JPS582397A - Oil and fat horizontal crystallizer - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a horizontal crystallizer for fats and oils, and particularly to a horizontal crystallizer for fats and oils that can be operated continuously.

Generally, when the purpose is to obtain crystal components in fats and oils as pure, giant-grown crystals by cooling, it is essential to make the temperature distribution within the cooling system uniform or to make the fluctuations in the distribution extremely small. It is a condition. It is clear that by complying with these conditions, a crystal component of good quality, pure growth, and having good p characteristics can be obtained.

However, in the short-time rapid cooling method based on the conventional crystallization method such as jacket cooling or shaft cooling with a protruding cooling surface, the temperature difference ΔT between the outer circumference of the cooling wall and the center of the shaft becomes unnecessarily large. It is difficult to obtain high-quality crystals because phenomena such as fine crystal seed crystal components crystallized on the cooling surface wall may be redissolved during the moving growth process, crystal parts may be distorted, or twin crystals may occur. I can't.

In addition, in order to minimize the distribution temperature difference ΔT in the cooling system, it is often necessary to perform forced stirring using an external device, but if forced stirring is performed more than necessary, the liquid layer will be disturbed and the liquid cross section will be The shearing force exerted by the blade edges causes crystal fragmentation, which also makes it difficult to obtain desired crystals.

Therefore, in order to achieve uniform cooling with less temperature distribution and obtain good crystals, it is common practice to use a refrigerant with a small temperature difference with the system to be cooled, or to carry out gradual long-term cooling with a small temperature gradient. ＼ Gradual cooling has a slow heat transfer, and it takes about 8 hours to complete cooling.
This method is preferable because it takes a long time, up to 12 hours, and as shown in Fig. 7, the heat of crystallization generated during crystallization is maximized, causing the entire cooling system to rise by as much as 2 to 4 degrees Celsius. I can't seem to get any crystals.

On the other hand, a horizontal crystallizer has been proposed which has a cooling surface in the form of a concentric coil fixed to a shaft, in which a refrigerant is passed through the coil and the cooling surface rotates together with the shaft (Japanese Patent Publication No. 55-5
0442, Japanese Patent Publication No. 5F5-3081), these conventionally known cooling surfaces with one stage of concentric circles have a larger effective cooling area for the object to be cooled than the conventional wall cooling method. Therefore, the action of removing crystal heat cannot be said to be effective for the purpose of rapid cooling either.

The object of the present invention is to provide horizontal crystallization of fats and oils, which can quickly cool the object to be cooled in a system with a small temperature difference ΔT between the outer circumference and the inner circumference, and obtain crystalline components with good properties and quality. The goal is to provide equipment.

The present inventors have found that crystals with good properties and quality can be obtained by performing crystallization while efficiently removing the crystal heat generated during crystal growth, and based on this knowledge, As a result of investigating various crystallizers that perform rapid cooling for a short time at a uniform temperature of 1°C or less on the cross section of the body fluid to be cooled, we found that a refrigerant with a large temperature difference flows in a spiral shape from the outer periphery and In order to achieve rapid cooling, we invented a crystallizer with a large heat transfer property in which the cooling surface can be rotated around a rotating shaft.

That is, the crystallizer of the present invention has a plurality of cooling coil bundles formed by spirally winding cooling coil tubes around a rotational axis in a crystallization tank, so that the surfaces of the cooling coils are not tilted or tilted relative to the rotational axis. Rotating shafts are rotatably mounted at a predetermined pitch so as to be orthogonal to each other, and refrigerant can be continuously supplied into the cooling coil tubes from the outer periphery to the inner periphery of each of the cooling coil bundles. The apparatus is characterized in that it cools the object to be cooled supplied into the crystallization tank.

Embodiments of the crystallizer of the present invention shown in the drawings will be described below.

FIG. 1 is a cross-sectional view of an embodiment of the crystallization apparatus of the present invention. In the drawing, 1 is a horizontal cylindrical crystallization tank, with a raw material micellar supply port 2 at one end of the upper part and a crystallized slurry at the other end of the lower part. It has a discharge port 3.

