COOKIE PRODUCTION WITH EXTRUSION HEAT TREATMENT AND POST EXTRUSION MIXING AND BAKING

Abstract: The present invention relates to the production of cookies which exhibit a cookie crumb-like structure and structural integrity using a cooker extruder to mix and heat ingredients comprising flour and oil to promote browning and flavor development. The heat treated mass produced in the cooker extruder is admixed with ingredients comprising water in a post extrusion mixer. The dough-like mixture produced in the post extrusion mixer is leavened and further browned using post-extrusion baking, such as microwave, dielectric radio frequency, infrared, conductive, or convection baking, frying, or a combination thereof. The shortening or fat content of the dough-like mixture may be from about 12 % by weight to about 40 % by weight, preferably from about 20 % by weight to about30 % by weight, based upon the weight of the dough-like mixture. Separation of oil from the remaining mass and extruder surging and starch gelatinization are avoided preferably by admixing water into heat-treated ingredients comprising flour and oil after and during substantial cooling of the heat-treated ingredients. The extruder and post extrusion mixer are operated at low pressures, generally less than about 20 bars absolute, preferably less than about 10 bars absolute. The relative amount of solid, crystalline or granulated sugar, such as sucrose, subjected to the heat treatment may be used to control the tenderness and crunchiness of the final product.

Description: COOKIE PRODUCTION WITH EXTRUSION HEAT TREATMENT AND POST EXTRUSION MIXING AND BAKING FIELD OF THE INVENTION The present invention relates to the production of cookies having a crumb-like structure using extrusion heat treatment and post extrusion mixing and baking. BACKGROUND OF THE INVENTION In the production of a high oil content farinaceous composition by extrusion cooking, mobility and immiscibility of the water and oil phases generally increase with increasing temperature. Additionally, the mechanical action of extruder screws tends to increase separation of oil from the remaining mass. The tendency for the oil to separate is at locations within the extruder at which the components are subjected to the highest pressure. Exemplary of high pressure locations in a twin screw extruder are: 1) the space between the extruder screw tips and the die orifice, and 2) the narrowest or more restricted passageways between the left and right hand screw elements. Oil separation under system pressure (screw or die pressure) can be manifested in extruder surging or uneven mass flow rates from the die. Upon extrusion from the die, separated oil may: 1) appear as a coating on the remaining dough mass, or 2) periodically discharge separately from the remaining dough mass. Non- homogeneous dough production and discontinuous extruder operation may thus result from oil separation. The problem of oil separation increases with increasing oil levels. Water separation from flour, up to the boiling point of water, is generally not a problem because of the more hydrophilic properties of flour components such as gluten and starch. As flour and water temperatures are raised, increased migration of water into starch granules, protein (e.g. gluten) denaturization, and starch gelatinization tend to occur. The binding or reaction of water with flour components may promote separation of oil: a) by making the flour components more polar or hydrophilic and b) by creating a greater mass of hydrophilic components. Conventional cookie production involves forming cookie dough preforms or pieces followed by baking of the pieces. Low temperatures, typically at about room temperature, are used to form the dough. The low temperature mixing generally avoids separation of shortening or fat from hydrophilic dough components. While baking temperatures in a conventional oven, such as a band oven, may promote oil separation, there is no mixing or pressing action performed at the baking temperatures. Any oil separation which may occur in such ovens does not generally interfere with continuous operability of the cookie production process as it would in a continuous cooker/extruder process. In addition to high temperature mixing and high system pressure, the presence of sugar in a cookie dough may also increase oil and water separation. Solubilization of sugars in water increases the relative amount of the hydrophilic mass. This in turn may tend to promote oil separation. In the process of the present invention, cookie products are produced using an extrusion cooker to promote Maillard browning and flavor development without the problems caused by the separation of oil from the remaining cookie dough mass. The extruded cookies or cookie-like products of the present invention have a cookie crumb or crumb-like structure and texture and exhibit structural integrity. SUMMARY OF THE INVENTION The present invention provides a continuous process for the production of cookies which exhibit a cookie crumb-like structure and structural integrity using a cooker extruder, post extrusion mixing, and post extrusion heating, such as dielectric radio frequency baking, microwave baking, conductive baking, hot air baking, infra red heating, frying or combinations thereof. The use of substantially the entire maximum available length of the extruder to heat treat ingredients comprising shortening or fat, flour and optionally, at least one texturizing ingredient such as sugar, permits significant production of browning and flavor components. It further substantially reduces the amount of post extrusion heat treatment required for final baking of the output product. Also, thermal stress on the extruder screws may be reduced by maintaining a more even temperature profile in the extruder. A cookie crumb-like structure is achieved by avoiding substantial starch gelatinization. Preferably, the starch carrying ingredients are coated with the oil, and then water is added to the hot flour and oil mass during and/or after heat treatment. Using an amount of water such that the water content of the dough-like mixture is sufficiently low so as to avoid substantial starch gelatinization further assures that no or substantially no starch gelatinization occurs. The use of low water contents also tends to reduce oil separation from hydrophilic cookie dough components at elevated temperatures. In embodiments of the present invention the ingredients are heated in the cooker extruder to a high temperature, for example at least about 150 β F, to reduce post extrusion baking time, and promote Maillard browning and flavor development. Preferably, the ingredients are heated to a temperature of at least about 200°F, more preferably at least about 250 β F, most preferably from about 300 β F to about 500"F, to obtain a heat-treated mass. The heat treated mass is formed at a relatively low pressure within the cooker extruder, generally less than about 20 bars absolute, preferably less than about 10 bars absolute. In embodiments of the present invention, the heat treated mass is cooled and admixed at low pressures with liquid water or a source of water and optional sugar in a post extrusion or second stage mixing device to obtain a substantially homogeneous dough-like mixture. Post extrusion mixing devices which may be used include a continuous mixer or a seond stage extruder or combinations thereof. The heat treated mass is cooled to a sufficiently low temperature so that upon its encountering of points of high pressure, the added water does not cause substantial oil separation and extruder surging. Cooling of the heat treated mass is preferably initiated prior to and continues after addition of the water. The temperature of the dough-like mixture which is formed is most preferably less than about 150°F but above about 100°F at the exit end of the post extrusion mixer. Preferably, the heat treated mass temperature upon addition of or during admixing with water or a liquid source of water in the cooker extruder and/or in the post extrusion mixer is from about 100 β F to about 300"F, more preferably from about 110 β F to about 212 β F. If the heat treated mass temperature is too low, viscosity may deleteriously increase, mixing may be more difficult, pressure may increase and substantial oil separation or surging may occur. Also, higher temperatures in the cooker extruder and/or in the post extrusion mixing device reduce post extrusion heating times. The added shortening or fat content of the dough¬ like mixture may, for example, be from about 12% by weight to about 40% by weight, preferably from about 20% by weight to about 30% by weight, based upon the weight of the dough-like mixture. The elimination or significant reduction of added water or a source of added water in a cooker extruder or post extrusion mixer tends to reduce oil separation from hydrophilic cookie dough components at elevated temperatures. It also reduces post extrusion heating time. However, added water or a source of water is needed in cookie production for formability or machinability of cookie doughs into sheets or pieces at high production rates. Water also helps to disperse cookie ingredients and to promote flavor and color development. In the present invention, preferably the amount of water added is less than the amount needed to reach a threshold or maximum consistency. In preferred embodiments of the present invention, the amount of water added to the heat treated mass may range from about 0.5% by weight to about 10% by weight, based upon the weight of the dough-like mixture. It may, for example, be from about 2% by weight to about 6% by weight, based upon the weight of the dough-like mixture, depending upon the heat treatment temperatures and the desired consistency for shaping or forming. The water content of the dough-like mixture is preferably as low as possible to reduce post extrusion heating time and to reduce the risk of substantial oil separation and extruder surging. It is generally less than about 20% by weight, preferably less than about 15% by weight, more preferably less than about 10% by weight, based upon the weight of the dough-like mixture. Process compatible ingredients can be added to adjust the texture of the products produced by the process of the present invention. For example, the relative amount of at least one solid, crystalline, or granulated sugar, such as sucrose, which is subjected to the heat treatment can be used to control the tenderness δ and crunchiness of the final product. Addition of a solid, or crystalline or granulated sugar, such as sucrose, and subjecting it to high extrusion temperatures tends to melt and/or dissolve the sugar crystals and thus promote a crunchy texture in the final product. Addition of all or a portion of the solid sugar to the cooled mass rather than subjecting it to high extrusion temperatures tends to avoid sugar melting and/or dissolution, and promotes a tender texture in the final product. In embodiments of this invention the sugar component may be added in an amount to provide, for example, from about 10% by weight to about 40% by weight, preferably from about 20% by weight to about 30% by weight total sugar solids, based upon the total weight of the dough-like mixture. Crystalline or granulated sucrose alone or used with other sugars is preferred. Dough-like mixtures of the present invention are extrudable through a die into a continuous rope or sheet. The pressure drop upon extrusion or across the extruder die is generally less than about 20 bars absolute, preferably less than about 10 bars absolute. The work done in producing the heat treated mass or the dough-like mixture, defined as the specific mechanical energy is generally low, for example less than about 40 watt-hrs/kg (or 18 watt-hrs/lb) . Preferably, substantial frictional heating does not occur in the cooker extruder with substantially all of the heating being provided by external or jacketed heaters. Puffing or expansion due to moisture or steam release upon exiting of the dough-like mass from the post extrusion mixer typically does not occur. The post extrusion mixer extrudate is formed into pieces and the pieces are leavened and further browned by subjecting them to at least one other heating source, such as a microwave oven, infrared oven, convection oven, dielectric radio frequency oven, a fryer, or conductive heater, to obtain cookie products which exhibit structural integrity and a crumb-like structure and texture. Generally, the volume increase upon post extrusion heating ranges from about 20% to about 200%. Leavening agents are optional and may be included in amounts up to about 5% by weight, based upon the weight of the dough-like mixture. Dough-like mixtures of the present invention having a shelf-stable water activity of less than about 0.7, preferably less than about 0.6 may be packaged as shelf stable products in moisture and oxygen impermeable packaging materials for subsequent leavening and browning in conventional home microwave or convection ovens. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a side view of an extruder and second stage mixing device of the present invention. Fig. 2. is an end cross-section of the extruder taken along line 2-2 of Fig. 1. Fig. 3 is a top view, partially broken away of the extruder and second stage mixing device of Fig. 1. Fig. 4 is a schematic representation of the screw configuration of the extruder of Fig. 1. Fig. 5 is a schematic representation of the screw configuration of the second stage mixing device of Fig. 1 wherein the second stage mixing device comprises an extruder. Fig. 6 is a schematic representation of an alternative screw configuration for the extruder of Fig. 1. Fig. 7 is a schematic representation of the screw configuration of the second stage mixing device of Fig. 1 wherein the second stage mixing device comprises a continuous mixer. DETAILED DESCRIPTION OF THE INVENTION In the present invention cookies are continuously produced using an extrusion cooker to continuously mix ingredients, to reduce post extrusion heating time, and to promote browning and flavor development. In preferred embodiments of the present invention, the heat treated mass continuously produced in the extrusion cooker is extruded and transferred to a post extrusion or second stage mixer, where it is cooled and admixed with ingredients comprising water to form a dough-like mixture. The dough-like mixture continuously produced in the post extrusion mixer is leavened using at least one other energy source to obtain baked goods having a crumb-like structure or cookie crumb. The post extrusion leavening may be by microwave energy, dielectric radio frequency energy, infrared energy, conductive heating, frying, or heated air, such as from a convection oven or fluidized bed heater. In addition to leavening the composition, the post extrusion heating further browns the dough-like mixture. Separation of oil from the remaining mass and extruder surging are avoided preferably by admixing water into heat-treated ingredients comprising flour and oil which are at a temperature of about 100°F to about 300"F, more preferably from about 110"F to about 212 β F. In embodiments of the present invention, water addition may be after and/or during substantial cooling of the heat treated ingredients. After the cooling of the heat treated ingredients, the post extrusion heating leavens the substantially unleavened extrudate. The volume increase resulting from the post extrusion heating or leavening step generally ranges from about 20% to about 200%, based upon the volume of the extrudate. The flour component may be any comminuted cereal grain or edible seed meal, derivatives thereof and mixtures thereof. Exemplary of the flour components which may be used are wheat flour, corn flour, oat flour, barley flour, rye flour, rice flour, potato flour, grain sorghum flour, corn starch, physically and/or chemically modified flours or starches, such as pregelatinized starches, and mixtures thereof. The flour may be bleached or unbleached. Wheat flour or mixtures of wheat flour with other grain flours are preferred. The amount of flour used in the compositions of the present invention ranges, for example, from about 30% by weight to about 70% by weight, preferably from about 45% by weight to about 55% by weight. Unless otherwise indicated, all weight percentages are based upon the total weight of all ingredients forming the dough-like mixtures or formulations of the present invention except for inclusions such as flavor chips, nuts, raisins, and the like. Thus, "the weight of the dough-like mixture" does not include the weight of inclusions. The flour may be replaced in whole or in part by flour substitutes or bulking agents such as, polydextrose, hollocellulose, macrocrystalline cellulose, mixtures thereof, and the like. Corn bran, wheat bran, oat bran, rice bran, mixtures thereof, and the like, may also be substituted in whole or in part for the flour for making a fiber enriched product, to enhance color, or to affect texture. Corn flour and/or wheat bran may be used, for example, to enhance color and affect texture. Exemplary amounts range up to about 15% by weight corn flour and up to about 20% by weight wheat bran, the percentages being based upon the total weight of ingredients forming the dough-like mixture. Preferably, the corn flour and wheat bran will each comprise from about 1 to about 10% by weight, more preferably from about 2% by weight to about 5% by weight, based upon the weight of the dough¬ like mixture. The shortening or fat used in the present invention may be any edible fat or oil or mixture thereof suitable for baking applications and may include conventional food-grade emulsifiers. Vegetable oils, lard, marine oils, and mixtures thereof which are fractionated, partially hydrogenated, and/or