above mentioned vapor/liquid contact surface enhanced structure 1.1.1 in form of droplets and flow top down, the solution is simultaneously be heated up by the primary heat exchanger located within the vapor/liquid contact surface enhanced structure 1.1.1; Fruit juice temperature is kept from 42 °C den 45°C; heat carrier from cold unit 6.2 is kept from -20°C d8n -8°C; heat carrier from hot unit 6.1 is kept from 75°C den 60°C blowing air 1.3 through the vapor/liquid contact surface enhanced structure 1.1.1 in opposite direction of the fluid flow; circulating air in order to entrain solvent vapour from evaporating compartment 1.1 to condensing compartment 1.2 through the connected space between these 2 compartments; condensing solvent vapour on the surface of the indirect heat exchanger 1.2.1; sucking of dry air into the circulation unit 1.3 order to supply air flow for the next circulation; collecting concentrated solution at the bottom of the evaporating compartment 1.1 and leading to the fluid circulation reservoir 2; collecting 1.1L lychee fruit concentrate 68°Brix through a valve on the side of fluid circulation reservoir 2; introducing inert gas to the fluid circulation reservoir 2 in order to minimize the effect of oxidation processes to achieve high quality of concentrated product; collecting condensed solvent at the bottom of the condensing compartment 1.2 and leading to the condensation reservoir.
In the lychee fruit concentrate containes 88% ester, 78% acohol, 88% ankane in comparision with the fresh fruit juice.
Examples 3: concentration of green coffee bean extract leading 14.4kg green coffee bean extract contains 15% Chlorogenic Acid (CGA) into circulation reservoir 2;
pumping heat sensitive solutions with circulation pump 3 to the first heat exchanger 4; irrigating heat sensitive solutions on the vapor/liquid contact surface enhanced structure 1.1.1 with a flux of 3.2L/min, fluids is then be equally distributed within the above mentioned vapor/liquid contact surface enhanced structure 1.1.1 in form of droplets and flow top down, the solution is simultaneously be heated up by the primary heat exchanger located within the vapor/liquid contact surface enhanced structure 1.1.1; Fruit juice temperature is kept from 42 °C den 55°C; heat carrier from cold unit 6.2 is kept from -8°C d§n -20°C; heat carrier from hot unit 6.1 is kept from 62°C d6n 70°C
blowing air 1.3 through the vapor/liquid contact surface enhanced structure 1.1.1 in opposite direction of the fluid flow;
circulating air in order to entrain solvent vapour from evaporating compartment 1.1 to condensing compartment 1.2 through the connected space between these 2 compartments; condensing solvent vapour on the surface of the indirect heat exchanger 1.2.1; sucking of dry air into the circulation unit 1.3 order to supply air flow for the next circulation; collecting concentrated solution at the bottom of the evaporating compartment 1.1 and leading to the fluid circulation reservoir 2;
collecting 2.2L concentrate 68% CGA through a valve on the side of fluid circulation reservoir 2 after 6 hours working;
introducing inert gas to the fluid circulation reservoir 2 in order to minimize the effect of oxidation processes to achieve high quality of concentrated product;
collecting condensed Ethanol at the bottom of the condensing compartment 1.2 and leading to the condensation reservoir late use.
