TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Process: (I) is pressure filtered through a plurality of spiral-wound filtration assemblies comprising: ultrafiltration, nanofiltration and reverse osmosis. The concentrate from the assemblies is conveyed to a completely stirred tank reactor (CSTR). The first pressure filtration inlet is 20-40 bar with a predetermined membrane cut off from 700-10000 Daltons and the concentrate is collected and the permeate is pressurized into a filtration inlet of reverse osmosis at 20-50 bar to collect its concentrate above its predetermined molecular weight cutoff from 50-100 Daltons. (I) is pasteurized and sterile and pressure filtered at 40-80 degreesC, and the concentrate is conveyed to anaerobic digestion at 30-70 degreesC. The filters for pressure filtration are of a polyamide type when temperatures of filtration are greater than 65 degreesC. The concentrate is withdrawn at predetermined volumes to maintain concentrations at a predetermined level of 10-25 wt. % of total solids and conveyed to a completely stirred tank reactor anaerobic digester. The withdrawn concentrate is diluted to the original wt. % of total solids in (I) to convey to an anaerobic digester. (I) is discharged pasteurized and pressure filtered through a plurality of spiral-wound filtration assemblies comprising ultrafiltration, nanofiltration and reverse osmosis and the final permeate from the assemblies is a water suitable for drinking. The permeate from ultrafiltration or nanofiltration is adjusted with an alkali including aqueous ammonia solution recovered from anaerobic digester denitrification to a predetermined pH of 4-7.5. The discharge is pasteurized and sterile and pressure filtered at 40-80 degreesC and a predetermined volume of the permeate less than 10000 and not less than 700 Daltons cutoff is conveyed to a process comprising anaerobic digestion and beverage water recovery. The final permeate is cooled in a heat exchanger and the exchanged heat recovered to the process. The final permeate water is polished by a predetermined process consisting of activated carbon filtration, vacuum degasification and aeration. The concentrate stream to the anaerobic digester is adjusted to a predetermined temperature of 30-70 degreesC and total solids concentration to a predetermined level of 10-25 % total solids by steps consisting of dilution with water consisting of fresh water; recycled water from the anaerobic digester discharge; concentration with solids consisting of thin or thick stillage; and recycled solids from the anaerobic digester discharge. The anaerobic digester is operated at a predetermined temperature of 30-65 degreesC with methane gas recovered as fuel. The anaerobic digester discharge is separated into liquid and solid fractions by a centrifugal decanter and the liquid fraction conveyed to a nanofiltration unit and solid fraction returned at a predetermined amount to the inlet to the anaerobic digester. The permeate from the liquid fraction conveyed to the nanofiltration unit is treated for ammonia removal by denitrification and the denitrified permeate returned at a predetermined volume to the inlet of the anaerobic digester. The aqueous ammonia solution from denitrification is returned to the process as nutrient to culture yeast or adjust the pH of permeate before reverse osmosis.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: (I) is pressure filtered through a plurality of spiral-wound filtration assemblies comprising: ultrafiltration, nanofiltration and reverse osmosis. The concentrate from the assemblies is conveyed to a completely stirred tank reactor (CSTR). The first pressure filtration inlet is 20-40 bar with a predetermined membrane cut off from 700-10000 Daltons and the concentrate is collected and the permeate is pressurized into a filtration inlet of reverse osmosis at 20-50 bar to collect its concentrate above its predetermined molecular weight cutoff from 50-100 Daltons. (I) is pasteurized and sterile and pressure filtered at 40-80 degreesC, and the concentrate is conveyed to anaerobic digestion at 30-70 degreesC. The filters for pressure filtration are of a polyamide type when temperatures of filtration are greater than 65 degreesC. The concentrate is withdrawn at predetermined volumes to maintain concentrations at a predetermined level of 10-25 wt. % of total solids and conveyed to a completely stirred tank reactor anaerobic digester. The withdrawn concentrate is diluted to the original wt. % of total solids in (I) to convey to an anaerobic digester. (I) is discharged pasteurized and pressure filtered through a plurality of spiral-wound filtration assemblies comprising ultrafiltration, nanofiltration and reverse osmosis and the final permeate from the assemblies is a water suitable for drinking. The permeate from ultrafiltration or nanofiltration is adjusted with an alkali including aqueous ammonia solution recovered from anaerobic digester denitrification to a predetermined pH of 4-7.5. The discharge is pasteurized and sterile and pressure filtered at 40-80 degreesC and a predetermined volume of the permeate less than 10000 and not less than 700 Daltons cutoff is conveyed to a process comprising anaerobic digestion and beverage water recovery. The final permeate is cooled in a heat exchanger and the exchanged heat recovered to the process. The final permeate water is polished by a predetermined process consisting of activated carbon filtration, vacuum degasification and aeration. The concentrate stream to the anaerobic digester is adjusted to a predetermined temperature of 30-70 degreesC and total solids concentration to a predetermined level of 10-25 % total solids by steps consisting of dilution with water consisting of fresh water; recycled water from the anaerobic digester discharge; concentration with solids consisting of thin or thick stillage; and recycled solids from the anaerobic digester discharge. The anaerobic digester is operated at a predetermined temperature of 30-65 degreesC with methane gas recovered as fuel. The anaerobic digester discharge is separated into liquid and solid fractions by a centrifugal decanter and the liquid fraction conveyed to a nanofiltration unit and solid fraction returned at a predetermined amount to the inlet to the anaerobic digester. The permeate from the liquid fraction conveyed to the nanofiltration unit is treated for ammonia removal by denitrification and the denitrified permeate returned at a predetermined volume to the inlet of the anaerobic digester. The aqueous ammonia solution from denitrification is returned to the process as nutrient to culture yeast or adjust the pH of permeate before reverse osmosis.