Improved process for producing a dietary corn fibre.

BACKGROUND OF THE INVENTION

Field of the Invention

This invention describes a method of ₅ processing a mixed fiber stream obtained by the wet corn milling process to make a product having a high total dietary fiber content.

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Description of the Presented Technique

In recent years, there has been an increasing awareness of the role fiber plays in the human diet. This is based not only on the role that fiber plays as a bulking agent but also on the role it is thought to play in preventing disease of the gastrointestinal system.

Dietary wheat fiber, wheat bran, has been consumed in breakfast cereals, all kinds of wheat bread, and similar products for many years. However, there is a recognized need for greater amounts of fiber to reinforce processed foods that are now consumed by a large part of the population. For these reasons, food suppliers have been looking for additional sources of dietary fiber.

A potential source of dietary fiord is corn fiord obtained as a by-product of wet corn milling. However, this product contains reasonably high percentages of starch and protein. Such additional components make the fiber less suitable for use in the cooking process or other food applications. This led workers to look for an economically and commercially acceptable process to reduce the amount of starch and protein while increasing the dietary fiber content of the fiber obtained.

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by the wet milling process of corn.

In US Patent No. 4,181,534, a process for treating the wet fiber stream obtained from the wet corn milling process is disclosed. According to said process, the fiber stream, while still in the wet state, is cooled by means of a whisk or impact of a millstone. The milled product is then separated into fractions with each fraction being an enriched fiber containing a high proportion of pentoses.

The process of enriching the fiber obtained from corn and soybeans is disclosed in US Patent No. 24,181,747. In this process, the crude fiber is heated with dilute aqueous acid to hydrolyze and dissolve undesirable by-products. The material is then extensively washed to obtain a fiber with a higher dietary fiber content.

US Patent No. 4,757,948 discloses a process for producing corn fibers with a high total dietary fiber content through a two stage process wherein the first utilizes a sieve and the second a rotating mill. The fiber fraction obtained according to this process is about eighty to eighty-five percent of the total dietary fiber.

While these prior processes may give an enriched fiber product, there is still a need for a simple low cost process to commercially produce a high dietary fiber content product from maize. A simple and economical process for enriching the dietary fiber content of corn fiber has now been discovered without the need for chemical hydrolysis or expensive milling. Through this process wet milling of corn can become a pro2

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high yield continuous process is a low value byproduct in a higher value food component. Moreover, with further refining processes, dietary fiber can be produced with a sulfur dioxide content (θθ2 ^^mu-it low.

SUMMARY OF THE INVENTION

According to this invention, there is provided a process for producing a corn fiber product having a high dietary fiber content characterized in that it comprises:

(a) diluting the raw fiber obtained from the wet milling process with water to obtain an aqueous raw corn fiber paste having a solids concentration of from about 2% to about 5% by weight.

(b) passing said aqueous raw corn fiber slurry through a hydrocyclone with the operating pressure of said hydrocyclone being adjusted to optimize fiber recovery in the high flow rate of the cyclone while carrying undesirable starch and protein components. coming out of the low flow current of the hydrocyclone, (c) passing said hydro cyclone outlet stream into a first centrifugal paddle screen having (1) screen openings that are sized to maximize the amount of starch and protein passing through the screen while maintaining a high yield and (2) and the gap (also called aperture) between the sieve and paddles that is selected to optimize fiber friction to remove starch and protein while maintaining a ren

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Reasonable misconduct;

(d) washing the solids separated by the first centrifugal blade screen; and (e) passing the washed solid to a second centrifugal paddle screen wherein the sieve openings and the space between the screen and paddles are optimized on the same basis as those used in the first centrifugal paddle screen.

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The washing phase may be conducted continuously or in batches. Heated water may optionally be used in the washing phase to facilitate SC2 removal. Wash water may also be treated to reduce SO2 content prior to washing, and / or followed by washing for recycling purposes. This treatment may be, for example, conducted with a steam separator to boil the wash water and thus remove the SC3.