Examples 4: concentration of onion extract
leading 20.7kg onion extract 7°Brix into circulation reservoir 2; pumping heat sensitive solutions with circulation pump 3 to the first heat exchanger 4; irrigating heat sensitive solutions on the vapor/liquid contact surface enhanced structure 1.1.1 with a flux of 3.2L/min, fluids is then be equally distributed within the above mentioned vapor/liquid contact surface enhanced structure 1.1.1 in form of droplets and flow top down, the solution is simultaneously be heated up by the primary heat exchanger located within the vapor/liquid contact surface enhanced structure 1.1.1; Fruit juice temperature is kept from 35 °C den 42°C; heat carrier from cold unit 6.2 is kept from -9°C den -15°C; heat carrier from hot unit 6.1 is kept from 55°C den 62°C blowing air 1.3 through the vapor/liquid contact surface enhanced structure 1.1.1 in opposite direction of the fluid flow;
circulating air in order to entrain solvent vapour from evaporating compartment 1.1 to condensing compartment 1.2 through the connected space between these 2 compartments; condensing solvent vapour on the surface of the indirect heat exchanger 1.2.1; sucking of dry air into the circulation unit 1.3 order to supply air flow for the next circulation; collecting concentrated solution at the bottom of the evaporating compartment 1.1 and leading to the fluid circulation reservoir 2; collecting 1.9L onion extract concentrate 70.5°Brix through a valve on the side of fluid circulation reservoir 2 after 8 hours working; introducing inert gas to the fluid circulation reservoir 2 in order to minimize the effect of oxidation processes to achieve high quality of concentrated product;
Examples 5: concentration of Protease solution leading 8.3kg onion extract 2°Brix/0.4U/mL into circulation reservoir 2; pumping heat sensitive solutions with circulation pump 3 to the first heat exchanger 4;
irrigating heat sensitive solutions on the vapor/liquid contact surface enhanced structure 1.1.1 with a flux of 3.2L/min, fluids is then be equally distributed within the above mentioned vapor/liquid contact surface enhanced structure 1.1.1 in form of droplets and flow top down, the solution is simultaneously be heated up by the primary heat exchanger located within the vapor/liquid contact surface enhanced structure 1.1.1; Fruit juice temperature is kept from 31.5 °C den 40°C; heat carrier from cold unit 6.2 is kept from -6°C den - 10°C; heat carrier from hot unit 6.1 is kept from 50°C aen 57°C
blowing air 1.3 through the vapor/liquid contact surface enhanced structure 1.1.1 in opposite direction of the fluid flow; circulating air in order to entrain solvent vapour from evaporating compartment 1.1 to condensing compartment 1.2 through the connected space between these 2 compartments; condensing solvent vapour on the surface of the indirect heat exchanger 1.2.1 ;
sucking of dry air into the circulation unit 1.3 order to supply air flow for the next circulation; collecting concentrated solution at the bottom of the evaporating compartment 1.1 and leading to the fluid circulation reservoir 2;
collecting 1.4 L concentrated Protease solution extract concentrate 9.2°Brix/3.1 U/mL through a valve on the side of fluid circulation reservoir 2 after 7 hours working; introducing inert gas to the fluid circulation reservoir 2 in order to minimize the effect of oxidation processes to achieve high quality of concentrated product;
The method and apparatus can also applied for other heat-sensitive solutions:
- Fruit juices: apple juice, water melone juice, coconut water, lychee juice, lime juice, nuoc tao, dragon fruit juice, guave juice,
- Green coffe bean extraction flruid
- Hibiscus flower extraction fluid
- Enzyme solution: Protease, Amylase
However, these examples are not intended to limit the invention. The scope of the invention is applicable to other heat-sensitive solutions not mentioned herein.
Apparatus of this invention can also be used for evaporation of heat-stable solutions

Claims

Claims
1. Apparatus for evaporation to concentrate heat-sensitive solutions at moderate temperature and ambient pressure comprises of:
working unit (1) is a closed chamber divided into two adjacent compartments, the evaporating (1.1) and the condensing compartment (1.2), which are separated by a baffle at lower position and connected to each other at the top position;
the evaporating compartment (1.1) consists of an underneath space which filled with the vapor/liquid contact surface enhanced structure (1.1.1), right above is a fluid irrigation unit (1.1.2), the upper space is free and connected with the condensing compartment (1.2);
the primary heat exchanger (1.1.1.1) is arranged within the vapor/liquid contact surface enhanced structure in order to implement first heating up of the feed;
the condensing compartment (1.2) consists of indirect heat exchangers (1.2.1) arranged parallel to each other to perform a condensation process whereby the thermal sensitive solution is traveling upward, and the heat transfer surface of the indirect heat exchangers (1.2.1) can be varied by increasing or decreasing the number of indirect heat exchangers (1.2.1);
a blower (1.3) is arranged between the condensing compartment (1.2) and the evaporating compartment (1.1) in order to ensure the air circulation within the working unit (1);
fluid circulation reservoir (2);
circulation pump (3);
secondary heat exchanger (4);
condensate collecting container (5);
heat pump connected with cooling (6.2) and heating loop (6.1);
switch cabinet (7) connected with measurement devices to monitor and control the operating parameters.