interesterified are exemplary of the shortenings or fats which may be used in the present invention. Edible reduced or low calorie, or non-digestible fats, fat substitutes, or synthetic fats, such as sucrose polyesters which are process compatible may also be used. The shortenings or fats may be solid or fluid at room temperatures of from about 75 β F to about 90 β F. The use of components which are solid or semi-solid at room temperatures are preferred so as to avoid possible oil seepage from the final product during storage. The shortening or fat component is preferably added to the extruder in the form of a heated oil to facilitate metering, mixing, and a fast heat up of the added ingredients. Generally, the amount of the shortening or fat component admixed with the flour component is, for example, at least about 12% by weight, and may, for example, go up to about 40% by weight, based upon the weight of the dough-like mixture. It preferably ranges from about 20% by weight to about 30% by weight, based upon the weight of the dough-like mixture. Exemplary emulsifiers which can be used include lecithin, sorbitan monostearate, mono- and/or di- glycerides, polyoxyethylene sorbitan fatty acid esters, such as polysorbates (e.g., polyoxyethylene (20) sorbitan monostearate) , and sodium stearoyl-2-lactate. Exemplary amounts are up to about 3% by weight of one or more emulsifiers based upon the weight of the flour. Process compatible ingredients which can be used to modify the texture of the products produced in the present invention include sugars such as sucrose, fructose, lactose, dextrose, galactose, maltodextrins, corn syrup solids, hydrogenated starch hydrolysates, protein hydrolysates, mixtures thereof, and the like. Reducing sugars, such as fructose, maltose, lactose, and dextrose or mixtures of reducing sugars may be used to promote browning. Fructose is the preferred reducing sugar, because of its ready availability and its generally more enhanced browning and flavor development effects. Exemplary sources of fructose include invert syrup, corn syrup, high fructose corn syrup, molasses. brown sugar, maple syrup, mixtures thereof, and the like. The texturizing ingredient, such as sugar may be admixed with the other ingredients in either solid or crystalline form, such as crystalline or granulated sucrose, granulated brown sugar, or crystalline fructose, or in liquid form, such as sucrose syrup or high fructose corn syrup. Humectant sugars, such as high fructose corn syrup, may be used to promote chewiness in the post-extrusion baked product. In embodiments of the present invention, the total sugar solids content, or the texturizing ingredient content, of the dough-like mixtures of the present invention is, for example, at least about 10% by weight, and may, for example, go up to about 40% by weight, based upon the weight of the dough-like mixture. It preferably ranges from about 20% by weight to about 30% by weight, based upon the weight of the dough-like mixture. Crystalline or granulated sucrose alone or with other sugars is preferred in the present invention. The sucrose content may, for example, be at least about 80% by weight, based upon the total sugar solids content of the dough-like mixture. The balance of the sugar solids may comprise fructose, dextrose, lactose, or mixtures thereof, for example. Sugar granulations which may be used range, for example, from about 4X to about 12X. The moisture contents of the dough-like mixtures of the present invention should be sufficient to provide the desired consistency to enable proper forming, machining, and cutting of the dough. The total moisture content of the dough-like compositions of the present invention will include any water included as a separately added ingredient, as well as the moisture provided by flour (which usually contains about 12% to about 14% by weight moisture) , and the moisture content of other dough additives included in the formulation, such as high fructose corn syrup, invert syrups, or other liquid humectants. Taking into account all sources of moisture in the dough-like mixture including separately added water, the total moisture content of the dough-like mixtures of the present invention is generally less than about 20% by weight, preferably less than about 15% by weight, more preferably less than about 10% by weight, based upon the weight of the dough-like mixture. The dough-like compositions of the present invention generally have a water or moisture content of at least about 5% by weight, based upon the weight of the dough-like composition. Generally, if the amount of added water is too low, the extrudate will tend to be slurry-like and cannot be cut into pieces. As the amount of water is increased the extrudate consistency increases, until a threshold level is reached. At this level, additional water reduces the consistency. However, as the amount of water is increased to reduce the consistency, there is an increased risk of substantial oil separation and extruder surging. The lower the pressure and/or temperature to which the heat treated mass is subjected to after water addition: the lower is the risk. Thus, adding an extrusion die to the extruder or to the post extrusion mixer: a) increases the pressures encountered by the ingredients in the extruder or post extrusion mixer which, b) increases the risk that the addition of water beyond the amount needed to reach the threshold level of consistency will result in oil separation which can reduce machinability. The consistency of the extrudate can be determined by measuring the force needed to penetrate a sample at a constant rate of penetration. An Instron Texture Analyzer Model 4202 can be used to determine the modulus of the sample, which is a measurement of the consistency of the sample. The modulus is the slope, in the linear region, of a plot of the strain or deformation (x-axis) versus the stress (y-axis) . The strain can be measured in inches and the stress can be measured in lbs force. A cylindrical shaped probe having a diameter of 4 mm can be used for the measurement of the consistency. The probe can be set to penetrate the sample at a constant speed of 0.2 inches/min. The sample dimensions can be about 1 inch square and 1/4 inch high, or thick. The sample temperature can be room temperature (about 70 - 75 β F) or higher. The more force required to penetrate the sample, the greater is its modulus and the greater is its consistency. Consistencies suitable for forming or cutting operations depend upon the particular operation and particular equipment utilized. For example, a consistency which is too high for wire cutting may be suitable for sheeting or rotary molding. For rotary molding, trie consistency at about the threshold level is suitable. For extrusion through a die, for producing a sheet for example, or for wire cutting, the consistency should be less than the threshold value. However, to reduce the risk of substantial oil separation in the extruder, the post extrusion mixer, or in post extrusion forming operations and to reduce post extrusion baking times, it is generally preferred that the amount of water added be less than the amount needed to reach the threshold or maximum consistency. Thus, it is generally preferred that the water content of the dough-like mixture is such that additional water will increase the consistency of the dough-like mixture. If the ratios of the amounts of the other ingredients are kept constant then: the amount of water added which is needed to reach the threshold level of consistency will depend upon the heat treatment of the ingredients. Generally, the longer the heating, or the higher the temperature of heating, the lower is the amount of water needed to reach the threshold level of consistency. In preferred embodiments of the present invention, the amount of water admixed with the heat treated mass may range, for example, from about 0.5% by weight to about 10% by weight, based upon the weight of the dough¬ like mixture. Depending upon the time and intensity of heat treatment and the consistency needed for shaping or forming, and the pressures involved, it may be more preferably from about 2% by weight to about 6% by weight, based upon the weight of the dough-like mixture. The added water may be in the form of pure or tap water, a liquid source of water, such as sucrose syrup, corn syrup, high fructose corn syrup, eggs, honey, molasses, mixtures thereof, and the like, alone or in combination with a dry source of water, such as the moisture content of dried eggs, corn syrup solids, and the like. Water, in the form of tap water or a liquid source of water, such as high fructose corn syrup, for example, may also be added in the heat treating stage. It may be added with the flour for example, in low amounts (e.g. less than about 2% by weight, based upon the weight of the dough-like mixture) which do not result in: a) substantial oil separation or extruder surging or, b) substantial starch gelatinization. In addition to the foregoing, the dough-like mixtures of the invention may include other additives conventionally employed in cookies. Such additives may include, for example, milk by-products, egg or egg by-products, cocoa, vanilla or other flavorings, as well as inclusions such as nuts, raisins, coconut, flavored chips such as chocolate chips, butterscotch chips and caramel chips, and the like. A source of protein which is suitable for inclusion in baked goods may be included in the dough-like compositions of the present invention to promote Maillard browning. The source of protein includes non- fat dry milk solids, dried or powdered eggs, mixtures thereof, and the like. The amount of the proteinaceous source may, for example, range up to about 5% by weight, based upon the weight of the dough-like mixture. The dough-like cookie compositions of the present invention may contain up to about 5% by weight of a leavening system, based upon the weight of the dough¬ like mixture. Chemical leavening agents or injected gases such as carbon dioxide can be used, but are not necessary for leavening the dough-like compositions of the present invention. Leavening action may be achieved by post extrusion heating of the composition which is sufficient to vaporize water in the dough-like cookie composition. However, the leavening agents may be used to adjust or control the degree of leavening and/or to control the pH of the cookie products. The inclusion of a leavening agent or other edible pH-adjusting agents may promote browning of the cookie mixture during processing within the extruder or during post-extrusion mixing and heating. A desired pH for the cookies or the dough-like mass is from about 5 to about 9.5, preferably from about 7 to 8.5. Generally, the more alkaline the composition, the greater the degree of browning. However, the pH should be adjusted so as not to adversely affect taste of the final product. A higher pH may be used to promote browning when forming the heat treated mass of the present invention, followed by adjustment of the pH after and/or during cooling of the heat treated mass. Exemplary of chemical leavening agents or pH adjusting agents which may be used include alkaline materials and acidic materials such as sodium bicarbonate, ammonium bicarbonate, sodium acid pyrophosphate, tartaric acid, mixtures thereof, and the like. In the process of the present invention, the flour component and shortening or fat are continuously and separately fed into the upstream portion of a cooker extruder. One or more crystalline or granulated sugars may be continuously added or preblended with the flour. However, continuous separate addition of the crystalline sugar to the upstream end of the extruder is preferred to avoid particle separation in the dry blend. The flour component, the shortening or fat, and the sugar components are generally initially conveyed in the extruder with cooling or without the application of external heat. They are conveyed and admixed while being heated to obtain a heat treated mass. In the present invention, the ingredients may be heated to temperatures above the minimum gelatinization temperature of the starch (assuming that a sufficient amount of water was available for reaction with the starch) but no or substantially no gelatinization (measured by differential scanning calorimetry) occurs. It is desireable that the oil sufficiently coats the starch containing flour particles to prevent substantial penetration of moisture into the starch granules so as to avoid substantial gelatinization. A cookie crumb-like structure is obtained by avoiding substantial starch gelatinization. Generally, starch gelatinization occurs when: a) water in a sufficient amount, generally at least about 30% by weight, based upon the weight of the starch, is added to and mixed with starch and, b) the temperature of the starch is raised to at least about 80°C (176 β F) , preferably 100 β C (212"F) or more. The gelatinization temperature may depend upon the amount of water available for reaction with the starch. The lower the amount of available water, generally, the higher the gelatinization temperature. Gelatinization may be defined as the collapse (disruption) of molecular orders within the starch granule manifested in irreversible changes in property such as granular swelling, native crystallite melting, loss of birefringence, and starch solubilization. The point of initial gelatinization and the range over which it occurs is governed by starch concentration, method of observation, granule type, and heterogeneities within the granule population under observation. Pasting is the phenomenon following gelatinization in the dissolution of starch. It involves granular swelling, exudation of molecular components from the granule, and eventually, total disruption of the granules. See Atwell et al, "The Terminology And Methodology Associated With Basic Starch Phenomenon," Cereal Foods World. Vol. 33, No. 3, Pgs. 306-311 (March 1988) . In the present invention, conditions under which no or substantially no gelatinization is preferably achieved are by embedding or coating the starch carrying ingredients, such as wheat flour, within the oil and then adding the water to the flour and oil mass. No or substantially no gelatinization may also be further assured by: a) reducing or substantially eliminating the addition of water, and/or b) admixing the water with the heat treated mass below the minimum temperature at which starch gelatinization can occur. In the process of the present invention, heating of the flour, shortening or fat, and sugar at as high a temperature as possible and for as long as possible for a maximum throughput rate without burning or other deleterious effects, is generally desirable for the development of browning and flavor. Maillard browning and flavor development involve the reaction between a reactive carbonyl group of a carbohydrate and a primary amino acid of the composition. The reaction proceeds through a series of intermediate reactions to finally produce the brown nitrogenous polymers. The heat treating step is believed to at least develop precursors to the polymeric nitrogen containing compounds. During the post-extrusion baking step, the colors develop faster than an uncooked dough under similar baking conditions. The flour component, shortening or fat component, and optionally the sugar or other texturizing components are heated in the cooker extruder generally to a temperature of at least about 150 β F, preferably at least about 200 β F, more preferably at least about 250"F, and most preferably from about 300°F to about 500"F. The average residence time for the flour, shortening or fat, and optional sugar components at these elevated temperatures in the extruder is, for example, from about 25 seconds to about 150 seconds. The heat treated mass is formed at a relatively low pressure within the cooker extruder. Pressures during the heat treating stage are generally less than about 20 bars absolute, preferably less than about 10 bars absolute. It is believed that the use of low pressures in the cooker extruder reduces the tendency for oil to separate from the remaining cookie ingredients. Preferably, substantially no frictional heating occurs in the cooker extruder. Substantially all of the heating is preferably supplied by external or jacketed heating means. Generally, the work done in the production of the heat treated mass and dough-like mixture is low, for example, less than about 40 watt hrs/kg (or less than about 18 watt hrs/lb) . The heat treated mass temperature before and/or during admixing with water or a liquid source of water should be sufficiently low so that the added water does not result in substantial separation of oil and extruder surging. The reduction of the temperature of the heat treated mass substantially reduces mobility and immiscibility of the water and oil phases. Also, it has been observed that the oil is most likely to separate from the remaining mass at the points of highest pressure, such as at the extruder die. Generally, the lower the pressures encountered by the heat treated mass upon or subsequent to the addition of the water, the less the heat treated mass needs to be cooled to avoid substantial oil separation and extruder surging. The cooling of the heat treated mass may begin in the extruder or after extrusion. Post extrusion cooling is preferred because it provides for longer residence times at elevated temperatures in the extruder for flavor and color development. The use of substantially the entire maximum available length of the extruder to heat treat the ingredients comprising oil, flour and optionally, at least one texturizing ingredient such as sugar, permits significant production of browning and flavor components. It further substantially reduces the amount of post extrusion heat treatment required for final baking of the