When the product is removed from the second centrifugal paddle screen, an optional compression step may be used to remove water.

This step also reduces the SO2 content in the product.

DESCRIPTION OF PREFERRED EMBODIMENTS

In the wet milling process, the corn kernels are first softened by soaking them in water containing SO2. This is referred to as the maceration process. After maceration of the corn kernels, they are roughly ground with water to release the seed (the oil-containing portion of the grain). The seed is separated from the other solid components of the maize grain by passing the resulting paste through a hydrochloride.

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Mod. 71 - 20,000 ex. 90/08 clone. The low flow stream of the starch, protein and fiber containing hydrocyclone is then milled in an impact type mill followed by sieving to separate the blended raw fiber from the best starch and protein particles. This blended raw fiber is the starting material used in the process of this invention, a readily available raw material produced in large quantities by the wet milling industry. For a more detailed understanding of the industrial process of wet corn milling, see Starch Chemistry and Technology, Whistler and Paschall, Editors, Volume II, Chapter 1, p. 1-51, Academic Press, NY (1967).

In accordance with the present invention, the raw mixed fiber stream having a moisture content of about 80% to about 90% by weight is diluted with water to form a paste having a solids content of about 2% to about 5% by weight. The water used at this stage may be fresh water or recycled process water. This aqueous paste is then passed through a hydrocyclone.

Suitable hydrocyclones for use in the process of this invention are articles well known in the art. Hydrocyclones of various sizes and designs may be used as is clear to those skilled in the art. A particularly suitable hydrocyclone is one available from Dorr-Oliver Company, Stamford, Connecticut, which has a diameter of about 15.24 cm (6 inches) on the surface of its length of 91.44 cm. This hydrocyclone is described in detail in US Patent No. 2,913,112. It has been used for many years in the wet corn milling industry for the aqueous separation of corn seed, and its structure is described in detail in the chapter of Starch Chemistry and

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Techpology cited above. As can be seen from this article, hydrocyclone batteries can operate in parallel when large volumes of material are to be separated.

In the process of this invention, the pressure drop across the hydrocyclone is adjusted to maximize fiber recovery in the hydrocyclone high flow stream while causing undesirable starch and protein components to exit the hydrocyclone in the low flow stream. The pressure drop is preferably adjusted so that about 65% to about 75% of the volume of the aqueous slurry enters through the hydrocyclone outlets into the high flow rate of the hydrocyclone.

Under these preferred conditions, the pressure drop across the hydrocyclone is generally between about 0.56 to 0.9 kg / cm (8 to 12 psi). The low flow stream, which contains a higher concentration of starch and protein together with some fiber, returns to the wet corn milling process in which it is combined with the normal by-products of the process.

The high throughput stream of the hydrocyclone contains rough solid material that has a much higher dietary fiber content than the material passing through the low throughput stream of the hydrocyclone. This high throughput stream passes through a first centrifugal paddle sieve where the coarse solid material is further purified to give an intermediate having about 90% total dietary fiber on a dry substance basis.

Various centrifugal sieving apparatus capable of continuously separating solids and liquids may be used in the process of this invention. In general, such apparatuses comprise a cylindrical sieve, means for centrifugally giving the paste, and means for

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Mod. 71 - 20,000 ex. 90 (08) to remove separated solids from the sieve. In a large industrial process, commercially available centrifugal paddle sieves are most suitable for example vertical or horizontal rotary sieves.

Centrifugal paddle sieves are fitted with paddles (or tapping bars) which are affixed to a rotor. The blades rotate at a fixed distance from a sieve that is arranged circumferentially with respect to the rotor. The displayed distance is referred to as the space or opening between the blades and the sieve. Rotation of the blades causes material to enter the centrifugal blade screen to be thrown against the screen. Means (such as a paddle or blade at the inlet) are provided for moving material along the sieve from inlet to outlet.

When wet material, such as the high flow rate hydrocyclone stream in the present invention, enters a centrifugal paddle screen, the paddles throw the wet material against the screen. The water flows quickly. The paddles continue to throw the remaining material against the sieve as the material travels along the length of the sieve to exit.