2. Apparatus according to claims (1), characterized in that the vapor/liquid contact surface enhanced structure ( 1.1.1 ) is selected from a group comprising random or structured packings with specific surface area ranges from 100 to 2500 m2/ m3.
3. Apparatus according to claims 1 and 2, characterized in that the vapor/liquid contact surface enhanced structure (1.1.1) is selected from a group comprising random or structured packings with specific surface area ranges from 300 to 2000 m2/m3.
4. Apparatus according to any one of claim 1 to 3, characterized in that the vapor/liquid contact surface enhanced structure (1.1.1) is selected from a group comprising random or structured packings with specific surface area ranges from 500 to 1600 m2/m3.
5. Apparatus according to any one of claim 1 to 4, characterized in that the vapor/liquid contact surface enhanced structure (1.1.1) is selected from a group comprising random or structured packings with specific surface area ranges from 600 to 1200 m2/m3.
6. Apparatus according to any one of claim 1 to 5, characterized in that the indirect heat exchanger (1.1.1.1) is selected from the group comprising of tube heat transfer exchanger or plate heat exchanger.
7. Apparatus according to any one of claim 1 to 6, characterized in that the first heating is implemented by primary heat exchanger (4) selected from the group comprising of tube heat transfer, plate heat transfer and pipe-in-pipe heat exchanger.
8. Apparatus according to any one of claim 1 to 7, characterized in that the indirect heat exchanger (1.2.1) is selected from the group comprising of plate heat exchangers with a heat transfer surface ranges from 100 to 1800 m2/m3.
9. Apparatus according to any one of claim 1 to 8, characterized in that the indirect heat exchanger (1.2.1) is selected from the group comprising of plate heat exchangers with a heat transfer surface ranges from 300 to 1400 m2/m3.
10. Apparatus according to any one of claim 1 to 9, characterized in that the indirect heat exchanger (1.2.1) is selected from the group comprising of plate heat exchangers with a heat transfer surface ranges from 500 to 1000 m /m .
11. Apparatus according to any one of claim 1 to 10, characterized in that the indirect heat exchangers (1.2.1) are arranged in parallel and form an angle of -15° to 60° from the vertical
12. Apparatus according to any one of claim 1 to 11, characterized in that the indirect heat exchangers (1.2.1) are arranged in parallel and form an angle of -5° to 45° from the vertical.
13. Apparatus according to any one of claim 1 to 12, characterized in that the indirect heat exchangers (1.2.1) are arranged in parallel and form an angle of 0° to 30° from the vertical.
14. Apparatus according to any one of claim 1 to 14, characterized in that the heat transfer surface can be varied by increasing or decreasing the number of indirect heat exchangers (1.2.1).
15. Apparatus according to any one of claim 1 to 15, characterized in that air circulation unit (1.3) is a fan or blower.
16. Apparatus according to any one of claim 1 to 16, characterized in that heat-sensitive solutions are selected from the group comprising of juices, vegetable juices, milk, liquid foods, fermentation broths, crude enzymes, herbal extracts, solvent extracts.
17. Apparatus according to any one of claim 1 to 17, characterized in that heat-sensitive solutions can be with or without fibres and pulp.
18. Apparatus according to any one of claim 1 to 18, characterized that this apparatus is multi- feed compatible, which can be used for processing of different feeds.
19. Apparatus according to any one of claim 1 to 19, characterized in that the switch cabinet (7).
20. Method for evaporation to concentrate heat-sensitive solutions at moderate temperature and ambient pressure uses the apparatus according to any claim 1 to 19 comprising steps:
leading feed into circulation reservoir (2);
pumping heat sensitive solutions with circulation pump (3) to the first heat exchanger (4); irrigating heat sensitive solutions on the vapor/liquid contact surface enhanced structure (1.1.1), fluids is then equally distributed within the above mentioned vapor/liquid contact surface, enhanced structure (1.1.1) in form of droplets and flow top down, the solution is simultaneously be heated up by the primary heat exchanger located within the vapor/liquid contact surface enhanced structure (1.1.1);
blowing air (1.3) through the vapor/liquid contact surface enhanced structure (1.1.1) in opposite direction of the fluid flow;
circulating air in order to entrain solvent vapour from evaporating compartment (1.1) to condensing compartment (1.2) through the connected space between these 2 compartments; condensing solvent vapour on the surface of the indirect heat exchanger (1.2.1);.
sucking of dry air into the circulation unit (1.3) order to supply air flow for the next circulation; collecting concentrated solution at the bottom of the evaporating compartment (1.1) and leading to the fluid circulation reservoir (2);
collecting concentrated products through a valve on the side of fluid circulation reservoir (2); introducing inert gas to the fluid circulation reservoir (2) in order to minimize the effect of oxidation processes to achieve high quality of concentrated product;
collecting condensed solvent at the bottom of the condensing compartment 1.2 and leading to the condensation reservoir (5).