output product. Also, thermal stress on the extruder screws may be reduced by maintaining a more even temperature profile in the extruder. The separation of the heat treatment zone of the first stage extruder from the lower temperature operation of the second stage mixing apparatus also eliminates the loss of heat by conduction through the screw shafts and the screw elements because the screw shafts of the first and second mixing stages are physically separate from one another. If the heat treated mass temperature is too low upon and/or during admixing it with the water or liquid source of water, viscosity may deleteriously increase. This may result in mixing difficulties, pressure increases, and substantial oil separation and extruder surging. Additionally, the less cooling performed within the cooker extruder and within the post extrusion mixer, the less is the amount of post extrusion heating needed for leavening. If pressures are sufficiently low (such as when an extruder die is not utilized) and if the mass temperature during heat treatment is sufficiently low, no or substantially no cooling may be needed to avoid substantial oil separation or extruder surging. However, higher heat treated mass temperatures are preferred for: 1) the promotion of browning and flavor development, and 2) reduced post extrusion heating times. Thus, it is generally preferred that the heat treated mass be heated to a high temperature, for example about 300°F to about 500 β F, and that the heat treated mass temperature be reduced, as needed to avoid substantial oil separation or extruder surging, before and/or during admixing it with water or a liquid source of water. Cooling of the heat treated mass is preferably initiated prior to and continues during admixing it with water or a liquid source of water to reduce the risk of substantial oil separation upon mixing or extrusion. Preferably, the heat treated mass temperature upon addition of water or a liquid source of water is from about 100 β F to about 300 β F, more preferably from about 110 β F to about 212"F. Generally, the heat treated mass undergoes a temperature drop of at least about 35 β F, preferably at least about 50 β F before and/or during admixing it with the water or liquid source of water. The heat treated mass is preferably cooled to a temperature below the boiling point of water (212 β F), more preferably to a temperature lower than about 200 β F, most preferably less than about 150 β F before or during admixing it with the water or liquid source of water to reduce the risk of substantial steam generation, and substantial oil separation and extruder surging. Admixing the water or liquid source of water with the heat treated mass at a mass temperature which is lower than the minimum gelatinization temperature of the starches included in the formulation may further assure that no or substantially no starch gelatinization occurs, particularly as the amount of water is increased. At the exit end prior to or at the optional post extrusion mixer die, which is generally the point of maximum pressure, the temperature of the dough-like mixture which is formed in the post extrusion mixer should be less than the boiling point of water (212 β F), more preferably less than about 200°F, most preferably less than about 150°F. Generally, the temperature of the heat treated mass and dough-like mixture in the post extrusion mixer should not be reduced to below about 100 β F, for example, to avoid mixing difficulties, increased pressure, or increased risk of substantial oil separation or extruder surging due, for example, to increased viscosity or oil solidification. Also, excessively low extrudate temperatures may impair post extrusion forming, shaping, and cutting operations. Increased post extrusion heating times and/or temperatures for leavening purposes also result from excessive cooling. In producing the dough-like mixtures in accordance with the present invention it is preferred that substantially no moisture content reduction occurs and that the dough-like mixture retains a sufficient amount of water for proper leavening during post extrusion heating. All or a portion of the texturizing ingredient, such as solid, crystalline or granulated sugar, may be admixed with the cooled heat treated mass at the same or at a different location from addition of the water or other aqueous source to control the texture of the final baked product. Addition of a solid, crystalline or granulated sugar, such as sucrose, and subjecting it to high extrusion temperatures tends to promote sugar melting and/or dissolution and thus a crunchy texture in the final product. Addition of all or a portion of the crystalline sugar to the cooled mass rather than subjecting it to high extrusion temperatures tends to avoid excessive sugar melting, and/or solubilization and promotes a tender texture in the final product. Thus, all, a portion (e.g. about 15% to about 85% by weight, based upon the total amount of solid, crystalline or granulated sugars) , or none of the solid or crystalline sugars may be subjected to the heat treating stage to control texture in the final, post extrusion baked product. Also, the greater the degree, or portion of sugar melting and/or dissolving, the less the viscosity of the extrudate. Accordingly, the relative amounts of solid or crystalline sugar: a) subjected to heat treatment upstream, and b) subjected only to the downstream cooling stage may be used to control the extrudate viscosity for subsequent forming or machining, and/or to control the texture of the final baked good. The downstream or second stage addition of a texturizing ingredient, such as sugar, reduces the mass subjected to heat treatment which permits heating of the upstream or first stage ingredients to a higher temperature at a given throughput rate. Also, the downstream addition of the texturizing ingredient such as sugar, which is at a relatively low temperature (e.g. about room temperature) helps to cool the heat treated mass. Various granulations may also be used to control the degree of sugar melting and/or dissolving, with larger sizes tending to result in less melting or dissolving. The addition of liquid sugar, such as sucrose syrup, may additionally promote crunchiness of the final product. The residence time of the added liquid water or added liquid source of water, as well as the residence time of the texturizing ingredient, such as sugar, added downstream after initiation of the reduction of the heat treated mass temperature should be sufficient to enable the attainment of a substantially homogeneous dough-like mixture. The residence time in the cooling or reduced temperature stage should also be sufficiently long to reduce the mass temperature so as to avoid substantial expansion or puffing of the dough-like mass upon extrusion. The average residence time in the post extrusion mixer of the water and crystalline sugar added to the heat treated mass may, for example, be from about 60 seconds to about 180 seconds. The heat treated mass upon exiting the cooker extruder may be further heated to promote further browning and flavor development and to reduce the amount of post extrusion heating needed for final baking of the output product provided that adverse oil separation or extruder surging does not occur. This further heating may be up to an additional 200 β F for a short period of time, e.g. 5-20 seconds. For example, a microwave heating device may be placed between the extruder and the post extrusion mixer for heating the heat treated mass before it enters the post extrusion mixer. The minimal amount of final baking required due to the use of the entire length of the extruder for heat treatment and the further use of the microwave applicator permits the addition of heat sensitive ingredients to the formulation, for example, through a downstream feed port in the post extrusion mixer. A microwave applicator which may be used is disclosed in copending U.S. patent application serial no. 362,374 entitled "Extruder And Continuous Mixer Arrangement For Producing An At Least Partially Baked Product Having A Cookie-Like Crumb Structure The Extruder Including A Microwave Applicator" filed in the name of Bernhard Van Lengerich on June 7, 1989. The disclosure of the latter application is incorporated herein by reference in its entirety. As disclosed therein, the microwave applicator is formed as a continuation of the screw channel at the downstream most end of the extruder. The screw channel beyond the screw elements and within the microwave applicator is conformed to a round channel surrounded by a source of microwave energy. The residence time of the ingredients within the microwave applicator is relatively short, e.g. about 5-20 seconds. Just prior to extrusion, or upon extrusion through an extruder die, the dough-like mixture formed in the post extrusion mixer may be heated, for example, by about 5"F to about 30 β F. This heating may be used to adjust dough consistency or viscosity provided that adverse oil separation or extruder surging does not occur. The post cooling heating may be used, for example, for controlling flow in the die, particularly at low moisture contents. The pressure in the cooling stage is generally less than about 20 bars absolute, preferably less than about 10 bars absolute. The pressure drop across the extrusion die is generally less than about 20 bars and preferably less than about 10 bars. Low pressures are preferred to avoid separation of oil from the remaining mass and to avoid surging. The leavening agents or pH adjusters may be added to the cooled mass in the cooling stage or they may be added prior to the cooling stage. They may be added in dry form either separately or as a pre-blend with the flour or solid or crystalline sugar, for example. They may also be added in aqueous form separately or as part of the added water. Emulsifiers may suitably be added with the shortening or fat in the heating stage or with the water in the cooling stage of the process of the present invention. Ingredients which promote Maillard browning, such as proteinaceous materials and reducing sugars are preferably added in the heat treating stage. The dry ingredients may, for example, be preblended with the flour or added separately. The proteinaceous materials and the reducing sugars may also be added in the cooling stage depending upon the degree of browning desired, and the water content of the ingredients. These ingredients, as well as any other additives in dry form may be preblended with the upstream or downstream sugar, for example, or added separately therefrom. Likewise, additives which are in liquid form may be preblended with the added water or liquid source of water or they may be separately added to the extruder and/or post extrusion mixer. Generally, preblending of minor ingredients for addition to the extruder and/or post extrusion mixer is preferred for achieving homogeneity. Heat labile ingredients, such as various vitamins, minerals, flavorings, coloring agents, sweeteners, such as aspartame, and the like, are preferably added in the cooling stage so as to reduce the possibility of thermal decomposition or degradation. The heat labile ingredients may, for example, be preblended with sugar added downstream in the cooling stage or with the added water. They may also be added separately, for instance downstream of the sugar or water addition. Shear sensitive ingredients, such as chocolate chips or other flavored chips, raisins, nuts, fruit pieces or other inclusions or particulates are preferably added to the cooling stage. The shear sensitive ingredients are most preferably added downstream of the downstream sugar and water addition. Adding the shear sensitive ingredients near the exit or in the last barrel section of the post extrusion mixer serves to maintain particle integrity by reducing their exposure to the mechanical action of the screw elements. Flavor chips, such as chocolate chips may be added at temperatures below room temperature, for example at about 20 β F to about 65"F so as to reduce melting of the chips in the dough-like mixture. Generally, the heat treated mass is extruded from the cooker extruder without substantial moisture loss or flashing, such as would cause substantial expansion or puffing, because of the low water content of the mass and the low pressure drop upon exiting the extruder. Generally, a die is not used with the cooker extruder. The extrudate from the cooker extruder may be dropped or conveyed into the inlet of a continuous post-extrusion mixer. The dough-like mixture is extruded from the post extrusion mixer to obtain an extrudate without substantial moisture loss or flashing because the temperature of the dough-like mixture exiting the post extrusion mixer is less than about 212 β F. The extruded dough-like mixtures of the present invention will preferably have a shelf-stable water activity of less than about 0.7, preferably less than about 0.6. The shelf-stable compositions of the present invention may be packaged as shelf stable products in moisture and oxygen impermeable packaging materials for subsequent leavening and browning in a post extrusion oven such as a conventional home microwave or convection oven. The dough-like mixture may exit the post extrusion mixer through a die having various shapes, such as animal shapes, circles, squares, triangles, star-shapes, and the like. The extrudate may be cut at the die by a rotating knife for example, or by a wire cutting device. The dough-like mixture may be formed into a continuous rope by the use of a round shaped die orifice. It may also be formed into a ribbon or sheet by the use of a horizontally oriented slit or elongated sheet shaped die orifice. The continuous ropes, ribbons, or sheets may be cut into pieces using known reciprocating cutters. The dough-like mixtures of the present invention may be extruded without the use of a die plate. The thus obtained extrudate, or even die-extruded extrudates, may be formed into pieces using conventional dough-shaping and forming equipment, such as rotary molders, wire cutting machines, sheeting rolls and reciprocating cutters, and the like. Unlike conventional cookie production, the extruded dough-like mixtures of the present invention are generally formed into pieces when hot. Excessive cooling of the extrudate may result in crumbling of the pieces upon wire cutting or other cutting or shaping operations. Preferably, the extrudates are formed into pieces at temperatures of from about 100"F to about 150 β F. Consistency, viscosity and plasticity of the extrudates for proper machining may be adjusted, for example, by: a) water or oil addition or reduction in the extruder, b) water addition or reduction in the post extrusion mixer, or c) heating prior to the die, at the die, or after exiting from the die. Cookie bits or cookie crumb-like products may be produced by extruding the dough-like mixture under very low pressure drops, e.g. without passing it through an extruder die, or at low die flow rates so that the extrudate spontaneously forms into pieces upon falling, onto a moving belt for example. Pieces or drops may also be produced by passing the dough-like mixture through a horizontal or vertical extruder die with a multitude of holes of a size of about 1/8" to about 1/2". The extrudate strands may then be cut at the die by a rotating knife into cylindrically shaped preheated dough bits. The pieces may then be leavened by post extrusion heating to form cookie-like pieces or bits. The bits may be screened or sized to obtain cookie bits or "cookie chips" having a substantially uniform size distribution. The cookie bits or cookie chips may be incorporated into other products, such as "granola type" bars. They may be used to produce a "cookie chip chocolate" product: a) by incorporating the cookie chips or bits into molten chocolate in a mold and then solidifying the chocolate, b) by pouring molten chocolate over the bits in a mold, or c) by enrobing individual or a plurality of bits with melted chocolate. The cookie chips may, for example, have a maximum dimension of about 1/8" to about 1/2". The amount of the cookie bits incorporated into the product may, for example, be from about 10% by weight to about 90% by weight, based upon the weight of the cookie chip chocolate product. The leavened cookie¬ like pieces or bits also may be: a) ground into crumbs for use in pie crusts, for example or, b) compacted, in a mold for example, to produce unitary cookie products. The unleavened dough bits may also be compacted in a mold to obtain a unitary product which may be subsequently leavened. Bits having different sizes and/or compositions may be combined in the mold to produce the unitary products. Filled products may be produced in accordance with the present invention by coextruding the dough-like mixture with filler materials. The coextrudate may be formed by the use of a concentric die or a tube inserted within the die orifice. Filled products may also be produced by transporting the dough-like mixture extrudate to a conventional enrobing or encrusting machine, such as produced by the Rheon Manufacturing Company for post extrusion filling with a filler material. Examples of fillers which may be used include chocolate, vanilla, butterscotch, fruit, peanut butter, and cheese-flavored fillings. The filling material may also be a separately produced dough-like mixture for the production of multi-flavored, multi-colored, or multi- textured cookie products. The extrudate pieces are leavened and further browned using: a) electromagnetic radiation or electronic heating, such as dielectric radio frequency heating, microwave heating, or infrared heating, b) heated air, such as from a convection oven or fluidized bed heater, c) frying, or d) combinations thereof. For example, a combination may comprise microwave heating