Reference numeral 4 denotes a rotating shaft provided at the axial center of the crystallization tank 1, and is supported via a sealing packing 11. In addition, the rotating shaft 4
is a pline supply outer pipe 5 having a refrigerant pline inlet 5'.
and a return pline collecting inner pipe 6 having a return pline outlet 6', and a refrigerant pline inlet 5.
' and the return sibling line outlet 6' are connected to the crystallization tank 1, respectively.
They are located on the right lateral part and the left lateral part of. 7.7.7
．． . . . are branch pipes provided on the rotating shaft 4 in communication with the pline supply outer pipe 5, and are provided perpendicularly to the rotating shaft 4 at appropriate intervals. 8.8.8. ... is the branch pipe 7.7.7 above.
．． . . . and a cooling coil bundle communicated with the brine collection inner pipe 6, the cooling coil pipe 8' is centered around the rotation axis 4,
It is formed by winding it in a spiral shape in the direction perpendicular to the rotating shaft 4, and the pitch is 80 to 3.
The outer end of the cooling coil pipe 8' is connected to the other end of the branch pipe 7, and the inner end of the cooling coil pipe 8' is connected to the other end of the branch pipe 7. The return pline is connected to the collecting inner pipe 6. In addition,
In the figure, 9 and 10 are temperature indicators attached to the crystallization tank 1, and 12
is the inner diameter of the rotating shaft, 13 is the outer diameter of the cooling coil bundle, 14 is the outer diameter of the crystallization tank, and 14' is the length of the crystallization tank.

Further, as shown in FIG. 2, the device of the present invention achieves cooling by installing an impeller-shaped paddle R15 along the surface of the cooling coil bundle 8 as an auxiliary means to assist in efficient heat transfer by the cooling coil bundle 8. This can be done even more efficiently.

The width of the paddle blade 15 is determined simply by the width of the cooling coil pipe 8.
It is sufficient that the gap ζζ is such that the liquid flows as shown by the arrow in FIG. The Koapado blade 15 also has the effect of gently lifting up only fine particles that have not yet grown into crystals, without lifting up the crystals that have grown, thereby enabling rapid cooling in the cooled system with even smaller temperature distribution. It is something that makes you familiar.

Furthermore, as shown in FIG.
By attaching this, it is possible to prevent crystals from adhering to the cooling coil tube 8'. That is, as shown in FIG. 3, the scraper 16 has a large number of scraper brushes 16' of appropriate length on the surface facing the cooling coil bundle 8, and is not fixed to the rotating shaft 4 (however, , there is no groove etc. to prevent it from moving in the axial direction) The scraper is attached using ring 17.
Therefore, it is provided without interlocking with the rotation of the rotating shaft 4. Incidentally, it is also possible to fix the scraper 16 to the inner wall of the crystallization tank 1.

Next, the function and effect of the apparatus of the present invention will be explained. In order to crystallize oils and fats using the apparatus of the present invention, firstly, raw material micella (oils and fats) is introduced into the crystallization tank 1 from the raw material micellar machine □' inlet 2. The refrigerant pline inlet 5
Inject the refrigerant pline from ’. Thus, the refrigerant injected from the refrigerant pline inlet 5' passes through the pline supply outer pipe 5, which is the outer pipe of the rotating shaft 4, and into the branch pipes 7.7.7, as shown by the arrow in FIG. ．． The cooling coil tube 8L is guided to the outermost periphery of the cooling coil bundle 8,8゜8,... through...
, $/, g/, ..., and at this time exchanges heat with the raw material miscella supplied from the supply port 2, and is then collected in the return pline collection inner pipe 6, which is the inner pipe of the rotating shaft 4. , is discharged from the return pline outlet 6', while the supply port 2
The raw material miscella supplied from the cooling coil bundle 8.8.8
．． It is crystallized by contacting the refrigerant line through...
The crystallized slurry is continuously taken out from the crystallized slurry outlet 3.

At this time, the cooling coil bundle 8.8.8. is formed into a spiral shape with a dense pitch by the rotation of the rotating shaft 4. . . . rotates, and the peripheral speed is faster at the outer peripheral portion farther from the rotating shaft 4, and the heat transfer becomes smoother accordingly, so that a more efficient cooling effect can be achieved.

The device of the present invention has a cooling surface that is 1.5 to 3.0 times larger than that of conventional wall cooling devices, and the outermost circumference 1 of the cooling coil tube 8' and the supplied refrigerant rotate in a spiral shape. At this time, heat is efficiently transferred in a radial manner from the gap between the cooling coil tubes 8', and furthermore, since the cooling coil bundle 8 itself rotates in conjunction with the rotating shaft 4, it moves in the axial direction. heat transfer is promoted. By improving heat transfer, the apparatus of the present invention enables rapid cooling, has a remarkable effect of removing heat generated by crystalline components, and enables cooling with a more uniform temperature distribution.

In addition, the device of the present invention promotes forced liquid flow (indicated by arrows in FIG. 5) between the cooling coil tubes 8' by attaching an impeller-shaped paddle 15 that also serves as a support for the cooling coil bundle 8. In addition, the scraper mechanism can be easily installed, and when the scraper 16 is installed, there is no need to worry about scaling, and it is possible to maintain a constant heat transfer ability even during long-term operation, making it extremely industrial and more practical. It can be said to be a typical crystallizer.