21. The method according to claim 20 wherein temperature of the fluid contributed within the vapour/liquid contact surface enhanced structure (1.1.1) is kept within the rage from 20°C to 60°C.
22. The method according to claim 20 or 21 wherein temperature of the fluid contributed within the vapour/liquid contact surface enhanced structure (1.1.1) is kept within the rage from 25 °C to 55°C.
23. The method according to any one of claim 20 to 22 wherein temperature of the fluid contributed within the vapour/liquid contact surface enhanced structure (1.1.1) is kept within the rage from 35°C to 50°C.
24. The method according to any one of claim 20 to 23 wherein the loading of the vapour/liquid contact surface enhanced structure (1.1.1) is kept within the rage from 0.1 m3/m2h to 10 m3/m2h.
25. The method according to any one of claim 20 to 24 wherein the loading of the vapour/liquid contact surface enhanced structure (1.1.1) is kept within the rage from 0.5 m /m2h to 9 m3/m2h. .
26. The method according to any one of claim 20 to 25 wherein the loading of the vapour/liquid
3 2 3 2 contact surface enhanced structure (1.1.1) is kept within the rage from 1 m /m h to 7 m Im h.
27. The method according to any one of claim 20 to 26 wherein the primary (4) and secondary heat exchanger (1.1.1.1) use heat carrier, which is hot water from heating unit (6.1) of the heat pump (6).
28. The method according to any one of claim 20 to 27 wherein the indirect heat exchange (1.2.1) use heat carrier from cold unit (6.2) of the heat pump (6) is kept from the range from- 25 °C to +18°C.
29. The method according to any one of claim 20 to 28 wherein the indirect heat exchange (1.2.1) use heat carrier from cold unit (6.2) of the heat pump (6) is kept from the range from - 20 °C to +15°C.
30. The method according to any one of claim 20 to 29 wherein the heat pump (6) is used for taking the heat from the condensation to supply to the evaporation in order to maximize the heat usage efficiency.
31. The method according to any one of claim 20 to 30 wherein inert gas introduced into the fluid circulation reservoir (2) is selected from the group comprises of C02, N2 and its mixture.
32. The method according to any one of claim 20 to 31 wherein air is circulated in the space of the working unit between the evaporating compartment (1.1) and the condensing chamber (1.2) to maximize the retention of aromas and volatile compounds in the product.
PCT/VN2017/000011 2016-11-29 2017-11-24 Apparatus and method for evaporation to concentrate sensitive substances in solutions WO2018102835A1 (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113647457A (en) * 2021-08-17 2021-11-16 浙江百强乳业有限公司 Production process of paste condensed milk with improved solidification form

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2672473A1 (en) * 1991-02-08 1992-08-14 Durafroid Sa Method for improving the quality of grape juice with a view to using it to make wine, and device for implementing the said method
US5810975A (en) * 1992-02-12 1998-09-22 Sirven Apparatus for extracting solid residue from a fluid by evaporation
WO2012156923A1 (en) * 2011-05-17 2012-11-22 Microsphere System for concentrating industrial products and by-products

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2672473A1 (en) * 1991-02-08 1992-08-14 Durafroid Sa Method for improving the quality of grape juice with a view to using it to make wine, and device for implementing the said method
US5810975A (en) * 1992-02-12 1998-09-22 Sirven Apparatus for extracting solid residue from a fluid by evaporation
WO2012156923A1 (en) * 2011-05-17 2012-11-22 Microsphere System for concentrating industrial products and by-products

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113647457A (en) * 2021-08-17 2021-11-16 浙江百强乳业有限公司 Production process of paste condensed milk with improved solidification form

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