or dielectric radio frequency heating for internal heating and infrared heating for more intense surface heating. The microwave, infrared, and radio frequency energy may be applied at pressures of from about 0.2 bars to about 6 bars. When applying dielectric heating, the low conductive food product to be heated is placed between electrodes, which act as capacitor plates, and forms the dielectric of one or more capacitors. A high frequency voltage is applied across the electrodes. Alternating of the electrostatic field or of the polarity of the voltage results in heating of the product. The frequencies generally used for dielectric heating are about 2 to 90 MHz, e.g. about 13-14 MHz, about 27 MHz, or about 40-41 MHz. The frequencies generally used for microwave heating are, for example, about 2,450 MHz for domestic ovens and about 896 to 915 MHz for industrial ovens. The heating of the pieces in the dielectric or radio frequency oven, microwave oven, or combinations thereof, or in a fryer is generally performed so that proper leavening and browning is achieved, for example, within about 90 seconds, preferably within about 60 seconds, depending upon the thickness and diameter of the pieces. Infrared heating, conductive heating, and hot air heating are generally conducted within about two to three minutes. Infrared heating should generally be performed subsequent to another form of post extrusion heating. It tends to heat the surface and form a skin which prevents leavening gases from escaping. Generally, the heating of the pieces or cookie preforms in the post extrusion oven should be sufficient to result in an internal temperature of at least about 160 β F, preferably at least about 190"F in the cookie. Dielectric radio frequency ovens, microwave ovens, infrared ovens, hot air ovens, and the like which may be used are conventional, industrial scale continuous throughput ovens. Continuous, conventional fryers may also be used in embodiments of the present invention. Conductive heating devices which may be used include waffle-type conductive heaters. The post extrusion heated leavened products of the present invention have a water activity of less than about 0.7, preferably less than about 0.6. The water content of the products is generally less than about 6% by weight, suitably from about 2% by weight to about 4% by weight, based upon the weight of the post extrusion baked product, exclusive of inclusions. The products exhibit a cookie crumb-like structure appearance, and texture and structural integrity. Starch gelatinization (measured by differential scanning calorimetry) for the cookie products of the present invention is generally less than about 5%. In the process of the present invention, a cooker extruder having two screws is preferably utilized. Preferably the screws of the extruder will be co- rotating, i.e., rotate in the same direction. Co- rotating twin screw elements, generally provide thorough mixing and conveying of the components, with the elements of one screw continuously wiping the other screw. This is particularly advantageous when the composition being mixed has a relatively high viscosity. Suitable extruders which may be used in the present invention include: (1) WENGER model series TX by Wenger of Sabetha, Kansas, (2) model series MPF by Baker Perkins, (3) model series BC by Creusot Loire of Paris, France, and preferably 4) model series ZSK or Continua by Werner and Pfleiderer. Single screw extruders including those with a horizontally oscillating screw during rotation (i.e. a Buss kneader by Buss of Pratteln, Switzerland) may also be used in accordance with the present invention. The post extrusion mixer may be at least one additional extruder or one or more commercially available continuous mixers. The post extrusion mixers may be operated in series or parallel to each other. A continuous mixer for use in the present invention comprises co-rotating screws and jacketed barrels with heating and/or cooling means. A continuous mixer is similar in construction to a cooker extruder except that for the same screw diameter, a continuous mixer has a greater free internal volume and thus operates to mix and convey ingredients at relatively lower pressures and shear than does an extrusion cooker to obtain a substantially homogeneous output. A continuous mixer which may be used is model ZPM-120 by Werner and Pfleiderer. An extruder is preferable as the second stage mixing device when a pressure build up is required for shaping, as for example, through an extrusion die. The extruder also permits an axial exit of the extrudate for unidirectional continuous processing. On the other hand, in a high volume production environment, a continuous mixer is preferred to provide a higher volumetric throughput and a better heat transfer from the ingredients for efficient and rapid cooling. A continuous mixer also permits a more efficacious particulate feeding. Screw configurations which may be used in the present invention are disclosed in copending U.S. patent application serial no. 362,579 entitled "Extruder And Continuous Mixer Arrangement For Producing An At Least Partially Baked Product Having A Cookie-Like Crumb Structure" filed in the name of Bernhard Van Lengerich on June 7, 1989. The disclosure of the latter application is incorporated herein by reference in its entirety. Screw configurations which may be used in the present invention with a model ZSK-57 twin screw cooker extruder are shown in Figs. 4 and 6 of said application. Screw configurations which may be used in the present invention with a second stage or post extrusion mixing device are shown in Figs. 5 and 7 of said application. The Fig. 5 screw configuration may be used where the second stage mixing device comprises an extruder. The Fig. 7 screw configuration may be used with a model ZSK- 120 continuous mixer as the second stage mixing device. The extruder throughput or mass flow rates utilized in the present invention with a Werner and Pfleiderer ZSK 57 twin screw cooker extruder are generally from about 150 lbs/hr to about 850 lbs/hr of extrudate. Higher rates may be achieved with other models. For example, a throughput rate of 6000 lbs/hr may be achieved using a Werner and Pfleiderer model Continua 120 cooker extruder. Referring now to the drawings and initially to Fig. 1, there is illustrated a side view of an extruder 10 and second stage mixing device 100 arranged according to the present invention. The extruder 10 comprises a plurality of barrel sections, e.g., twelve barrel sections 11-22, (see Fig. 4) each of which includes a figure eight cross-section bore or screw channel 23 formed therethrough (see Fig. 2) . The sections 11-22 are fastened end-to-end, to one another with the respective bore sections 23 axially aligned, as is well known, to provide the screw barrel of the extruder 10. A dry ingredient feed port 30 is provided in barrel section 11 for input of, for example, flour and a liquid feed 32 is arranged between barrel sections 11 and 12 for input of oil. The output end 80 of the extruder 10 is aligned above an inlet feed port 101 of the second stage mixing device 100. Thus, the heat treated ingredients output by the extruder 10 are fed, together with added water, input through a water inlet port 200, directly into the second stage mixing device 100. Twin screws 24, 25 can be arranged in the extruder 10 in an intermeshing arrangement, to extend through communicating screw channels 26, 27 of the figure eight cross-section bore 23 from one end of the extruder barrel formed by the barrel sections to the other end thereof. The twin screws 24, 25 are coupled to an electric motor 28, arranged adjacent the upstream end of the extruder 10 for rotation within the screw channels 26, 27. As illustrated in Fig. 1, the extruder 10 is divided into a blending zone and a mixing and heat treatment zone. The mixing and heat treatment zone is preferably arranged to extend along a substantial portion of the length of the extruder 10. Referring now to Fig. 4, there is illustrated, in schematic form, a specific screw configuration for each of the twin screws 24, 25 of the extruder 10. The illustrated screw configuration is now described as a representative embodiment of the present invention. Each of the screws 24, 25 comprises a series of elements intermeshing with an adjacent identical series of elements of the other screw 24, 25. Screw elements 34, 35, the upstream most elements, are arranged directly beneath the dry ingredient feed port 30. The screw elements 34, 35 each include a continuous screw-like thread 36 to rapidly convey dry ingredients such as flour and a portion of the crystalline sugar into the screw channel 23. Each of the elements 34, 35 comprises an 80/80/SK screw element which indicates that the screw-like thread has a pitch of 80 and that each element is 80 mm in length. The SK designation indicates a shuffle kneader which includes undercut threads to catch and carry dry ingredients as they are input through the dry ingredient feed port 30. The liquid feed port 32 is arranged adjacent the dry ingredient feed port 30 for input of oil. The screw elements 34, 35 generally comprise the blending zone of the extruder 10. A screw element 37 is arranged immediately downstream from the 80/80/SK elements 34, 35 and comprises an 80/40 screw element (i.e., a pitch of 80 and a length of 40 mm) . The screw element 37 is followed immediately by a 60/60 screw element 38 and a 40/40 screw element 39. The progressively shorter, lower pitch screw elements 37, 38, 39 decrease the speed of conveyance to thereby increase the degree of fill of the ingredients within the free volume of the bore 23. Degree of fill refers to the percentage of the free volume of the bore 23 occupied by ingredients being conveyed by the screw elements 24, 25. An igel element 40, which is 40 mm in length, is arranged immediately downstream from the screw element 39. An igel element includes churning projections 41 to provide a chopping action to the ingredients within the bore 23. The igel element 40 does not itself convey material which causes a further increase in the degree of fill. The through put flow of ingredients through the igel element 40 is caused by the pushing action on the ingredients by the screw elements 34, 35, 37, 38 and 39 upstream from the igel element 40. Two 40/40 screw elements 42, 43 are arranged immediately downstream from the igel element 40 to continue the conveyance of the ingredients. Two additional 40 mm igel elements 44, 45 are provided downstream from the screw element 43. These igel element elements 44, 45 are spaced from one another by a 40/40 screw element 46. Moreover, an additional 40/40 screw element 47 is arranged immediately downstream from the igel element 45. The igel element elements 44, 45 and screw elements 46, 47 thereby provide alternating elements to chop, convey, chop and convey the ingredients. This sequence gradually increases the degree of fill and churns the ingredients to afford a better mixing of the ingredients. A first kneading block element 48 is positioned directly downstream from the screw element 47. The kneading block element is used to mix the ingredients and comprises a KB/4/5/20 element. This indicates that it is a kneading block having mixing discs staggered at 45" right hand angles, relative to one another around the axis of rotation of the screw, 5 total discs in the element and the element is 20 mm long. The kneading element 48 is followed by a 40/40 screw element 49. Thereafter, there is an alternating sequence of kneading block elements 50-56 and interposed screw elements 57-63. Each of the intermediate screw elements 57-63 comprises a 40/40 screw element while the kneading block elements 50-56 comprise, in downstream order, a KB/45/5/20 element (kneading block 50) , four KB/45/5/40 elements (kneading blocks 51-54) and two KB/45/5/60 elements (kneading blocks 55-56) . The gradual increase in size of the kneading block elements 50-56 and relatively short, low pitch screw elements 57-63 in-between the successive kneading block elements causes a continuing increase in degree of fill and a vigorous mixing of the ingredients. Immediately downstream from the screw element 63 is a further series of alternating kneading block elements 65-70 with interposed screw elements 64 and 71-75. Each of the screw elements 64, 71-75 comprises a 60/60 screw element and each of the kneading block elements 65-70 comprises a KB/45/5/60 kneading block element. This configuration of alternating kneading block elements 65- 70 further vigorously mix the ingredients. The alternating kneading element sequences defined by kneading element 50-56 and 65-70 in barrel sections 14- 21 provide a vigorous mixing zone throughout a substantial portion of the length of the extruder. Each of the barrel elements 11-22 includes an electrical heating element 500 and cooling water flow tubing 501 to control the temperature of the barrel element (see Fig. 2) . Such a temperature controlled barrel element comprises, for example, a model ZSK-57 extruder barrel element manufactured by Werner & Pfleiderer. The viscosity of the ingredients comprising flour and oil is not sufficient for friction heating due to vigorous mixing action of the kneading block elements 50-56 and 65-70. Accordingly, the heating elements 500 of barrel elements 12-22 are operated to raise the temperature of the ingredients. The electrical heating elements 500 of the barrel elements 12-22 are operated to raise the temperature of the barrels to as high as possible, e.g., 350 β F, for a given throughput rate to promote Maillard browning and flavor development and to reduce the amount of post extrusion heat treatment required for final baking. The heated barrel sections 12-22 generally comprise the heat treatment zone of the extruder 10. In this manner, substantially all of the length of the extruder 10 is used for vigorous mixing and heat treating the ingredients comprising flour and oil fed through the inlet feed ports to the extruder 10. Thus, the ingredients fed through the first dry ingredient feed port 30 and first liquid feed port 32 are thoroughly mixed and heat-treated by the overall conveying churning and mixing action of the screws 24, 25 and heating 49 effect of the barrel sections 12-21. The term "vigorous" as used herein means a mixing action which is sufficient to thoroughly mix the ingredients input through the first dry ingredient feed port 30 including the flour, oil and, optionally, crystalline sugar, and to facilitate distribution of the heat applied by the heating elements throughout the ingredients. In addition, the term relates to increasing the degree of fill to a level accommodating heat conduction from the heating elements through the screw channel 23 and into the ingredients. Screw elements 76-79 are arranged downstream from the kneading block element 70 and comprise one 80/80 and three 60/60 elements, respectively, to increase the speed of conveyance and transport the ingredients out the open end 80 of the extruder 10. Referring now to Fig. 5, the second stage mixing device 100 comprises an extruder, which is about 12 1/d and includes four barrel sections 102-105 fastened end- to-end with twin screws (screw 106 illustrated) in a similar manner as the extruder 10. A motor 150 (see Fig. 1) is coupled to the screws for rotation. Relatively high pitch screw elements 107-109, e.g., 120/120 screw elements, are arranged directly below the ingredients comprising oil and flour from the extruder 10, and any added crystalline sugar downstream from feed port 101. The added water is input through the liquid feed port 200. As noted above, the added water modifies the consistency of the mixture to provide an elastic mass having sufficient formability and machinability for post extrusion processing. The screw elements 107-109 are followed by alternating kneading blocks 110-112 with interposed screw elements 113-114. The screw elements 113-114 are shorter and of lower pitch than the screw elements 107- 109, e.g., 80/80 so that, together with the kneading blocks 110-112 (e.g., KB/ 45/5/80 elements), they act to lower the speed of conveyance and increase the degree of fill to permit thorough mixing of the ingredients by the kneading block elements 110-112. However, the number of alternating kneading block elements is fewer than in the first extruder 10 to provide a gentle lower temperature mixing to avoid oil separation after the addition of the water. The barrel sections 102-105 of the second stage extruder include temperature control means (not shown) which are operated to maintain the barrel sections at lower temperatures than in the barrel sections of the heat treatment zone of the extruder 10 to further prevent oil separation after water addition. The alternating kneading blocks 110-112 are followed by three screw elements 115-117 of decreasing pitch and length (e.g., two 120/120 elements followed by an 80/80 element) to feed the ingredients into final kneading block elements 118-119 (e.g, KB/45/5/100 elements) for final mixing. A screw element 120 (e.g., a 120/60 element) is interposed between the kneading block elements 118, 119 and a final screw element 121 (e.g., an 80/80 element) is arranged downstream from the kneading block elements 118, 119 to output the cookie dough from second stage extruder 100. A second downstream inlet feed port 122 can be formed in barrel section 104, above the screw elements 115, 116 for input of ingredients such as particulate ingredients, e.g., nuts, chocolate chips, etc., and/or heat sensitive ingredients. The screw elements 115-116 increase the speed of conveyance of the ingredients below the second feed port 122, which decreases the degree of fill and facilitates the intake and mixing of the ingredients fed through the inlet port 122 by the kneading block elements 118-119. Referring