TECHNOLOGY FOCUS - POLYMERS - Preferred Process: In the process (P3), the wet grind food fractionation continuous process comprises providing corn kernels having a moisture content of 10-30% moisture comprising a pericorp comprising of coarse fiber, an endosperm comprising of soft starch, hard starch, protein and fine fiber, and a germ, steeping the kernels in recycled deaerated water counter current food grade processes with or without sulfur dioxide utilizing the patented LAI continuous steeping process with anaerobic conditions for control of fermentation contamination, contaminant control and conditions for water uptake for membrane conditions to reduce steeping time, where the continuous steep overflow fraction is a quality corn steep solids (CSS) for fine bio fermentation feedstock catalyst or concentrated for marketing, the internal washing of the steeped corn provides the feedstock for the fractionation of the germ, the steeped corn at 44-45% moisture is course ground to free the germ from the kernel and diluted to 16-18% moisture with recycled downstream water and fractionated from the heavier mash with a hydrocyclone process, the germ overflow can be conditioned and refined to crude, degummed or refined food grade oils and quality corn oil meal, the underflow is fine ground and used for feedstock for production of bio chemicals and products or quality feedstocks for fermentation products or fractionated for food grade starch and other starch products, and the balance of the underflow is fractionated as needed for first strike fractionation of washed starch for food and treated starch, washed starch for liquefaction to sugar food products, washed gluten for food and process products and washed fiber for dietary food product and other processed products and the bi-products of the fractionation processes, the wash water is recycled to the dry grind process along with product not used for fractionation. In the process (P3), the dry grind process comprises: providing dent corn or other cereal grains including milo and adjunct of other starch containing grain products of 10-18% moisture for course grinding; and adding all available feedstock, bi-products and wash water available from the wet grind fractionation and other adjuncts of dextrose and starch liquid adjuncts, where the blend is adjusted to 40-42% for the feedstock to bio grind process, downstream waters are used in lieu of fresh water. In the process (P3), the bio grind process comprises: providing soaked course ground corn and/or starch containing grain starch product and fractionate balance from the food grade wet grind step and liquid reprocess sugars at depressed prices or competitive prices and concentrate; preheating the 40-42 dry substance feedstock and fine grind and liquefy, with the LAI Supramyl patented liquefaction process; fractionating the fiber and protein for animal feed blending with distillers solubles and washed fiber balance for cellulosic ethanol feedstock; and blending the sugars with steep water and yeast for fermentation feedstock. In the process (P3), the LAI cellulose grind process for refining corn fiber, corn stover and/or adjunct plant materials comprises: providing a plant material comprising starch, sugar, fiber comprising cellulose, hemicellulose, lignin and pectin; heating the fiber slurry under mild alkaline conditions to hydrolyze substantially all of the hemicellulose and pectin into soluble pentose and hexose sugars and treating with polygalacturonase as needed; separating the insoluble cellulose and lignin from the pentose and dextrose sugars fermenting for ethanol with dextrose and pentose yeasts; fractionate the ethanol with pervaporation filtration and return for concentration, distillation, dehydration and fuel blending in the ethanol bio grind process; heating the slurry of cellulose and lignin under severe alkaline conditions to hydrolyze substantially all of the lignin into soluble hydrolysate for fractionation for boiler feed stocks and enzyme treating; and treating the resulting insoluble cellulose with an amount of cellulose enzyme to convert to a secondary glucose solution and adding the glucose to the secondary yeast fermenter. In the process (P3), the fermentation and ethanol refining for both starch and cellulose ethanol processes will be combined for finishing comprising: one stage full mash pentose fermenter with special enzymes and yeast to ferment xylose, arabinose and other DP2 and higher sugars available in the recycle catalyst and other feedstock, where the ethanol is partially concentrated with the pervaporation membrane filter system, the permeate filtrate is concentrated in the final continuous cascade anaerobic process, and the concentrate syrup solids are evaporated for production of animal feed with the ethanol in the condensate reclaimed in the pervaporation membrane filter system; second one stage full mash fermenter with special enzymes and yeast is used to ferment the product of high temperature cellulose hydrolysis, where the ethanol is partially concentrated with the pervaporation membrane filter system, the permeate filtrate is concentrated in the final continuous anaerobic process, and the concentrate syrup solids are evaporated for production of animal feed with the ethanol in the condensate reclaimed in the pervaporation membrane filter system; and the final continuous cascade anaerobic fermenter process with partial fine bubble mixing and blanketing with carbon dioxide is used to ferment and concentrate fermenter ethanol for refining fuel ethanol. In the process (P3), the animal feed is refined by blending bio grind pre-fermentation fractionated protein and fiber from post cellulose grind and post distillation insoluble product, comprising: fractionation product available from pre-fermentation for corn gluten meal, dry distillers grains with solubles, corn gluten feed with balance becoming feedstock for the cellulose grind; balance of product from fractionation of ethanol from cellulose ethanol fermentation is blended with the bio grind product with any remaining partially hydrolyzed cellulose returned to the cellulose grind; soluble solids available from the steam distillation are returned to pre-fermentation blending; and waters containing soluble process solids are recycled back to the dry grind for washing, wet scrubbing environmental discharges, or dilution. In the process: food fractionation and refinery has priority and wash water is concurrent recycled to processing of fuel ethanol and animal feed products; and the starch liquefied before fractionation providing a fuel ethanol from starch to 3 gallon per corn bushel equivalent and recycled catalyst for cellulosic ethanol an additional 1 gallon per equivalent corn feedstock, producing a 5% improvement over most dry grind plants, 8.5% improvement over most wet mill food refineries and 15% over cellulose refineries with no additional catalyst. The wash water used for wet grind food refining is transferred counter current for processing with no waste. In the process, the steeping utilizes 10-30% moisture corn for feedstock and requires no added sulfur dioxide, the steep operates anaerobically with no steeping fermentation loss and is designed for optimum conditions for membrane flux to optimize steeping rates and soluble fractionation yields. In the process: the food grade germ is fractionated at 50% oil; the mash after germ fractionation is partially ground to leave corn grits in lieu of fine fiber which is transferred to the dry grind process for blending and liquefaction before fractionating to produce fine fiber of less than 0.2% starch to feed the cellulose system, where first cut is only is used for low cost fractionation and refining of food products; and distressed corn and other grains and grain products are used to supplement food grade fractionated products for ethanol liquefaction for reduced cost for solids control and starch liquefaction for fuel ethanol. The process comprises the use of recycle heat and low pressure steam (5 Bar, no flashing, no vapor), low temperature (200-220 degrees F), reduced steam and enzyme and less evaporation due to processing at 15% higher than typical jet systems, less retrogradation, color and by-products (Mail-lard reaction) and viscosity reduced internally for low viscosity discharge for ease of fractionation, where all of the by-product are used for quality animal feed or recycled or for re-processing. EXAMPLE - No suitable example given.