Therefore, the device of the present invention enables cooling of the refrigerant with a larger temperature difference, and achieves extremely large economical effects, such as being able to perform cooling in a short time of 1/2 to 115 times that of conventional devices.

The oils and fats to be crystallized in the crystallizer of the present invention include raw materials with a high crystal content from which cacao substitutes can be obtained, such as crude oils such as monkey fat, kokum butter, and shea butter, degummed oils, deoxidized oils, and Refining processes such as bleaching and deodorized oils can be used, and animal and vegetable oils and fats used for the purpose of removing high melting point components such as stearin, such as crude oil such as palm oil, cottonseed oil, rice bran oil, beef tallow, lard, and degumming. Oils, refining processes such as deacidification or bleaching, and deodorized oils can be used. Oils and fats other than these, such as corn oil, rapeseed oil, safflower oil,
Sunflower oil, soybean oil, hydrogenated products of these animal and vegetable oils, mixed fats and oils thereof, fractionated oils obtained by fractionating the above animal and vegetable fats, and hydrogenated products thereof, etc. are also used in the present invention. I can do it. Also, transesterified products of the same or different types of animal and vegetable oils and fats can also be used as raw materials.

The apparatus of the present invention (the crystallization of the above-mentioned fats and oils is carried out using a single oil or a mixing system in which the oil and fat are diluted and blended in 0.1 to 9 times the amount of a solvent such as hexane or acetone). Clarify the effectiveness of the device in detail.

Experimental Example 1 Using a bench scale crystallizer of the present invention as described below, batch cooling crystallization of intermediate melting point components was carried out for the second stage crystallization fractionation of three divisions of monkey fat with a high content of crystalline components. Ta.

[Crystallizer]

Sal fat 1 heated to 60°C was added to the crystallization tank of the apparatus of the present invention.
9s of mixed miscella (mixture of oil and solvent) at 40°C prepared at a ratio of 3 parts (by weight) to 3 parts (by weight) of solvent hexane
oz to make it full.

The rotation of the cooling coil bundle is 15 r, the charging temperature of the p-m% mixed micella is 40°C, the crystallization end temperature is -6°C, the temperature at the refrigerant brine inlet is -12°C, the temperature at the outlet of the refrigerant pline is -3°C, Refrigerant pline flow rate 30001/
Crystallization was performed with Hr. 45 minutes after the start of cooling, when the average temperature of the micella is θ°C, the temperatures at the center of the shaft and at the outer circumference are 0.2°C and -0.1°C, respectively, and the liquid temperature distribution difference J
It was possible to obtain a uniform micellar state at T = 0.3°C or lower.

When the micella was cooled to a final temperature of -6°C under the temperature distribution described above, the cooling time was 1.5 hours, as shown in Figure 6, and the crystallization was completed in 1.5 hours. The maximum temperature value of is also suppressed to below 1℃, and the obtained crystal components have a particle size of 200 to 400μ (microns), and although the particle size is slightly small, the particle size is pure and uniform, and the crystals are tight, so f It had good over-separability and was of extremely excellent quality and properties.

Table 1 shows the properties and filtration separation performance of the fractionated monkey fat medium melting point crystal component and liquid oil obtained by the apparatus of the present invention.

Table 1 Filtration time (seconds) (The same applies to Tables 2 to 4) Comparative Experiment Example A crystallization tank with the same dimensions as Experiment 1 was used, the stirring blade was changed to a paddle-shaped 4-blade, and the tank was Crystallization was performed by wall cooling with a jacket provided on the wall. The conditions were the same as in Experimental Example 1, such as the blending ratio of miscella (raw oil and solvent), charging temperature, and number of stirrings, and the temperature at the refrigerant pline inlet was -12°C, and the refrigerant pline flow rate was 30001/Hr. At this time, the temperature at the outlet of the refrigerant pline was -6°C. When the average temperature of the micella in the system is 0°C, the temperatures at the center and outer circumference of the shaft are 0.9°C1-07°C, respectively, and the liquid temperature distribution difference ΔT
It showed a rather large temperature distribution value of =1.6℃.

When the micella was cooled to a final temperature of -6°C under the above-mentioned temperature distribution, the cooling time was 6.5°C as shown in Figure 7.
It took 5 hours, and the maximum temperature due to the heat of crystallization of the micellar state rose to 2.5°C.

Table 2 shows the fractionated crystal components obtained by the wall cooling crystallization method according to the prior art, the properties of the liquid oil, and the r-overseparation performance.