now to Fig. 6, there is illustrated, in schematic form, an alternative screw configuration for each of twin screws 24', 25* of the extruder 10. As in the embodiment of Fig. 4, each of the screws 24', 25* comprises a series of elements intermeshing with an adjacent identical series of elements of the other screw 24*, 25'. Screw elements 34', 35•, the upstream most elements, are arranged directly beneath the first dry ingredient feed port 30'. The screw elements 34' , 35* each include a continuous screw-like thread 36' to rapidly convey dry ingredients such as flour and a portion of the crystalline sugar into the screw channel 23* . Each of the elements 34', 35' comprises an 80/80/SK screw element. The first liquid feed port 32' is arranged adjacent the first dry ingredient feed port 30' for input of oil. The screw elements 34', 35' generally comprise the blending zone of the extruder. A screw element 37' is arranged immediately downstream from the 80/80/SK elements 34', 35' and comprises an 80/40 screw element. The screw element 37' is followed immediately by a 60/60 screw element 38* and a 40/40 screw element 39*. The progressively shorter, lower pitch screw elements 37', 38', 39' decrease the speed of conveyance to thereby increase the degree of fill of the input oil and flour ingredients within the bore 23• . An igel element 40', which is 40 mm in length, is arranged immediately downstream from the screw element 39'. The igel element 40' includes churning projections 41 to provide a chopping action to the ingredients within the bore 23' . Two 40/40 screw elements 42', 43' are arranged immediately downstream from the igel element 40' to continue the conveyance of the ingredients. Two additional 40 mm igel elements 44', 45* are provided downstream from the screw element 43'. These igel elements 44', 45' are spaced from one another by a 40/40 screw element 46'. Moreover, an additional 40/40 screw element 47' is arranged immediately downstream from the igel element 45*. The igel elements 44', 45' and screw elements 46', 47' thereby provide alternating elements to chop, convey, chop and convey the ingredients. As in the screw configuration illustrated in Fig. 4, this sequence gradually increases the degree of fill and churns the ingredients to afford a better mixing of the ingredients. A first kneading block element 48' is positioned directly downstream from the screw element 47' . The kneading block element is used to mix the ingredients and comprises a KB/45/5/20 element. The kneading element 48' is followed by a 40/40 screw element 49 • . Thereafter, there is an alternating sequence of kneading block elements 50'-56' and interposed screw elements 57'-63'. Each of the intermediate screw elements 57'-63 » comprises a 40/40 screw element while the kneading block elements 50'-56' comprise, in downstream order, a KB/45/5/20 element (kneading block 50'), four KB/45/5/40 elements (kneading blocks 51*-54') and two KB/45/5/60 elements (kneading blocks 55'-56') . The gradual increase in size of the kneading block elements in size of the kneading block elements 50'-56' and relatively short, low pitch screw elements 57'-63' in-between the successive kneading block elements causes a continuing increase in degree of fill and a vigorous mixing of the ingredients. Thus, the kneading block elements 50'-56* in barrel sections 14'-17' comprise a vigorous mixing zone. Each of the barrel elements 11'-22' includes heating elements 500 and cooling water flow tubing 501 as shown in Fig. 2 to control the temperature of the barrel element. Such a temperature controlled barrel element comprises, for example, a model ZSK-57 extruder barrel element manufactured by Werner & Pfleiderer. The electrical heating elements of barrel elements 12'-22* are operated to raise the temperature of the ingredients. The heating elements of the barrel elements 12'-22' are operated to raise the temperature of the barrels to as high as possible, e.g., at least 350 β F, for a given throughput rate to promote Maillard browning and flavor development and to reduce the amount of post extrusion heat treatment required for final baking. Thus, the ingredients fed through the first dry ingredient feed port 30' and first liquid feed port 32' are thoroughly mixed and heat-treated by the overall conveying, churning and mixing action of the screws 24' , 25' in barrel sections 14'-17' and the heating effect of the barrel sections 12'-22'. The barrel sections 12'- 22' generally comprise the heat treatment zone of the extruder 10 which extends throughout substantially the entire length of the extruder 10. The vigorous mixing occurs in barrel sections 14'-17• . Immediately downstream from the last screw element 63' of the alternating screw and kneading block elements is a conveyance zone comprising a series of screw elements 64'-68* of generally increasing length and screw pitch. The conveyance zone is for the optional addition of crystalline sugar into the heat treatment zone to control texture and crunchiness of the final product. Thus, crystalline sugar can optionally be added downstream from the feed port 30' to reduce the exposure of the sugar to full heat treatment as a further control over the crunchiness of the cookie texture. As illustrated in Fig. 6, the series of screw elements 6 '-68' are located in barrel sections 17', 18* and 19'. Barrel section 18' can include a feed port 31' which can be opened or closed depending upon whether crystalline sugar is to be added into the conveyance zone. The screw elements 64'-68' comprise 60/60, 80/80/SK, 80/80/SK, 80/40 and 80/80 screw elements, respectively, which increases the speed of conveyance of the heat treated ingredients. Screw elements 69'-71' are arranged downstream from the screw elements 64'-68' and comprise one 60/60 and two 30/30 elements, respectively, to reduce the speed of conveyance and again gradually increase the degree of fill. A kneading block element 72', which comprises a KB/45/5/20 element, is provided downstream from the screw elements 69'-71' to further mix the ingredients including any optional sugar fed into the conveyance zone defined by the screw elements 64'-68'. Two additional screw elements 73• , 74' , which comprise a 40/40 and 80/160 element, respectively, convey the ingredients to a final kneading block element 75', which comprises a KB/45/5/60 element for final mixing of the ingredients. The kneading block elements 72', 75' provide the final mixing zone of the extruder. The final elements of the twin screws 24', 25' comprise screw elements 76'-78', which include an 80/80, a 60/60 and a 60/120 element, respectively. These elements convey the ingredients to the inlet port of the second stage mixing device 100. Referring now to Figure 7, there is illustrated in schematic form, a screw configuration for a second stage mixing device 100 which comprises a continuous mixer. The continuous mixer 100 includes three barrel sections 600-602 with the dry ingredient inlet port 101 and added water feed port 200 arranged in barrel section 600, the downstream inlet port 122 in barrel section 602 and a vertical output opening 603 in barrel section 602. The continuous mixer is a twin screw arrangement with one of the two identical screws 604 illustrated in Figure 7. Each of the screws includes 21 elements as set forth in the following table: Element No. Length (Fig. 7) (in mm) Element Type 605 270 single lobe conveying element 606 90 double lobe conveying element 607 30 kneading disc 608 30 kneading disc - 30° right hand staggered relativeto kneading disc 607 609 30 kneading disc - 30° right hand staggered relative to kneading disc 608 610 90 double lobe conveying element 611 30 kneading disc 612 30 kneading disc - 30" right hand staggered relative to kneading disc 611 613 30 kneading disc - 30° right hand staggered relative to kneading disc 612 614 30 kneading disc - 30" left hand staggered relative to kneading disc 613 615 30 kneading disc - 30° left hand staggered relative to kneading disc 614 616 60 kneading disc with pitch (for conveying effect) - 30° right hand staggered relative to kneading block 615 617 90 double lobe conveying element 618 90 double lobe conveying element 619 90 double lobe conveying element 620 60 kneading disc with pitch 621 30 kneading disc - 30° right hand staggered relative to element 620 622 30 kneading disc - 30" right hand staggered relative to element 621 623 90 double lobe conveying element 624 €0 kneading disc with pitch 625 60 kneading disc with pitch 30° right hand staggered relative to element 620 The single lobe screw element 605 rapidly conveys the heat treated ingredients comprising flour and oil from the extruder 10 together with any crystalline sugar input through the feed port 101 and the added water fed into the screw channel of the continuous mixer 100. The various kneading discs 607-609, 611-616, and 621, 622 ' with intermediate double lobe conveying elements 607, 610, 617, 618, 619 and 623 gently mix and convey the dough-like mass including added water toward the vertical output opening 603. The left hand staggering of kneading discs 614, 615 reduces the rate of conveying within the kneading discs 612-615 to increase the amount of mixing. The kneading discs with pitch 616, 620 both mix and convey the ingredients. The downstream inlet port 122 is arranged above the screw elements 617, 618 which provide a conveyance zone within the continuous mixer for rapid intake of particulate materials which may be input through the port 122. The double lobe conveying element 623 is arranged partially above the vertical output opening 603 to convey the dough-like mass toward and out of the continuous mixer 100. The kneading discs with pitch 624, 625 tend to dump the ingredients fed by the double lobe screw element 623 out of the opening 603. The barrel sections 600-602 include cooling jackets for water flow. A cooling water flow is pumped through the jackets in barrel sections 600-602 to reduce and adjust dough temperature during the gentle mixing and conveying of the dough-like mass by the continuous mixer. The present invention is further illustrated in the following examples where all parts, ratios, and percentages are by weight and all temperatures are in °F, unless otherwise stated: EXAMPLE 1 The ingredients, their feed placement, and their relative amounts used to prepare a cookie having a crumb-like structure and texture using extrusion heating, post extrusion mixing and microwave baking in accordance with the present invention were: INGREDIENT AND PLACEMENT WEIGHT ■ ' Component 1: first dry feed port Wheat flour, bleached (about 12% by weight water) 50.19 Non-fat dry milk (about 52% by weight lactose) 1.51 Salt 0.75 Component 2: second dry feed port White sugar (sucrose), granulated 15.82 Brown sugar (about 89% sucrose, 3% invert, 4% non-sugar solids, 3% water) 7.38 Component 3: first licπiid feed port Soybean spray oil 22.53 Component 4: second liquid feed port Tap water 0.81 Component 5: second dry feed port Sodium bicarbonate 1.01 Total 100.00 The co-rotating twin screw cooker extruder used to prepare the cookie products of the present invention was a Werner and Pfleiderer ZSK-57 equipped with an extruder screw configuration as shown in Fig. 6 of copending U.S. patent application serial no. 362,579 entitled "Extruder And Continuous Mixer Arrangement For Production Of An At Least Partially Baked Product Having A Cookie-Like Crumb Structure," filed in the name of Bernhard Van Lengerich on June 7, 1989. The extruder had twelve barrels, each provided with external, jacketed heating and cooling means. The first dry feed port was set up at barrel l and was open to the atmosphere. The first liquid feed port was set up between barrels 1 and 2. The first barrel, which contained the first dry feed port, was set on constant cool. The remaining eleven barrels were divided into 7 separately measured barrel temperature zones. The first through the twelfth barrels are hereafter also referred to in the Examples as "barrel 1," "barrel 2," "barrel 3," etc. Barrels 2 and 3 corresponded to temperature zone 1, barrel 4 corresponded to zone 2, barrels 5 and 6 corresponded to zone 3, barrels 7 and 8 corresponded to zones 4, and 5, respectively, barrels 9 and 10 corresponded to temperature zone 6, and barrels 11 and 12 corresponded to temperature zone 7. The thermocouples for measuring actual barrel temperatures were located in barrels 2, 4, 5, 7, 8, 10, and 12. Barrels 2 through 12 were set to heat to 300°F. Paddles and screw elements were arranged on the screw shafts from upstream to downstream to provide: a) rapid conveying of the added dry ingredients in barrel 1, b) conveying of the dry ingredients and added oil and gradually increasing the degree of fill in barrel 2, c) chopping or mixing action for admixing the oil and dry ingredients, conveying to gradually increase the degree of fill, and mixing in barrel 3, d) repeated conveying and an increased degree of mixing in barrel 4, e) increased mixing, conveying and increased mixing to gradually increase the degree of fill in each of barrels 5 and 6, f) increased mixing, conveying, and increased mixing to provide the highest degree of mixing in barrel 7, g) fast conveying in barrel 8, h) conveying with a gradual increase in degree of fill in barrel 9, i) conveying and mixing with a gradual increase in degree of fill in barrel 10, j) conveying and mixing in barrel 11, and k) conveying with a buildup in pressure sufficient to transport the heat treated mass out of the open end of the extruder. An extruder die was not utilized. Gradually increasing the degree of fill tends to reduce points of high pressure which may cause oil separation. The fast conveyance initiated in barrel 8 may be used for the optional addition of crystalline sugar into the heat treatment zone via an optionally opened feed port in barrel 8. The optional addition of the crystalline sugar in barrel 8 may be used to reduce the exposure of the sugar to full heat treatment as a further control over the crunchiness of the cookie. The twin screw continuous mixer used to prepare the cookie products of the present invention was a Werner and Pfleiderer ZPM-120 equipped with a screw configuration as shown in Fig. 7 of copending U.S. patent application serial no. 362,579 entitled "Extruder And Continuous Mixer Arrangement For Production Of An At Least Partially Baked Product Having A Cookie-Like Crumb Structure," filed in the name of Bernhard Van Lengerich on June 7, 1989. The continuous mixer had three barrel sections fastened end-to-end, each provided with cooling jackets for water flow. A cooling water flow is pumped through the jackets in the barrel sections to reduce and adjust the temperature of the composition during the gentle mixing and conveying in the continuous mixer. The second dry feed port was set up at barrel 1 of the continuous mixer and was open to the atmosphere. The second liquid feed port was the same as the second dry feed port at barrel 1. The second liquid feed inlet pipe was inserted into the open port at barrel 1 so that the second dry feed ingredients and the second liquid feed ingredients were separately fed into the same open port. The vertical output opening of the continuous mixer was located at the bottom end portion of the third barrel. The single lobe screw element of barrel 1 rapidly conveys the heat treated ingredients comprising flour and oil from the extruder together with the dry ingredients input through the second dry feed port and the added water fed via the second liquid feed port into the screw channel of the continuous mixer. Kneading discs with intermediate double lobe conveying elements gently mix and convey the dough-like mass including added water toward the vertical output opening. The left hand staggering of some of the kneading discs reduces the rate of conveying within the kneading discs to increase the amount of mixing. Kneading discs with pitch are located downstream of the left hand staggered kneading disks to both mix and convey the ingredients. The third barrel was equipped with a third feed port, which was open to the atmosphere, for input of shear sensitive and/or heat sensitive ingredients such as particulate ingredients, e.g., nuts, chocolate chips, raisins, etc. This downstream inlet port is arranged above double lobe screw elements which provide a conveyance zone within the continuous mixer for rapid intake of particulate materials, for example, which may be input through the port. A double lobe conveying element is arranged partially above the vertical output opening to convey the dough-like mass toward and out of the continuous mixer. Kneading discs with pitch located downstream of the latter double lobe conveying element tend to dump the ingredients fed by the double lobe screw element out the opening. The cooker extruder screws were rotated at about 130 rpm at about 1% of maximum torque. The continuous mixer screws were rotated at about 60 rpm at about 19% of maximum torque. The ingredients were fed in their relative amounts to provide a throughput or mass flow rate of the dough-like mixture extrudate from the continuous mixer of about 297 lbs/hrs. Component 1 was prepared by mixing the ingredients to obtain a substantially homogeneous dry blend. The component 1 dry blend was continuously fed to the first dry feed port. Component 2 was prepared by mixing the ingredients to obtain a second substantially homogeneous dry blend which was continuously fed downstream to the second dry feed port. Component 3 was prepared by melting the semi-solid soybean spray oil to obtain a liquid oil which was continuously fed to the first liquid feed port. Component 4 was continuously fed to the second liquid feed port. Component 5 was continuously fed to the second dry feed port, separate from component 2. On a calculated basis, the water content of the dough-like mixture formed in