In the present invention, the segregated liquid passing through the sieve contains fine fiber, amide and protein that have been separated from the coarser fiber. This is combined with the low flow current of the hydrocyclone and back to the wet corn milling process as noted above. The separated solid is a coarse fiber core containing about 65% to about 80% water.

The operation of the paddle screen is optimized by setting three parameters. One parameter refers to the sieve openings. If they are too small,

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you will get too much starch and protein with the coarse fiber core. If they are too large, too much fiber is lost to the separated liquid. Another parameter is the distance between the sieve and the blades. If it is too large, the material will not be sufficiently rubbed (rubbed) to separate starch and protein from the coarse fiber core. The centrifugal paddle sieve will perform essentially only a function of expelling water. If it is too small, the centrifugal paddle sieve will not work effectively. The third parameter is the blade sieve speed operation. The goal of optimizing the parameters is to minimize fiber loss while increasing friction to remove starch and protein from the fiber.

A preferred paddle screen for the process of the invention is the Indiana Canning Machine 77, which is a horizontal rotary screen obtained from the Indiana Canning Machine Company, Indianapolis, Indiana. The general use of such starch and fiber sorting machines is described in US Patent No. 3,813,298. For use at this stage of the present invention, it is placed in a sieve having apertures between about 2 mm and about 4 mm, preferably about 3 mm in diameter, and the space between the sieve and paddles is placed between about mm and about 15 mm, preferably between about mm and about 11 mm. Operating speeds may be from 500 to about 2,200 revolutions per minute (rpm), with speeds of about 500 to about 1500 rpm being preferred.

Coarse fiber core of the first paddle sieve is washed in two stages. In the first phase, it is preferable to use a wash station comprised of one or more tanks. The washing station can be operated continuously or in batch form,

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showing more efficient results with continuous operation. Washing in the tank or tanks removes released starch, gluten, smells, SO2 and other forms of fiber contamination.

In a preferred embodiment, water is added to the coarse fiber core for a first tank wash which is provided with a stirrer. Water is optionally heated to increase dissolution of SC3. The wet fiber exiting the first wash tank is then pumped into a second agitation wash tank. This tank is particularly useful for removing more S0₂.

Wash water may be treated to reduce SC&gt; 2 content prior to washing, and / or treatment may be conducted followed by washing if the washing water is to be recycled. If such treatment is desired, a vapor separator may be used to evaporate the S0₂·

The residence times in the tank or wash tanks are selected to optimize the removal of contaminants. For SO2, for example, the optimum residence time is the time required for the concentration of SO2 in the fiber to approximate approximately the concentration of SO2.₂ in the wash water. Displayed values ​​are selected to approximate the optimal dwell time. With the two tank wash system described above, the combination of fiber dwell time in the wash tanks is from about 5 to about 30 minutes, preferably from about 10 to about 20 minutes. It may take a longer amount of time, but it does not provide a significant improvement in results.

When using heated water, residence times may be shortened and removal

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SO2 is improved.

Water temperatures between about 46 ° C (150 ° F) and 65 ° C (210 ° F) can be used, with the most efficient temperatures above about

C (170 F). The preferred range is from about 52 ° C (170 ° F) to about 63 ° C (205 ° F). Temperatures below about 46 ° C (150 ° F) are ineffective in improving S0 removal.₂. Temperatures exceeding 63 ° C (20 ° F) may result in undesirable odors.

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I

The wet fiber exiting the second wash tank is pumped into a second centrifugal paddle sieve for the second wash stage. This phase removes most of the contaminants along with most of the wet fiber water.

The second centrifugal paddle screen is placed in the same manner as the first centrifugal paddle screen. The operation of this paddle screen is also optimized on the basis of the same criteria as the first centrifugal paddle screen. The preferred paddle screen at this stage of the process is also the Indiana Canning Machine No. 77. For use at this stage, it is fitted with a sieve having apertures between about 2 mm and about 4 mm, preferably about 3 mm in diameter, and the space between the sieve and paddles is placed between about mm and about 15 mm, and preferably between about mm and 11 mm. Operating speeds can be from about 500 to about 2200 rpm. Preferred operating speeds are between about 500 and 1500 rpm.