Table 2 Experimental Example 2 In addition to the same equipment as Experimental Example 1, each cooling coil bundle was
Using a crystallizer equipped with 5 paddle blades as shown in FIG. 4, the second stage batch crystallization of monkey fat was divided into three parts. Rotation of cooling coil bundle 15r, p, m, 1 part (weight) of sal fat heated to 60°C and 3 parts (weight) of solvent hexane Mixed micellar preparation temperature 40°C 1 Product analysis end temperature -6
The crystallization was carried out at a temperature of -12° C. at the inlet of the refrigerant pline, a temperature of -2.5° C. at the outlet of the refrigerant pline, and a flow rate of 30001/Hr through the refrigerant pline. When the average temperature of the micella is 0°C 40 minutes after the start of cooling, the temperatures at the center of the shaft and at the outer circumference are 0.1°C and -0 part 1°C, respectively, and the liquid temperature distribution difference ΔT = 0. It was possible to obtain a uniform micellar state at 2°C.

When the micella was cooled to a final temperature of -6°C under the temperature distribution described above, crystallization was completed in 1.2 hours, and the maximum temperature of the micellar state due to the heat of crystallization was 1.
℃ or less, the obtained crystals have good purity and a particle size of 20
Uniform particle size from 0 to 300μ (microns), quality,
It was excellent in both properties and separation properties.

Table 3 shows the properties of the fractionated monkey fat medium melting point crystal component and liquid oil obtained by the apparatus of the present invention equipped with paddle blades, and the values of the sludge separation performance.

Table 3 Experimental Example 3 Using the same crystallizer as the apparatus used in Experimental Example 1, batch cooling crystallization was performed for the second stage continuous crystallization fractionation of palm oil divided into three parts.

Palm bleaching crude oil heated to 60°C was prepared at a ratio of 1 part (by weight) to 2.0 parts (by weight) of solvent hexane at 40°C.
The mixed miscella was continuously supplied from the supply port at the top of one side of the crystallization tank at a supply rate of 6601/Hr, and the temperature at the inlet of the refrigerant line was -12°C at a rotation rate of 15 r-pm% of the cooling coil bundle. The rate of slurry pipe 660//Hr at a temperature of -6°C where rapid cooling was performed at a temperature of -8°C at the outlet of the refrigerant pline and a flow rate of 3000 J/Hr, and crystallization was completed from the outlet at the bottom on the opposite side of the crystallization tank. It was continuously discharged. The temperatures of the micella at the outer periphery and near the axis in the crystallization tank are -1.4°C and -2.0°C, respectively, and a liquid temperature distribution difference ΔT = 0.6°C shows a uniform temperature distribution cross section. was.

As described above, the crystalline components obtained by continuous cooling to a final temperature of -6°C in a uniform temperature distribution zone can be cooled by rapid thermal transfer using the apparatus of the present invention, so that there is no temperature maximum due to heat of crystallization and the crystals are not sticky. As a result, the crystals are compact, pure, uniform in particle size, extremely easy to separate, and of high quality.
It had excellent properties.

Table 4 shows the quality and properties of the fractionated crystal components and liquid oil obtained by the apparatus of the present invention, as well as the f over-separation performance of the slurry obtained by continuous crystallization, and the apparatus used in the comparative experimental examples, regardless of the apparatus of the present invention. Using the same equipment as wall cooling, paddle type 4 blades), the flow rate of the refrigerant pline was halved (1i500A'/
The quality characteristics of the crystal components and liquid oil obtained in each case and the values of f-overseparation performance are shown.

Table-4

[Brief explanation of the drawing]