the continuous mixer was about 7.1% by weight, based upon the total weight of the dough-like mixture. At steady state, the barrel set temperatures and the actual barrel temperatures for the cooker extruder were : Barrel Set Actual Barrel Barrel # Temperature, "F Temperature, "F 1 cool 2 300 271 3 300 4 300 268 5 300 300 6 300 7 3 30000 299 8 300 269 9 300 10 300 265 11 300 1122 330000 300 Tap water was passed through the cooling jackets of the continuous mixer to cool the heat treated mass from the extruder while admixing it with the other ingredients fed to the continuous mixer. The pressure in the extruder and in the continuous mixer was less than about 10 bars. The material temperatures in the extruder were about 217 β F at barrel 3, about 222°F at barrel 5, and about 281°F at barrel 11. The average or median residence time of the ingredients heated in the cooker extruder was about 60- 90 seconds. The average or median residence time of the ingredients in the continuous mixer from the second feed ports was about 90 to 150 seconds. The heat treated mass formed in the cooker extruder was extruded without a die and resulted in a slurry-like substantially homogeneous heat treated mass. The heat treated mass was permitted to fall into the second dry ingredient feed port (the upstream end of the continuous mixer) . The extrudate temperature upon exiting the extruder was about 201 β F. The substantially homogeneous dough-like mixture formed in the continuous mixer was extruded from the mixer without a die and resulted in a substantially unleavened extrudate. The dough-like mixture upon exiting the continuous mixer had a temperature of about 130°F. The dough-like mixture was immediately transferred to an auger fed wire-cutting machine and was cut into pieces while hot. The diameter of the pieces was about 1 inch. The consistency of the dough-like mixture was measured at about 72°F using an Instron Texture Analyzer Model 4202 equipped with a cylindrical shaped probe having a diameter of 4 mm. The dimensions of the sample were about 1 inch square by about 1/4 inch high. The probe was set to penetrate the sample at a constant speed of 0.2 inches/min. With strain measured in inches and stress measured in lbs force, the modulus of the dough-like mixture sample was about 232 psi. Eight pieces were subjected to microwaving in a microwave oven for about 70 seconds to produce distinctly leavened cookies. The cookies were surface browned and had a crumb-like structure and crumb-like texture. EXAMPLE 2 Cookies having a crumb-like structure and texture may be produced as in Example 1 except: after wire cutting, the pieces may be subjected to heating in a continuous 12 kw dielectric radio frequency (27 MHz) oven for about 60 seconds to produce distinctly leavened, surface browned cookies. EXAMPLE 3 The procedure of Example 1 was followed using a composition without added water. The equipment of Example 1 was used in this Example. The ingredients, their feed placement, and their relative amounts were: INGREDIENT AND PLACEMENT WEIGHT % Component 1: first dry feed port Wheat flour, bleached (about 12% by weight water) 50.60 Non-fat dry milk (about 52% by weight lactose) 1.52 Salt 0.76 Component 2: second dry feed port White sugar (sucrose), granulated 15.95 Brown sugar (about 89% sucrose, 3% invert, 4% non-sugar solids, 3% water) 7.44 Component 3: first liquid feed port Soybean spray oil 22.71 Component 4: second liquid feed port Tap water none Component 5: second dry feed port Sodium bicarbonate 1.02 Total 100.00 The cooker extruder screws were rotated at about 120 rpm at about 1% of maximum torque. The continuous mixer screws were rotated at about 60 rpm at about 19% of maximum torque. The ingredients were fed in their relative amounts to provide a throughput or mass flow rate of the dough-like mixture extrudate from the continuous mixer of about 295 lbs/hrs. The components were prepared and fed as in Example 1 except component 4, the tap water, was not used. On a calculated basis, the water content of the dough-like mixture formed in the continuous mixer was about 6.3% by weight, based upon the total weight of the dough-like mixture. At steady state, the barrel set temperatures and the actual barrel temperatures for the cooker extruder were: Barrel Set Actual Barrel Barrel # Temperature. *F Temperature, *F 1 cool 2 300 253 3 300 4 3 30000 253 5 300 277 6 300 7 300 288 8 300 268 9 300 10 300 253 11 300 12 300 286 Tap water was passed through the cooling jackets of the continuous mixer to cool the heat treated mass from the extruder while admixing it with the other ingredients fed to the continuous mixer. The pressure in the extruder and in the continuous mixer was less than about 10 bars. The material temperatures in the extruder were about 217°F at barrel 3, about 222°F at barrel 5, and about 281"F at barrel 11. The average or median residence time of the ingredients heated in the cooker extruder was about 60- 90 seconds. The average or median residence time of the ingredients in the continuous mixer from the second feed ports was about 90 to 150 seconds. The heat treated mass formed in the cooker extruder was extruded without a die and resulted in a slurry¬ like substantially homogeneous heat treated mass. The heat treated mass was permitted to fall into the second dry ingredient feed port (the upstream end of the continuous mixer) . The extrudate temperature upon exiting the extruder was about 205°F. The substantially homogeneous mixture formed in the continuous mixer was extruded from the mixer without a die and resulted in a substantially unleavened extrudate. The mixture upon exiting the continuous mixer had a temperature of about 132 β F. The mixture had a low viscosity and was immediately transferred to an auger fed wire-cutting machine. However, the mixture was too soft for cutting on the wire cutter. The modulus of the mixture, as measured in Example 1, was about 35 psi. The low moisture mixture may be packaged as a shelf-stable product. The viscosity of the mixture, either before or after packaging, may be increased by the addition of water, in an amount of about 1% by weight for example, to provide proper consistency for shaping or machining. The dough-like mixture may then be leavened by subjecting it to microwave energy or convection heating to obtain distinctly leavened, surface browned cookies having a crumb-like structure and texture. EXAMPLE 4 The procedure of Example 1 was followed using a composition with about 2.45% by weight added water, based upon the weight of the composition. The equipment of Example 1 was used in this Example. The ingredients, their feed placement, and their relative amounts were: INGREDIENT AND PLACEMENT WEIGHT % Component 1: first dry feed port Wheat flour, bleached (about 12% by weight water) 49.37 Non-fat dry milk (about 52% by weight lactose) 1.48 Salt 0.74 Component 2: second dry feed port White sugar (sucrose) , granulated 15.55 Brown sugar (about 89% sucrose, 3% invert, 4% non-sugar solids, 3% water) 7.26 Component 3: first liquid feed port Soybean spray oil 22.16 Component 4: second liquid feed port Tap water 2.45 Component 5: second dry feed port Sodium bicarbonate 0.99 Total 100.00 The components were prepared and fed as in Example 1. The cooker extruder screws were rotated at about 120 rpm at about 1% of maximum torque. The continuous mixer screws were rotated at about 60 rpm at about 19% of maximum torque. The ingredients were fed in their relative amounts to provide a throughput or mass flow rate of the extrudate from the continuous mixer of about 302 lbs/hrs. On a calculated basis, the water content of the mixture formed in the continuous mixer was about 8.6% by weight, based upon the total weight of the mixture. At steady state, the barrel set temperatures and the actual barrel temperatures for the cooker extruder were: Barrel Set Actual Barrel Barrel # Temperature, °F Temperature, *F 1 COOl 2 3 30000 284 3 300 4 300 288 5 300 300 6 300 7 3 30000 300 8 300 271 9 300 10 300 278 11 300 1122 330000 300 Tap water was passed through the cooling jackets of the continuous mixer to cool the heat treated mass from the extruder while admixing it with the other ingredients fed to the continuous mixer. The pressure in the extruder and in the continuous mixer was less than about 10 bars. The material temperatures in the extruder were about 237 β F at barrel 3, about 230 β F at barrel 5, and about 248"F at barrel 11. The average or median residence time of the ingredients heated in the cooker extruder was about 60- 90 seconds. The average or median residence time of the ingredients in the continuous mixer from the second feed ports was about 90 to 150 seconds. The heat treated mass formed in the cooker extruder was extruded without a die and resulted in a slurry-like substantially homogeneous heat treated mass. The heat treated mass was permitted to fall into the second dry ingredient feed port (the upstream end of the continuous mixer) . The extrudate temperature upon exiting the extruder was about 201"F. The substantially homogeneous mixture formed in the continuous mixer was extruded from the mixer without a die and resulted in a substantially unleavened extrudate. The mixture upon exiting the continuous mixer had a temperature of about 130 β F. The mixture was immediately transferred to an auger fed wire-cutting machine. However, the mixture was too crumbly for cutting on the wire cutter. The modulus of the mixture, as measured in Example 1, was about 1121 psi. The consistency of the mixture, can be decreased by increasing the amount of oil, by reducing or increasing the amount of water added, by reducing the heat treating temperatures, or by a combination thereof to provide proper consistency for wire cutting. However, the obtained dough-like mixture may be successfully machined in a rotary molder to form individual pieces. The dough-like mixture may then be leavened by subjecting it to microwave energy or dielectric radio frequency heating to obtain distinctly leavened, surface browned cookies having a crumb-like structure and texture. EXAMPLE 5 The ingredients, their feed placement, and their relative amounts used to prepare a cookie having a crumb-like structure and texture using extrusion heating, post extrusion mixing and microwave baking in accordance with the present invention were: INGREDIENT AND PLACEMENT WEIGHT % Component 1: first dry feed port Wheat flour, bleached (about 12% by weight water) 50.50 Non-fat dry milk (about 52% by weight lactose) 1.51 Salt 0.76 Component 2: second dry feed port White sugar (sucrose), granulated 15.06 Brown sugar (about 89% sucrose, 3% invert, 4% non-sugar solids, 3% water) 7.03 Component 3: first liquid feed port Soybean spray oil 22.67 Component 4: second liquid feed port Tap water 1.22 Component 5: second dry feed port Sodium bicarbonate 1.25 Total 100.00 The procedure of Example 1 was followed and the equipment of Example 1 was used in this Example. The cooker extruder screws were rotated at about 125 rpm at about 3% of maximum torque. The continuous mixer screws were rotated at about 60 rpm at about 19% of maximum torque. The ingredients were fed in their relative amounts to provide a throughput or mass flow rate of the dough-like mixture extrudate from the continuous mixer of about 295 lbs/hr. On a calculated basis, the water content of the dough-like mixture formed in the continuous mixer was about 7.5% by weight, based upon the total weight of the dough-like mixture. The barrel set temperatures in the cooker extruder were constant cool in barrel 1 and 350"F in barrels 2 through 12_ Actual barrel temperatures for the cooker extruder were not measured. Tap water was passed through the cooling jackets of the continuous mixer to cool the heat treated mass from the extruder while admixing it with the other ingredients fed to the continuous mixer. The pressure in the extruder and in the continuous mixer was less than about 10 bars. The average or median residence time of the ingredients heated in the cooker extruder was about 60-90 seconds. The average or median residence time of the ingredients in the continuous mixer from the second feed ports was about 90 to 150 seconds. The heat treated mass formed in the cooker extruder was extruded without a die and resulted in a slurry¬ like substantially homogeneous heat treated mass. The heat treated mass was permitted to fall into the second dry ingredient feed port (the upstream end of the continuous mixer) . The dough-like mixture temperature within the exit of the extruder was about 255"F. The substantially homogeneous mixture formed in the continuous mixer was extruded from the mixer without a die and resulted a substantially unleavened extrudate. The mixture upon exiting the continuous mixer had a temperature of about 126°F. The dough-like mixture was immediately transferred to an auger fed wire-cutting machine and was cut into pieces while about 106°F. The diameter of the pieces was about 1 inch. Eight pieces were subjected to microwaving in a microwave oven for about 70 seconds to produce distinctly leavened cookies. The cookies were surface browned and had a crumb-like structure and crumb-like texture. EXAMPLE 6 Cookies having a crumb-like structure and texture using extrusion heating, post extrusion mixing and dielectric radio frequency baking in accordance with the present invention may be produced as in Example 5 except: after wire cutting the pieces may be subjected to heating in a continuous 12 kw dielectric radio frequency (27 MHz) oven set at about 81% power for about 60 seconds to produce distinctly leavened, surface browned cookies. EXAMPLE 7 The ingredients, their feed placement, and their relative amounts used to prepare a cookie having a crumb-like structure and texture using extrusion heating, post extrusion mixing and microwave baking in accordance with the present invention were: INGREDIENT AND PLACEMENT WEIGHT % Component 1: first dry feed port Wheat flour, bleached (about 12% by weight water) 49.43 Non-fat dry milk (about 52% by weight lactose) 1.48 Salt 0.74 Component 2: second dry feed port White sugar (sucrose), granulated 15.58 Brown sugar (about 89% sucrose, 3% invert, 4% non-sugar solids, 3% water) 7.26 Component 3: first liquid feed port Soybean spray oil 22.35 Component 4: second liquid feed port Tap water 2.23 Component 5: second dry feed port Sodium bicarbonate 0.93 Total 100.00 The procedure of Example 1 was followed and the equipment of Example 1 was used in this Example. The cooker extruder screws were rotated at about 125 rpm. The continuous mixer screws were rotated at about 60 rpm at about 23% of maximum torque. The ingredients were fed in their relative amounts to provide a throughput or mass flow rate of the dough-like mixture extrudate from the continuous mixer of about 302 Ibs/hrs. On a calculated basis, the water content of the dough-like mixture formed in the continuous mixer was about 8.4% by weight, based upon the total weight of the dough-like mixture. At steady state, the barrel set temperatures and the actual barrel temperatures for the cooker extruder were: Barrel Set Actual Barrel Barrel # Temperature, "F Temperature, "F 1 cool 2 300 205 3 300 4 300 202 5 300 300 6 300 7 300 300 8 300 270 9 300 10 300 255 11 300 12 300 301 Tap water was passed through the cooling jackets of the continuous mixer to cool the heat treated mass from the extruder while admixing it with the other ingredients fed to the continuous mixer. The pressure in the extruder and in the continuous mixer was less than about 10 bars. The material temperature in the extruder at barrel 12 was about 290 β F. The average or median residence time of the ingredients heated in the cooker extruder was about 60- 90 seconds. The average or median residence time of the ingredients in the continuous mixer from the second feed ports was about 90 to 150 seconds. The heat treated mass formed in the cooker extruder was extruded without a die and resulted in a slurry-like substantially homogeneous heat treated mass. The heat treated mass was permitted to fall into the second dry ingredient feed port (the upstream end of the continuous mixer) . The dough-like mixture temperature within the exit of the extruder was about 265°F. The substantially homogeneous dough-like mixture formed in the continuous mixer was extruded from the mixer without a die and resulted in a substantially unleavened extrudate. The dough-like mixture upon exiting the continuous mixer had a temperature of about 118°F. The dough-like mixture was pressed into a sheet about 5 mm thick by hand while hot. The sheet was cut into cylindrical pieces by hand using a cookie cutter. The diameter of the pieces was about 1 1/4 inch. Six pieces were subjected to microwaving in a microwave oven for about 45 seconds to produce distinctly leavened cookies. The cookies were surface browned and had a crumb-like structure and crumb-like texture. EXAMPLE 8 Cookies having a crumb-like structure and texture using extrusion heating, post extrusion mixing and microwave baking in accordance with the present invention were produced as in Example 7 except nut pieces were added to the open third dry feed port in barrel 3 of the continuous mixer at a rate of about 120 lbs/hr. EXAMPLE 9 A cookie having a crumb-like structure and texture using extrusion heating, post extrusion mixing and microwave baking may be produced in accordance with the present invention as in Example 1 except: a) the screw configuration for the Werner and Pfleiderer ZSK-57 cooker extruder may be replaced with the screw configuration shown in Fig. 4 of copending U.S. patent application serial no. 362,579 entitled "Extruder And Continuous Mixer Arrangement For Production Of An At Least Partially Baked Product Having A Cookie-Like Crumb Structure," filed in the name of Bernhard Van Lengerich on June 7, 1989, and b) the Werner and