Separate liquid passing through the sieve can be combined with the low flow rate of the hydrocyclone and back to the wet corn milling process. The separated solid contains from 65 to 80% water and has a total content of 10%.

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Mod. 71 - 20,000 ex. -90/08 high dietary log. This material is then dried or optionally pressed followed by drying. Pressing the material removes water and consequently reduces the SC&gt; 2 content in the dried product.

Various commercial presses can be used to press the separate solid taken from the second centrifugal blade screen. Examples of suitable presses include screw presses and belt presses. One press that has been used in some experimental work of the present invention is the Bauer Heli press, twin screw press that is available from ABB Bauer, PO

Box 968, Springfield, Ohio 45501 USA Another press that can be used is the Vetter Dewatering screw press which is available from Dedert Corporation, Olympia Pield, Illinois USA. This is a single screw press. Both presses are capable of reducing the moisture content in the separated solid material to about 50 to 60% by weight.

The liquid separated from the press can be combined with the low flow rate of the hydrocyclone and back to the wet corn milling process as mentioned above. The solid material of the press is then dried. Material entering the dryer may be drawn from the safety outlet stream of the centrifugal blade screen or press. The drying process may be performed in various types of continuous or batch dryers which are articles well known in the art. Particularly suitable dryers for continuous operation include pneumatic conveyor dryers, jet dryers, rotary steam tube dryers and the like.

When a jet dryer is used, about 90 to about 95% of the material entering the jet dryer is recycled to give

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The average residence time is from about 3 to about 8 minutes and preferably from about 5 to about 6 minutes.

Dry material, which has a moisture content of about 2 to about 10% by weight, can be ground to any desired size depending on the purpose for which the product is used.

High total content dietary fiber product obtained by this process has a light color and a pleasant taste. It is suitable for use in a variety of food products. Thus, a continuous process has been developed which can be used for large scale production of a feed grade fiber having a high total dietary fiber content and which is prepared from a readily available starting material.

The following examples further illustrate the present invention and have enabled other persons skilled in the art to understand it more fully. It should be understood, however, that. The invention is not only limited to the examples given below. In the examples, all percentages given are based on weights unless otherwise indicated. Total dietary fiber values ​​were determined by the method of Prosky, et al, J. Assoe. Off. Anal. Chem., 67, 1044-1051 (1984). Represent material remaining after removal.

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of starch, protein, fat and ashes of a given sample

EXAMPLE 1

Separate portions of 10-20% solid fiber streams obtained during wet corn milling were used in the operations described in this example. The fiber stream was diluted with water to form a slurry with solids concentration of about 2.25 wt%. The diluted aqueous slurry of the raw corn fiber was then passed through a 15.24 cm (6 inch) diameter hydrocyclone (Dorr-Clone, Dorr-Oliver Company) at a delivery rate of about 190 liters per minute. . The pressure drop across the hydrocyclone was (8 psi) 0.56 kg / cm 2. The volume ratio of the high flow stream to the supply stream was 0.71. The high throughput stream was then blown through a centrifugal paddle screen (Indiana Canning Machine Company, model No. 77), adapted with a screen having openings with a diameter of 3.2 mm and a gap between the paddles and the screen. 9.5 mm. The machine was driven at a speed of 600 rpm. Dietary fiber that was released from the paddle sieve was washed, dried and analyzed. The results of two of the operations are given in Table 1. They demonstrate that when the raw fiber stream of the wet corn milling process is subjected to the process of this invention, the obtained dietary fiber fraction has a dietary fiber content greater than 90%.

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TABLE 1

Material

Initial

Production (% of

Original FDT)

FDT^The\ Starch (° / obs^to}) (% bs^s)

Fat Protein (% bs)^B) (° / o bs^D)

46,9 30,1 16,0

1,8

Product?