FIG. 1 is a longitudinal cross-sectional view showing one embodiment of the present invention, FIG. 2 is a longitudinal cross-sectional view showing another embodiment of the present invention with paddle blades attached, and FIG. A partial longitudinal sectional view showing the state in which the scraper is attached to the invented device, Figure 4 is A of Figure 2.
-A' line cross-sectional view Figure 5 is a model diagram of liquid flow by attaching a paddle blade, Figure 6 is a diagram showing the required rapid cooling time and crystal heat removal effect according to the present invention, and Figure 7 is a diagram according to the conventional method. FIG. 3 is a diagram showing the required cooling time and the maximum of crystal heat. 1... Crystallization tank, 2... Raw material micella supply port, 3...
Crystallization completed slurry discharge port, 4...rotating shaft, 5...pline supply outer pipe, 5'...refrigerant pline inlet, 6...
・Return pline collection inner pipe, 6'...Return pline fn outlet, 7...Branch pipe, 8...Cooling coil bundle, 8'...
・Cooling coil tube, 9, 10...Temperature indicator, 11...
・Packskin for sealing, 12... Inner diameter of rotating shaft, 13.
... Outer diameter of the cooling coil bundle, 14... Outer diameter of the crystallization tank, 1
4'... Length of crystallization tank, 15... Paddle blade, 16
Scraper, 16'...Scraper brush, 1
7...Scraper mounting is by ring, D...shaft mounting is by pitch Patent applicant Asahi Denka Kogyo Co., Ltd. Procedures Amendment Document November 27, 1981 1, Incident indication patent application No. 102109/1982 2, Name of the invention: Horizontal crystallizer for oils and fats 3. Relationship with the person making the amendment: Patent applicant (038) Asahi Denka Kogyo Co., Ltd. 4, agent's voluntary amendment (amendment made within 1 year and 3 months from the filing of the patent application) 6 ,
Claims column and Detailed Description of the Invention column of the specification to be amended. 7. Contents of the amendment (1) Amendment of the scope of claims as attached. (2) On page m8, line 11, "Sama ni nashi de deru" was corrected to "sama ni shishida deru." (3) “Oils and fats” in the bottom two lines of page 8 have been corrected to “mixtures of oils and fats and solvents.” (4) Delete 10 lines of “Batch” from the bottom of page 17. (5) On page 18, lines 1 and 2, "inside the crystallization tank" was corrected to "in the center of the crystallization tank." (6) In lines 4-3 from the bottom of page 18, "Refrigerant brine flow rate is halved (1500l/Hr) J" is corrected to "Raw material miscella flow rate is halved (33G, //Hr) J." Above 2, patent Claims (1) A plurality of cooling coil bundles formed by spirally winding cooling coil tubes around a rotational axis in a crystallization tank, all of whose surfaces are perpendicular to the rotational axis. Equipped with rotatable shafts mounted at a predetermined pitch,
A refrigerant can be continuously supplied into the cooling coil tubes from the outer periphery to the inner periphery of each of the cooling coil bundles, thereby cooling the object to be cooled supplied into the crystallization tank. A horizontal crystallizer for oils and fats. (2) Impeller-shaped paddle blades are attached to the rotating shaft along the surface of the cooling coil bundle to increase the liquid flow of the object to be cooled in the gap between the east of the cooling coils. ) Horizontal crystallizer for oils and fats as described in item ). (3) A scraper that does not operate in conjunction with the rotation of the rotating shaft is provided along the surface of the cooling coil bundle to continuously remove scale from the surface of the cooling coil tube. The horizontal crystallizer for oils and fats according to item (2) or item (2). (4) The horizontal crystallizer for fats and oils according to claim (1), wherein the pitch is between 801 nM and 300 nM. (5) A supply port is provided at the top of one side of the crystallization tank, and a discharge port is provided at the bottom of the opposite side of the crystallization tank, and the object to be cooled is continuously supplied through the supply port, and crystallization is completed through the discharge port. A horizontal crystallizer for fats and oils according to any one of claims (1) to (3), wherein the slurry is continuously taken out.

Claims (5)

[Claims] (1) A plurality of cooling coil bundles formed by spirally winding cooling coil tubes around the rotation axis are placed in a crystallization tank with their surfaces perpendicular to the rotation axis t. Rotating shafts mounted at pitches are rotatably provided, and the cooling coil bundles are provided with a shaft extending from the outer circumference to the inner circumference of each of the cooling coil bundles (so that refrigerant can be continuously supplied thereto). A horizontal crystallizer for fats and oils, characterized in that the object to be cooled supplied to the crystallizer tank is cooled. (2) impeller-shaped paddle blades are attached to the rotating shaft along the surface of the cooling coil bundle, and arranged to increase the liquid flow of the object to be cooled in one gap between the cooling coil bundles;
A horizontal crystallizer for fats and oils according to claim (1'). (3) A scraper that does not operate in conjunction with the rotation of the rotating shaft is provided along the surface of the cooling coil bundle to continuously remove scale from the surface of the cooling coil tube. The horizontal crystallizer for fats and oils according to item 1 or item (2). (4) The horizontal crystallizer for fats and oils according to claim 1, wherein the pitch is from 80 mm to 300 mm. (5) A supply port is provided at the top of one side of the crystallization tank, and a discharge port is provided at the bottom of the opposite side of the crystallization tank, and the object to be cooled is continuously supplied from the second supply port, and the crystallized slurry is made from the above discharge port. A horizontal crystallizer for fats and oils according to any one of claims (1) to (3), which is configured to continuously take out oil and fat.