Pfleiderer ZPM- 120 continuous mixer may be replaced with a four barrel extruder and screw configuration as shown in Fig. 5 of said latter application. For the Werner and Pfleiderer ZSK-57 extrusion cooker, paddles and screw elements are arranged on the screw shafts from upstream to downstream to provide: a) rapid conveying of the added dry ingredients in barrel 1, b) conveying of the dry ingredients and added oil and gradually increasing the degree of fill in barrel 2, c) chopping or mixing action for admixing the oil and dry ingredients, conveying to gradually increase the degree of fill, and mixing in barrel 3, d) repeated conveying and an increased degree of mixing in barrel 4, e) increased mixing, conveying and increased mixing to gradually increase the degree of fill in each of barrels 5 and 6, f) increased mixing, conveying, and increased mixing to provide the highest degree of mixing in barrel 7, g) further conveying and vigorous mixing in barrels 8, 9, 10 and 11, and h) increased speed of conveyance to transport the heat treated mass out of the open end of the extruder. Gradually increasing the degree of fill tends to reduce points of high pressure which may cause oil separation. For the second stage twin screw extruder (12 1/d) described in said latter copending U.S. patent application serial no. 362,579, four barrel sections are fastened end-to-end, each provided with external jacketed heating and cooling means. The second dry feed port is set up at barrel 1 of the second stage extruder and is open to the atmosphere. The second liquid feed port is the same as the second dry feed port at barrel 1. The second liquid feed inlet pipe is inserted into the open port at barrel 1 so that the second dry feed ingredients and the second liquid feed ingredients can be separately fed into the same open port. For the screw configuration of the second stage twin screw extruder shown in Fig. 5 of said latter copending U.S. patent application serial no. 362,579 relatively high pitch screw elements are arranged directly below the second dry ingredient feed port and second liquid inlet to convey the added ingredients downstream and away from the feed port. These elements rapidly convey the heat treated mass from the extruder and the liquid and dry ingredients added to the second stage extruder via the second dry ingredient feed port in barrel 1 of the second stage extruder. The rapid conveying screw elements of barrel 1 are followed by alternating kneading blocks with interposed screw elements in barrel 2 of the second stage extruder. The screw elements in barrel 2 are shorter and of lower pitch than the screw elements of barrel 1 so that. together with the kneading blocks, they act to lower the speed of conveyance and increase the degree of fill to permit thorough mixing by the kneading blocks in barrel 2. However, the number of alternating kneading blocks is fewer than in the first stage cooker extruder to provide a lower pressure and gentle mixing to protect the crystalline structure of the sugar grains. The alternating kneading blocks are followed by three screw elements in barrel 3 of gradually decreasing pitch and length to feed the ingredients into final kneading blocks for final mixing in barrel 4. In barrel 4 a screw element is interposed between the kneading blocks, and a final screw element is arranged downstream from the kneading blocks to output the at least substantially homogeneous cookie dough from the second stage extruder. The exit portion of the second stage extruder is located at the bottom end portion of barrel 4. A third dry feed port, open to the atmosphere, can be formed in barrel 3 for input of shear sensitive and/or heat sensitive ingredients such as particulate ingredients, e.g., nuts, chocolate chips etc. The screw elements below the third dry feed port increase the speed of conveyance of the ingredients which decreases the degree of fill and facilitates the intake and mixing of particulate materials by the kneading blocks in barrel 4. EXAMPLE 10 The ingredients, their feed placement, and their relative amounts used to prepare a rotary molded cookie having a crumb-like structure and texture using extrusion heating, post extrusion mixing and microwave baking in accordance with the present invention were: INGREDIENT AND PLACEMENT WEIGHT % Component 1: first dry feed port Wheat flour, bleached (about 12% by weight water) 46.22 Non-fat dry milk (about 52% by weight lactose) 1.39 Salt 0.69 Component 2: second dry feed port White sugar (sucrose), granulated 14.57 Brown sugar (about 89% sucrose, 3% invert, 4% non-sugar solids, 3% water) 6.78 Component 3: first liquid feed port Soybean spray oil 18.27 Component 4: second liquid feed port Tap water 11.15 Component 5: second dry feed port Sodium bicarbonate 0.93 Total 100.00 The procedure of Example 1 was followed and the equipment of Example 1 was used in this Example. The cooker extruder screws were rotated at about 120 rpm at about 2% of maximum torque. The continuous mixer screws were rotated at about 60 rpm at about 21% of maximum torque. The ingredients were fed in their relative amounts to provide a throughput or mass flow rate of the dough-like mixture extrudate from the continuous mixer of about 323 lbs/hrs. On a calculated basis, the water content of the dough-like mixture formed in the continuous mixer was about 16.9% by weight, based upon the total weight of the dough-like mixture. At steady state, the barrel set temperatures and the actual barrel temperatures for the cooker extruder were: Barrel Set Actual Barrel Barrel # Temperature, "F Temperature, "F 1 cool 2 350 300 3 350 4 350 312 5 350 327 6 350 7 350 350 8 3 35500 336 9 350 10 350 350 11 350 12 350 349 Tap water was passed through the cooling jackets of the continuous mixer to cool the heat treated mass from the extruder while admixing it with the other ingredients fed to the continuous mixer. The pressure in the extruder and in the continuous mixer was less than about 10 bars. The material temperature in the extruder at barrels 3, 5, and 11 was about 243°F, 244°F, and 333, respectively. The average or median residence time of the ingredients heated in the cooker extruder was about 60-90 seconds. The average or median residence time of the ingredients in the continuous mixer from the second feed ports was about 90 to 150 seconds. The heat treated mass formed in the cooker extruder was extruded without a die and resulted in a slurry-like substantially homogeneous heat treated mass. The heat treated mass was permitted to fall into the second dry ingredient feed port (the upstream end of the continuous mixer) . The extrudate temperature upon exiting the extruder was about 215"F. The substantially homogeneous dough-like mixture formed in the continuous mixer was extruded from the mixer without a die and resulted in a substantially unleavened extrudate. The dough-like mixture upon exiting the continuous mixer had a temperature of about 107"F. The dough-like mixture was formed into pieces using a rotary molder having the detailing of an Oreo cookie base cake. The dough-like mixture was formed into pieces and the pieces were successfully released from the rotary molder, but the pieces were devoid of detailing. The dough-like mixture may be successfully rotary molded in a less detailed rotary mold. Six pieces were subjected to microwaving in a microwave oven for about 40 seconds to produce distinctly leavened cookies. The cookies were surface browned and had a crumb-like structure and crumb-like texture. EXAMPLE 11 The ingredients, their feed placement, and their relative amounts used to prepare a rotary molded cookie having a crumb-like structure and texture using extrusion heating, post extrusion mixing and microwave baking in accordance with the present invention were: INGREDIENT AND PLACEMENT WEIGHT % Component 1: first dry feed port Wheat flour, bleached (about 12% by weight water) 45.23 Non-fat dry milk (about 52% by weight lactose) 1.36 Salt 0.68 Component 2: second dry feed port White sugar (sucrose), granulated 14.26 Brown sugar (about 89% sucrose, 3% invert, 4% non-sugar solids, 3% water) 6.65 Component 3: first liquid feed port Soybean spray oil 19.09 Component 4: second liquid feed port Tap water 11.82 Component 5: second dry feed port Sodium bicarbonate 0.91 Total 100.00 The procedure of Example 1 was followed and the equipment of Example 1 was used in this Example. The cooker extruder screws were rotated at about 120 rpm at about 1% of maximum torque. The continuous mixer screws were rotated at about 60 rpm at about 21% of maximum torque. The ingredients were fed in their relative amounts to provide a throughput or mass flow rate of the dough-like mixture extrudate from the continuous mixer of about 330 lbs/hrs. On a calculated basis, the water content of the dough-like mixture formed in the continuous mixer was about 17.4% by weight, based upon the total weight of the dough-like mixture. At steady state, the barrel set temperatures and the actual barrel temperatures for the cooker extruder were: Barrel Set Actual Barrel Barrel # Temperature. °F Temperature, "F 1 cool 2 350 295 3 350 4 350 316 5 350 325 6 350 7 350 350 8 8 3 35500 333 9 350 10 350 350 11 350 12 350 350 Tap water was passed through the cooling jackets of the continuous mixer to cool the heat treated mass from the extruder while admixing it with the other ingredients fed to the continuous mixer. The pressure in the extruder and in the continuous mixer was less than about 10 bars. The material temperature in the extruder at barrels 3, 5, and 11 was about 255°F, 245"F, and 333 β F, respectively. The average or median residence time of the ingredients heated in the cooker extruder was about 60-90 seconds. The average or median residence time of the ingredients in the continuous mixer from the second feed ports was about 90 to 150 seconds. The heat treated mass formed in the cooker extruder was extruded without a die and resulted in a slurry-like substantially homogeneous heat treated mass. The heat treated mass was permitted to fall into the second dry ingredient feed port (the upstream end of the continuous mixer) . The extrudate temperature upon exiting the extruder was about 240°F. The substantially homogeneous dough-like mixture formed in the continuous mixer was extruded from the mixer without a die and resulted in a substantially unleavened extrudate. The dough-like mixture upon exiting the continuous mixer had a temperature of about 114"F. The dough-like mixture was formed into pieces using a rotary molder. The detailing was better than that obtained in Example 10. Six pieces were subjected to microwaving in a microwave oven for about 40 seconds to produce distinctly leavened cookies. The cookies were surface browned and had a crumb-like structure and crumb-like texture. EXAMPLE 12 The procedure of Example 1 was followed using a composition with about 12.61% by weight added water, based upon the weight of the composition. The equipment and procedure of Example 11 was used in this Example. The ingredients, their feed placement, and their relative amounts were: INGREDIENT AND PLACEMENT WEIGHT % Component 1: first drv feed port Wheat flour, bleached (about 12% by weight water) 49.37 Non-fat dry milk (about 52% by weight lactose) 1.48 Salt 0.74 Component 2: second drv feed port White sugar (sucrose), granulated 15.55 Brown sugar (about 89% sucrose, 3% invert, 4% non-sugar solids, 3% water) 7.26 Component 3: first liquid feed port Soybean spray oil 22.16 Component 4: second liquid feed port Tap water 2.45 Component 5: second drv feed port Sodium bicarbonate 0.99 Total 100.00 The components were prepared and fed as in Example 1. The cooker extruder screws were rotated at about 120 rpm at about 1% of maximum torque. The continuous mixer screws were rotated at about 60 rpm at about 19% of maximum torque. The ingredients were fed in their relative amounts to provide a throughput or mass flow rate of the extrudate from the continuous mixer of about 302 lbs/hrs. On a calculated basis, the water content of the mixture formed in the continuous mixer was about 8.6% by weight, based upon the total weight of the mixture. At steady state, the barrel set temperatures and the actual barrel temperatures for the cooker extruder were: Barrel Set Actual Barrel Barrel # Temperature, Temperature. °F 1 cool 2 350 308 3 350 4 350 317 5 350 346 6 350 7 350 348 8 350 313 9 350 10 350 346 11 350 12 350 342 Tap water was passed through the cooling jackets of the continuous mixer to cool the heat treated mass from the extruder while admixing it with the other ingredients fed to the continuous mixer. The pressure in the extruder and in the continuous mixer was less than about 10 bars. The material temperature in the extruder at barrels 3, 5, and 11 was about 239 β F, 232"F, and 32 β F, respectively. The average or median residence time of the ingredients heated in the cooker extruder was about 60-90 seconds. The average or median residence time of the ingredients in the continuous mixer from the second feed ports was about 90 to 150 seconds. The heat treated mass formed in the cooker extruder was extruded without a die and resulted in a slurry-like substantially homogeneous heat treated mass. The heat treated mass was permitted to fall into the second dry ingredient feed port (the upstream end of the continuous mixer) . The extrudate temperature upon exiting the extruder was about 230 β F. The substantially homogeneous dough-like mixture formed in the continuous mixer was extruded from the mixer without a die and resulted in a substantially unleavened extrudate. The dough-like mixture upon exiting the continuous mixer had a temperature of about 106"F. The dough-like mixture was oily to the touch and did not roll on the rotary molder. A leavenable, rotary moldable dough-like mixture may be produced by reducing the moisture content of the dough-like mixture. The dough-like mixture may then be leavened by subjecting it to microwave energy or dielectric radio frequency heating to obtain distinctly leavened, surface browned cookies having a crumb-like structure and texture. EXAMPLE 13 Cookies having a crumb-like structure and texture were produced as in Example 10 except: after rotary molding, the pieces were subjected to heating in a continuous 12 kw dielectric radio frequency (27 MHz) oven for about 59 seconds to produce distinctly leavened, surface browned cookies. EXAMPLE 14 The ingredients, their feed placement, and their relative amounts used to prepare a cookie having a crumb-like structure and texture using extrusion heating, post extrusion mixing, wire cutting and microwave baking in accordance with the present invention were: INGREDIENT AND PLACEMENT WEIGHT % Component 1: first dry feed port Wheat flour, bleached (about 12% by weight water) 46.07 Non-fat dry milk (about 52% by weight lactose) 1.38 Salt 0.69 Component 2: second dry feed port White sugar (sucrose), granulated 14.52 Brown sugar (about 89% sucrose, 3% invert, 4% non-sugar solids, 3% water) 6.78 Component 3: first liquid feed port Soybean spray oil 16.67 Component 4: second liquid feed port Tap water 12.96 Component 5: second drv feed port Sodium bicarbonate 0.93 Total 100.00 The procedure of Example 1 was followed and the equipment of Example 1 was used in this Example. The cooker extruder screws were rotated at about 130 rpm at about 2% of maximum torque. The continuous mixer screws were rotated at about 60 rpm at about 21% of maximum torque. The ingredients were fed in their relative amounts to provide a throughput or mass flow rate of the dough-like mixture extrudate from the continuous mixer of about 324 lbs/hr. On a calculated basis, the water content of the dough-like mixture formed in the continuous mixer was about 18.7% by weight, based upon the total weight of the dough-like mixture. At steady state, the barrel set temperatures and the actual barrel temperatures for the cooker extruder were: Barrel Set Actual Barrel Barrel # Temperature, Temperature, "F 1 cool 2 300 281 3 300 4 300 293 5 300 299 6 300 7 300 301 8 300 300 9 300 10 300 305 11 300 12 300 300 Tap water was passed through the cooling jackets of the continuous mixer to cool the heat treated mass from the extruder while admixing it with the other ingredients fed to the continuous mixer. The pressure in the extruder and in the continuous mixer was less than about 10 bars. The material temperatures in the extruder were about 250 β F at barrel 3, about 240 β F at barrel 5, and about 283 β F at barrel 11. The average or median residence time of the ingredients heated in the cooker extruder was about 60- 90 seconds. The average or median residence time of the ingredients in the continuous mixer from the second feed ports was about 90 to 150 seconds. The heat treated mass formed in the cooker extruder was extruded without a die and resulted in a slurry-like substantially homogeneous heat treated mass. The heat treated mass was permitted to fall into the second dry ingredient feed port (the upstream end of the continuous mixer) . The substantially homogeneous dough-like mixture formed in the continuous mixer was extruded from the mixer without a die and resulted in a substantially unleavened extrudate. The dough-like mixture was immediately transferred to an auger fed wire-cutting machine and was cut into pieces while hot. The diameter of the pieces was about 1 inch. Six pieces were subjected to microwaving in a microwave oven for about 50 seconds to produce distinctly leavened cookies. The cookies were surface browned and had a crumb-like structure and crumb-like texture. EXAMPLE 15 Cookies having a crumb-like structure and texture were produced as in Example 14 except: after wire cutting, the pieces were subjected to heating in a continuous 12 kw dielectric radio frequency (27 MHz) oven for about 66 seconds to produce distinctly leavened, surface browned cookies.