1st operation 6.5

91,4 4,8 5,1

1,8

Product 22operation 4.4

92,5 5,7 5,0

2,1

a) FDT = Total Dietary Fiber o) bs = dry basis

EXAMPLE 2

The general procedure of Example 1 was followed except that the water used for the dilution of the raw fiber was processed water from the wet corn milling process. In operations 3, 4 and 5 the space between the paddles and the screen in the paddle screen apparatus has been changed to show the influence of this space on product quality. In operations 6-11, the dietary fiber slurry washed in the first paddle sieve was passed to a second paddle sieve before the product was isolated. The results of these operations are given in Table II. Operations 3-5 demonstrate that the space between the blades and the sieve is reduced, and the percentage of total dietary fiber in the product increases. In operations 7-11, where they all use a space between the blades and the sieve similar to that of operation 4, they demonstrate that the passage of dietary fiber through a

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The second paddle sieve provides a product with somewhat high dietary fiber content than the process using the same conditions that include only one pass through the paddle sieve.

TABLE II

Dietary fiber

Production

<td></td><td>Operations</td><td>(% of FDT^dZoriginal</td><td>Total (% bs)^B)</td>

<td></td><td>₃c&gt;</td><td> —</td><td> 89,5</td>

<td></td><td> 4</td><td> 5,6</td><td> 91,1</td>

<td></td><td> 5^ç)</td><td> 4,7</td><td> 94,4</td>

<td></td><td> 6</td><td> —</td><td> 93,4^d)</td>

<td></td><td> 7</td><td> 4,0</td><td> 93,8</td>

<td></td><td> 8</td><td> 5,0</td><td> 93,1</td>

<td></td><td> 9</td><td> 7,0</td><td> 92,8</td>

<td></td><td> 10</td><td> 5,2</td><td> 92,2</td>

<td></td><td> 11</td><td> 7,8</td><td> 92,1</td>

<td>The)</td><td colspan="2">FDT - Total Dietary Fiber</td><td></td>

<td>B)</td><td>bs = base on</td><td>dry</td><td></td>

<td>ç)</td><td>In operations</td><td>3 and 5, the space between</td><td>the shovels and</td>

was respectively 13 mm and 6.4 mm. In all other operations, the space was 9.5 mm.

(d) the average of five washes per batch. Operations 7-11 were continuously washed in a second paddle sieve.

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I

EXAMPLE 3

The raw corn fiber stream as in Example 1 was diluted with water to provide a slurry with a solids concentration of about 2 wt%. The dilute aqueous slurry of crude corn fiber was then passed through the hydrocyclone as in Example 1. In the various operations, the pressure drop across the hydrocyclone was between 0.7 and 0.9kg / cm.

The volume ratio of the high throughput stream to the supply stream was about 0.65. The results of four operations are given in Table III.

TABLE III

Production (% of FDT^The^

Original operations

Total Dietary Fiber (% b _s^B) )

<td> 12</td><td> 6,5</td><td> 85,6</td>

<td> 13</td><td> 9/4</td><td> 81,7</td>

<td> 14</td><td> 6,6</td><td> 84,1</td>

<td> 15</td><td> 3,6</td><td> 84,3</td>

a) FDT = Total Dietary Fiber

b) bs = dry base

EXAMPLE 4

This example summarizes various operations to provide information of the results obtained in a parameter range. The general procedure of the Example was followed to obtain a coarse fiber core from the first centrifugal blade screen.

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Mod. 71 - 20,000 ex. - 90/08 Coarse fiber core having 70% humidity was taken from the outlet stream of the first centrifugal paddle sieve and dropped by gravity through a 8 inch x 2.54 cm = 8.32 cm tube = = 20.32 cm) for a 380 l stirring tank (100 gallons x 3.81 = 380 l). 3.81 (1 gallon) to 11.41 (3 gallons) per minute was added by a jet of water to the paddle screen discharge to prevent a build up of the product in the barrel. The fiber in this phase is past the basic separation phase, and is ready for washing to remove any loose starch, gluten, flavors, SO2, and any other forms of contamination that are typically associated with material that is normally present. destined to become food. This fiber has about 250 to about 450 parts per million (ppm)

SOg based on total weight including water.

The 380 l (100 gallon) tank was used as a collection vessel for fiber, fresh water and recycled water from the filtered stream of the second centrifugal paddle sieve. The concentration of dry substance in the tank was about (0.5 to 1.5 ounces (31.0g&gt;) 15.55g to 46.65g per (gallon) 3.8 1. The use of recycled water allowed a larger volume of water to be pumped out of the tank while keeping the amount of fresh water used in the process low. In fact, water was pumped around the washing station about three times the proportion of fresh water use, which was measured at the inlet and outlet of this station.

About 7 gallons (20 gallons) per minute of fresh water was measured in the wash tank. The fresh water was heated with a hydro heater to about 84 ° (184 ° f) by direct contact with steam. The tank temperature of 380 l (100 gallons) was about 79 ° (175 ° F).

I

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The hot fiber from this tank was pumped at 228 l (60 gallons) / minute into a second 300 gallon (304 l) agitation tank. This tank was used to increase the average time the fiber was in contact with the wash water, further reducing the SO content.₂· Between the two tanks, the average residence time was 14 minutes. The contents of the second tank were pumped at 228 l (6th gallons) / minute into the second centrifugal paddle sieve.

The second centrifugal paddle sieve was fitted with a sieve having openings of 3 mm in diameter and with a gap of 9 mm between the paddles and the sieve. The machine was set at a speed of 1100 rpm to improve the expulsion of water.

The filtration of the second centrifugal paddle sieve was divided between the 380 l (100 gallon) wash tank recycle loop and an outlet stream equivalent to the amount of fresh water entering the 380 l (100 gallon) tank. This salt stream was either sent to the crude mixed fiber stream dilution tank or combined with the low flow rate of the hydrocyclone and back to the wet corn milling process.

The fiber exiting the second centrifugal shovel sieve circulated at an average of about 3628.72 g and 5443.08 g / min (8-12 lbs / m) at 70 or 75% humidity. The total dietary fiber was about 92 to 94% dry basis, and the concentration of SO₂ It was about 20 to 50 parts per million based on total weight, including water. From here the fiber was wetted with 3.8 l to 11.4 l / min (1 to 3 gallons / min) of cold fresh water over a 3048 cm (100 ft) pipe for a Bauer Heli press. twin screw.

The press was used to reduce

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the moisture content of the fiber to about 52% to 54%. About half of the water remaining in the fiber taken from the second centrifugal paddle sieve, together with about half of the remaining SOg. some of the starch that also remained was removed by filtration. This resulted in the removal of about half of the total SO 2 that remained in the wet fiber after washing.

The SO2 concentration in the fiber when leaving the press was about 20 to 50 parts per million based on total weight, including water.

The press fiber was dried in a pneumatic conveying drier at an air outlet temperature (lamp drier) of about 126 ° (260 ° P) to a residence time of about 5 to about 6 minutes. A dry fiber having a moisture content of about 5% was supplied to an Asima Bauermeister mill (available from Bauermeister, 4127 Willow Lake Boulevard Memphis, Tennessee 38118 USA), which grinds the fiber to about 100 Mesh (Mesh ns de openings by 2.54 cm by length -Mesh 100 x 2.54 cm = 254 cm). From here the fiber was bagged and reeded.

It should be noted that other types of grinding equipment may be used in accordance with the invention. For example, the Prater Model CLM 100 mill or other Prater products may be used such as Aerosplit Rema or MAC 3 (which are friction mills with air classifiers). These are available by Prater at 1515 South 55th Court, Chicago, Illinois 60650 USA

EXAMPLE 5

Like Example 4, this example summarizes various operations under various test conditions.

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MAL1S / I

The results are summarized in Tables IV-VI.