Claims: What is claimed is: 1. A method for the production of cookies comprising: a) heating ingredients comprising flour, and shortening or fat in a cooker extruder to form a heat treated mass, b) reducing the temperature of said heat treated mass, c) admixing water with the heat treated mass to Obtain a substantially homogeneous cookie dough-like mixture having a temperature of from about 100 β F to about 212"F, d) forming the dough-like mixture into pieces, and e) leavening the pieces, the water being admixed with said heat-treated mass at a pressure and at a heat treated mass temperature which are sufficiently low so as to avoid substantial separation of oil and to avoid extruder surging. 2. A method as claimed in claim 1 wherein said ingredients are heated in said cooker extruder to a temperature of at least about 200°F to form said heat treated mass. 3. A method as claimed in claim 2 wherein said heat treated mass is cooled in a post extrusion mixer to a temperature of less than about 150°F so as to avoid substantial separation of oil and to avoid extruder surging. 4. A method as claimed in claim 1 wherein the water content of said dough-like mixture is less than about 15% by weight, based upon the weight of the dough-like mixture. 5. A method as claimed in claim 1 wherein the shortening or fat content of said dough-like mixture is at least about 12% by weight, based upon the weight of the dough-like mixture. 6. A method as claimed in claim 1 wherein the sugar content of said dough-like mixture is at least about 10% by weight crystalline sugar, based upon the weight of the dough-like mixture. 7. A method as claimed in claim 6 wherein said crystalline sugar comprises sucrose. 8. A method as claimed in claim 7 wherein at least one reducing sugar is admixed with said ingredients comprising flour in an amount which promotes Maillard browning. 9. A method as claimed in claim 1 wherein at least one protein source is admixed with said ingredients comprising flour in an amount which promotes Maillard browning. 10. A method as claimed in claim 1 wherein said dough¬ like mixture comprises: a) less than about 20% by weight water, b) from about 12% by weight to about 40% by weight shortening or fat, c) from about 10% by weight to about 40% by weight of at least one sugar, and d) from about 30% by weight to about 70% by weight of at least one flour, said percentages being based upon the weight of said dough-like mixture. 11. A method as claimed in claim 1 wherein said heat treated mass is formed at a pressure within the cooker extruder of less than about 10 bars absolute. 12. A method as claimed in claim 11 wherein the average residence time of said ingredients comprising flour at a temperature of at least about 200°F in said cooker extruder is from about 15 seconds to about 120 seconds. 13. A method as claimed in claim 12 wherein the heat treated mass is admixed with water in a post extrusion mixer and the average residence time of the ingredients in the post extrusion mixer from the point of addition of the added water to the heat treated mass is from about 60 seconds to about 120 seconds. 14. A method as claimed in claim 3 wherein said heat treated mass is cooled to a temperature of less than about 150 β F prior to addition of said water. 15. A method as claimed in claim 1 wherein the temperature of said heat treated mass is reduced by at least about 35°F prior to said addition of the water to the heat treated mass. 16. A method as claimed in claim 6 wherein at least a portion of said sugar is admixed with the flour and shortening or fat prior to said addition of the water to the heat treated mass. 17. A method as claimed in claim 6 wherein at least a portion of said sugar is subjected to said heating for forming said heat treated mass. 18. A method as claimed in claim 6 wherein at least a portion of said sugar is admixed with the heat treated mass after reducing the temperature of the heat treated mass. 19. A method as claimed in claim 6 wherein at least a portion of said sugar and the water are admixed with said heat-treated mass at a pressure and at a heat treated mass temperature which are sufficiently low so as to avoid substantial separation of oil and to avoid extruder surging. 20. A method as claimed in claim 1 wherein the amount of water admixed with said heat treated mass is from about 0.5% by weight to about 10% by weight, based upon the weight of the dough-like mixture. 21. A method as claimed in claim 20 wherein the water admixed with the heat treated mass comprises a liquid source of water selected from the group consisting of high fructose corn syrup, corn syrup, sucrose syrup, and mixtures thereof. 22. A method for the production of cookies comprising: a) heating ingredients comprising flour, and shortening or fat in a cooker extruder to a temperature of at least about 150 β F to form a heat treated mass, b) admixing water with the heat treated mass at a heat treated mass temperature of from about 100"F to about 300"F to obtain a substantially homogeneous cookie dough-like mixture, d) forming the dough-like mixture into pieces, and e) leavening the pieces in a post extrusion heater, the water being admixed with said heat-treated mass at a pressure and at a heat treated mass temperature which are sufficiently low so as to avoid substantial separation of oil and to avoid extruder surging. 23. A method as claimed in claim 22 wherein the water content of the dough-like mixture is such that additional water will increase the consistency of the dough-like mixture. 24. A method as claimed in claim 22 wherein said ingredients are heated in said cooker extruder to a temperature of at least about 250 β F to form said heat treated mass. 25. A method as claimed in claim 22 wherein said ingredients are heated in said cooker extruder to a temperature of from about 300 β F to about 500°F to form said heat treated mass. 26. A method for the production of cookies comprising: a) forming a dough-like mixture from ingredients comprising flour, water, at least one sugar, and shortening or fat wherein at least the flour and shortening or fat are heated to a temperature of at least about 150°F in a cooker extruder, b) extruding the dough-like mixture from a post- extrusion mixing device at a temperature of from about 100"F to about 212 β F, and c) leavening the pieces in a post extrusion heater. 27. A method as claimed in claim 26 wherein the water content of the dough-like mixture is such that additional water will increase the consistency of the dough-like mixture. 28. A method as claimed in claim 26 wherein said ingredients are heated in said cooker extruder to a temperature of at least about 250"F. 29. A method as claimed in claim 26 wherein said ingredients are heated in said cooker extruder to a temperature of from about 300"F to about 500 β F. 30. A method as claimed in claim 27 wherein said ingredients subjected to said heating in the cooker extruder includes added water. 31. A method as claimed in claim 26 wherein said dough¬ like mixture is coextruded with a filler material. 32. A method for producing leavened products comprising: a) forming a substantially homogeneous dough-like mixture by heating ingredients comprising at least one flour and shortening or fat to a temperature of at least about 150 β F while mixing them under conditions to prevent substantial starch gelatinization, the amount of shortening or fat being at least about 12% by weight, based upon the weight of the dough¬ like mixture, b) extruding the dough-like mixture at a temperature of from about 100 β F to about 212 β F, c) forming the extrudate into pieces, and d) leavening the pieces by subjecting them to post extrusion heating. 33. A method as claimed in claim 32 wherein said ingredients are heated to a temperature of at least about 200 β F to form a heat treated mass and water is admixed with the heat treated mass to obtain said dough¬ like mixture. 34. A method as claimed in claim 33 wherein said heat treated mass is cooled to a temperature of less than about 150"F. 35. A method as claimed in claim 33 wherein at least one sugar is subjected to said heating for forming said heat treated mass. 36. A method for the production of leavened products comprising: a) heating ingredients comprising flour, and " shortening or fat to a temperature of at least about 150°F while mixing them to form a heat treated mass, b) admixing water and a chemical leavening agent with the heat treated mass at a heat treated mass temperature of from about 100°F to about 300°F to obtain a substantially homogeneous dough-like mixture, c) extruding the dough-like mixture at a temperature of from about 100 β F to about 212 β F, and, d) leavening the dough-like mixture in a post extrusion heater. 37. A method as claimed in claim 36 wherein the water content of the dough-like mixture is such that additional water will increase the consistency of the dough-like mixture. 38. A method as claimed in claim 36 wherein said ingredients are heated to a temperature of at least about 250°F to form said heat treated mass. 39. A method as claimed in claim 36 wherein said ingredients are heated to a temperature of from about 300°F to about 500 β F to form said heat treated mass. 40. A method for the production of leavened products comprising: a) forming a dough-like mixture from ingredients comprising flour, water, a chemical leavening agent, at least one sugar, and shortening or fat wherein at least the flour and shortening or fat are mixed while being heated to a temperature of at least about 150°F, b) extruding the dough-like mixture at a temperature of from about 100 β F to about 212 β F, and c) leavening the pieces in a post extrusion heater. 41. A method as claimed in claim 40 wherein said ingredients are heated to a temperature of at least about 250 β F. 42. A method as claimed in claim 40 wherein said ingredients are heated to a temperature of from about 300°F to about 500"F. 43. A method as claimed in claim 40 wherein said ingredients subjected to said heating in the cooker extruder includes added water. 44. A method as claimed in claim 40 wherein said dough¬ like mixture is coextruded with a filler material. 45. A method for the production of leavened products comprising: a) heating and mixing ingredients comprising flour, and shortening or fat to form a heat treated mass having a temperature of at least about 150 β F, b) reducing the temperature of said heat treated mass, c) admixing water and a leavening agent with the heat treated mass to obtain a substantially homogeneous cookie dough-like mixture having a temperature of from about 100°F to about 212 β F, d) forming the dough-like mixture into pieces, and e) leavening the pieces. 46. A method as claimed in claim 45 wherein said dough-like mixture comprises: a) less than about 20% by weight water, b) from about 12% by weight to about 40% by weight shortening or fat, c) from about 10% by weight to about 40% by weight of at least one sugar, and d) from about 30% by weight to about 70% by weight of at least one flour, said percentages being based upon the weight of said dough-like mixture. 47. A method for the production of a shelf stable, leavenable cookie mixture comprising: a) admixing ingredients comprising flour and shortening or fat in a cooker extruder, b) heating said ingredients in the extruder to a temperature sufficient to promote browning and to form a heat treated mass, c) transferring the heat treated mass to a post extrusion mixing means and reducing the temperature of said heat treated mass, d) admixing at least one sugar with the heat treated mass to obtain a substantially homogeneous mixture, and e) discharging the mixture from the mixer at a temperature of from about 100"F to about 212 β F, wherein the mixture has a water activity of less than about 0.7 and is leavenable to form a crumb-like texture by heating. 48. The method as claimed in claim 47 wherein a source of water is admixed in an amount sufficient to form a dough-like mixture and wherein the total water content of said dough-like mixture is sufficiently low such that further water addition increases the consistency of the mixture and said mixture has a water activity of less than about 0.7. 49. The method as claimed in claim 47 wherein said heat treated mass is cooled in the mixing means to a temperature of less than about 150 β F. 50. A method as claimed in claim 47 wherein said dough-like mixture comprises: a) less than about 20% by weight water, b) from about 12% by weight to about 40% by weight shortening or fat, c) from about 10% by weight to about 50% by weight sugar, d) from about 30% by weight to about 70% by weight of at least one flour. said dough-like mixture having a water activity of less than about 0.7 and wherein the percentages are based upon the weight of said dough-like mixture. 51. The method of claim 48 wherein said flour and fat are heated to at least 200°F to about 500 β F for about 20 seconds to about 120 seconds to form said heat treated mass. 52. The method of claim 47 wherein at least a portion of said sugar is added to the flour and fat mass and subjected to heating in the extruder to form said heat treated mass. 53. The method of claim 47 wherein the mixture includes at least one pH-adjusting agent and said mixture has a pH of about pH 5 to about pH 9.5 54. The method of claim 47 wherein at least one edible additive is admixed with the heat treated mass with sufficient mixing to uniformly distribute the additive and to form a cookie composition. 55. The method of claim 47 wherein said heat treated mass includes a fiber source. 56. A process for making cookie dough products comprising: a) adding cookie ingredients to a cooker extruder to form a heat treated mass, b) adding the heat treated mass to a second stage mixer to form a cookie mixture, and c) forming the cookie mixture into pieces at a temperature of from about 100"F to about 150 β F. 57. A process as claimed in claim 56 wherein the cookie mixture is formed into pieces by wire cutting. 58. An apparatus for producing a product having a cookie-like crumb structure, which comprises: (a) an extruder including a housing having a screw channel formed along the longitudinal axis of the housing; (b) at least one screw-type element rotatably received within the screw channel to convey and mix ingredients; (c) a feed port means arranged in the housing adjacent the upstream end thereof to input ingredients into the screw channel for conveyance and mixing by the screw- type element; (d) means for inputting at least certain ingredients of a cookie-like dough formulation, including oil and flour. with less than a preselected total water content, by weight, of the ingredients; (e) the means for inputting being coupled to the feed port means; (f) a vigorous mixing zone formed by the screw channel and screw-type element downstream from the feed port means to vigorously mix and convey the ingredients input into the feed port means; (g) a temperature control means operating to elevate the temperature of the screw channel for heat treatment of the ingredients input into the feed port means in a heat treatment zone of the housing extending downstream from the feed port means; (h) a second state mixing apparatus including an inlet port coupled to the downstream end of the extruder housing to receive, mix and convey the heat treated ingredients conveyed through the extruder; (i) an added water inlet port arranged in the second stage mixing apparatus; (j) a source of water coupled to the added water inlet port to add a preselected amount of water through the added water inlet port to increase the water content and modify the consistency of the heat treated ingredients from the extruder input into the inlet port of the second stage mixing apparatus; (k) a mixing zone formed by the second stage mixing apparatus and operating to mix the added water throughout the heat treated ingredients under pressure and temperature conditions to avoid substantial oil separation from the heat treated ingredients and added water; and (1) an output means at the downstream most end of the second stage mixing apparatus. 59. The apparatus of claim 58 wherein the vigorous mixing zone extends for substantially the entire length of the housing. 60. The apparatus of claim 58 wherein the heat treatment zone extends for substantially the entire length of the housing. 61. The apparatus of claim 58 wherein the inlet port and added water inlet port are arranged at the upstream most end of the second stage mixing apparatus. 62. The apparatus of claim 58 wherein the second stage mixing apparatus comprises an extruder. 63. The apparatus of claim 58 further comprising a downstream dry ingredient feed port in the second stage mixing apparatus. 64. The apparatus of claim 58 wherein the screw-type element comprises a sequence of elements including, in downstream order, a shuffle kneader, an alternating sequence of screw elements and igel elements followed by an alternating sequence of screw elements and kneading block elements, the sequence of elements operating to vigorously mix and convey the ingredients input through the feed port means, prior to input of the added water in the second stage mixing apparatus, the sequence of elements together with the screw channel comprising the vigorous mixing zone. 65. The apparatus of claim 64, wherein the second stage mixing apparatus includes at least one screw-type element which comprises a sequence of elements including, in downstream order, an alternating sequence of screw elements and kneading elements to mix and convey the ingredients input into the second stage mixing apparatus at low pressure and low temperature, relative to the vigorous mixing and heat treatment zones of the extruder. 66. The apparatus of claim 58 wherein the feed port means of the extruder comprises a dry ingredient feed port adjacent to a liquid feed port. 67. The apparatus of claim 58 wherein the extruder comprises a twin-screw extruder. 68. The apparatus of claim 58 wherein the second stage mixing apparatus comprises a continuous mixer. 69. The apparatus of claim 68 wherein the continuous mixer comprises a twin screw continuous mixer. 70. The apparatus of claim 58 further comprising a means for inputting crystalline sugar coupled to the inlet feed port of the second stage mixing apparatus. 71. The apparatus of claim 70 wherein a screw-type element of the second stage mixing apparatus forms a high speed conveyance zone beneath the inlet feed port of the second stage mixing apparatus for rapid intake of the crystalline sugar into the continuous mixing apparatus. 72. The apparatus of claim 58 wherein the temperature control means comprises an electric heating element means arranged in the housing to apply heat to the screw channel. 73. The apparatus of claim 72 wherein the temperature control means further comprises a cooling water flow means arranged around the screw channel to reduce the temperature of the screw channel. 74. The apparatus of claim 73 wherein the temperature control means includes a thermostat control to selectively activate the electric heating element means and cooling water flow means to control the temperature of the screw channel. 75. A two-stage mixing apparatus which comprises: (a) a housing including a screw channel formed along the longitudinal axis of the housing; (b) at least one screw-type element rotatably received in the screw channel for conveyance and mixing of ingredients; (c) a feed port means arranged in the housing at the upstream end thereof to input ingredients into the screw channel for conveyance and mixing by the screw-type element; (d) a temperature control means operating to elevate the temperature of the screw channel along a preselected portion of the screw channel; (e) the screw-type element being configured to provide a vigorous mixing and conveying action on ingredients input through the feed port means; (f) the housing having an output means; (g) a second stage mixing apparatus coupled to the output means to receive ingredients from the housing; (h) an added water inlet port arranged in the second stage mixing apparatus; (i) a source of water coupled to the added water inlet port; and (j) the second stage mixing apparatus operating to apply a gentle mixing and conveying to the ingredients received from the housing and the added water. 76. An apparatus for producing a product having a cookie-like crumb structure, which comprises (a) an extruder including a housing having a screw channel formed along the longitudinal axis of the housing; (b) at least one screw-type element rotatably received within the screw channel to convey and mix ingredients; (c) a feed port means arranged in the housing adjacent the upstream end thereof to input ingredients into the screw channel for conveyance and mixing by the screw- type element; (d) means for inputting at least certain ingredients of a cookie-like dough formulation, including oil and flour, with less than a preselected total water content, by weight, of the ingredients; (e) the means for inputting being coupled to the feed port means; (f) a vigorous mixing zone formed by the screw channel and screw-type element downstream from the feed port means to vigorously mix and convey the ingredients input into the feed port means; (g) a temperature control means operating to elevate the temperature of the screw channel for heat treatment of the ingredients input into the feed port means in a heat treatment zone of the housing extending downstream from the feed port means. 77. The apparatus of claim 76 further comprising a means operatively coupled to the extruder for modifying the consistency of the ingredients. 78. The apparatus of claim 77 wherein the means for modifying the consistency of the ingredients comprises a source of water and a mixing apparatus to mix water from the source of water throughout the heat-treated ingredients to increase the water content and modify the consistency of the heat treated ingredients under pressure and temperature conditions to avoid substantial oil separation. 79. The apparatus of claim 58 further comprising a heat treatment device coupled to the output means of the apparatus to receive and further heat treat the ingredients output by the output means. 80. The apparatus of claim 79 wherein the heat treatment device comprises a microwave device. 81. The apparatus of claim 79 wherein the heat treatment device comprises a radio frequency device.

Inventors: VAN LENGERICH BERNHARD, WARREN CATHRYN CLARK, VAN LENGERICH, BERNHARD, WARREN, CATHRYN, CLARK
Applicants: NABISCO BRANDS INC, NABISCO BRANDS, INC.
Application year: 1990
Main classification: A21D8
IPC codes: A21B5, A21C1, A21C11, A21D8, B01F7