The general procedure of Example 1 was followed to produce coarse shell fiber.

Table IV provides a comparison of dietary fiber made according to Example 1 and dietary fiber made according to a modified process of Example 4. In the modified process of Example 4, all process steps and conditions were followed except fresh water which was not heated with a hydro heater, the second 3040 1 (800 gallon) tank was not used, and the Bauer press was not used. 0 380 l (100 gallon) wash tank residence time averaged about 2 minutes. In the Table, the term bs and PDT means “% dry and fiber base

<td>Total Dietary ”</td><td> •</td>

<td>Operations N2</td><td>table IV Modification of Example 1 Example 4 % dry basis% dry basis dietary fiber dietary fiber total (a) total (b)</td>

<td> 1</td><td> 89,9</td>

<td> 2</td><td> 90,5</td>

<td> 3</td><td> 90,9</td>

<td> 4</td><td> 93,1</td>

<td> 5</td><td> 92,4</td>

<td> 6</td><td> 94,1</td>

(a) Laboratory wash to remove any loose starch and / or protein

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(b) Dried, but not ground.

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J

The fiber from all operations was dried in a pneumatic conveying dryer with a moisture content of about 3 to about 5%. the fiber was ground to 100 mesh (mesh ns of openings per linear inch - per 2.54 cm by length - 100 x 2.54 cm = 254 cm). When the milled product was measured for total dietary fiber content, it was found that such content had been reduced to about 1 to 2%.

Table V illustrates the effects of certain process conditions on SOg content. The procedure of Example 4 was followed except fresh water which was not heated in steps 1-3. In operations 4-7 the hydro-heater was used to heat fresh water and a heated steam jacket was provided around the 3040 1 (800 gallon) wash tank. The combined average residence time in the two storage tanks was Washing was about 14 minutes. All SO2 measurements in parts per million are based on total weight, including water. The temperatures indicated for operations 4-7 refer to the wash tank water temperature of 3040 l (800 gallons). In operation 6, the sample was taken two hours after the temperature reading. The wash water ratio for all samples was about 38 1 (10 gallons) of water per pound of dry substance (ss), or about 76 1 (20 gallons) / per minute.

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63.489

Case 3392-A

<img file="PT97564B_D0018.tif" />

Table VI shows the effects of the pressing phase on the content of S0.₂. The process of Example 4 was followed. The press was not used in operations 1-3, but a twin thread Bauer press was used in operations 4-5. The 3040 L (800 gallon) wash water temperature in the tank was maintained at about 82 ° C (180 ° F).

TABLE VI

Operation

Fiber of the second centrifugal paddle sieve

Fiber pressed parts per million S0₂(52% humidity)

P ro du to ac ac ed parts per million S0₂ (3.5% humidity)

<td> 1</td><td colspan="2"> 35</td><td> 70</td>

<td> 2(1)</td><td> 22</td><td></td><td> 52</td>

<td> 3(1)</td><td> 21</td><td></td><td> 48</td>

<td> 4</td><td> 25</td><td> 25</td><td> 35</td>

<td> 5(1)</td><td> 25</td><td> 15</td><td> 35</td>

(1) The wash tanks operated in batch form.

They were operated continuously in operations 1 and 4.

After two or more weeks of storage of the finished product, the content of S0₂ was measured again. It was found that there was a 50-66% reduction in SO concentration.₂. The reduction is particularly apparent in the product produced using wash water at a temperature of about 87 ° (190 ° F) - 93 ° (200 ° F) in the 30401 (800 gallon) tank.

So it is apparent that it was provided,

63.489

Case 3392-A

<img file="PT97564B_D0019.tif" />

According to the invention, a process for producing a high total content dietary corn fiber that fully meets the purposes and benefits we have set ourselves. While the invention has been described in conjunction with specific embodiments, it is apparent that many alternatives - modifications - and variations will be apparent to those skilled in the art in light of the above knowledge. Accordingly, it is intended to include all such alternatives - modifications - and variations as mentioned within the spirit and extent of the appended claims.