阅读说明：本技术 用于提高废水流出物和生物固体的质量的系统、方法和设备 (Systems, methods, and apparatus for improving the quality of wastewater effluents and biosolids ) 是由 M·斯科特·康利 马克·梅内德斯 于 2018-02-27 设计创作，主要内容包括：递送负载在无机多孔介质上的微生物的方法。处理废水以提高流出物和生物固体质量的方法。减少氨和使废水流出物反硝化的方法。降低废水流出物中的磷浓度的方法。源自废水处理的生物固体的组合物。用于提高废水流出物和生物固体质量的废水处理组装。(A method of delivering a microorganism supported on an inorganic porous medium. A method of treating wastewater to improve effluent and biosolids quality. A process for reducing ammonia and denitrifying a wastewater effluent. A method for reducing the concentration of phosphorus in a wastewater effluent. A composition of biosolids derived from wastewater treatment. A wastewater treatment assembly for enhancing the quality of wastewater effluents and biosolids.)

1. A method of producing fertilizer or compost comprising:

a) providing a microbial solution comprising at least one microbial species supported on an inorganic porous medium;

b) providing a reaction vessel comprising an influent stream, an effluent stream, an aqueous phase, and a biosolids phase, wherein the biosolids phase comprises at least one nutrient source for the at least one microbial species;

c) adding the microbial solution comprising the at least one microbial species supported on the inorganic porous media to the reaction vessel, wherein the at least one microbial species consumes a portion of the biosolids phase;

d) separating the effluent stream into a treated aqueous phase and a treated biosolids phase; and

e) dehydrating the treated biosolid phase to produce the fertilizer or compost.

2. The method of claim 1, wherein the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

3. The method of any one of claims 1 or 2, wherein the at least one microbial species is aerobic.

4. The method of any one of claims 1 or 2, wherein the at least one species of microorganism is anaerobic.

5. The method of any one of claims 1 or 2, wherein the at least one species of microorganism is facultative.

6. The method of any one of claims 1 or 2, wherein the influent stream comprises residential wastewater, agricultural wastewater, industrial wastewater, runoff wastewater, or any combination thereof.

7. The method of any one of claims 1 or 2, wherein adding the microbial solution comprising the at least one species of microbe supported on the inorganic porous media to the reaction vessel reduces the amount of the biosolid phase.

8. The method of any one of claims 1 or 2, wherein adding the microorganism solution comprising the at least one species of microorganism supported on the inorganic porous medium to the reaction vessel increases the carrying capacity of the reaction vessel.

9. The method of any one of claims 1 or 2, wherein separating the discharged stream into the treated aqueous phase and the treated biosolids phase comprises decanting, filtering, centrifuging, or any combination thereof.

10. The method of any one of claims 1 or 2, wherein dewatering the treated biosolids phase comprises centrifugation or filtration.

11. The method of any one of claims 1 or 2, wherein the treated biosolid phase comprises less than about 3 Maximum Probability Number (MPN) salmonella enterica species per 4 grams of solids on a dry matter basis.

12. The method of any one of claims 1 or 2 wherein the treated biosolid phase comprises less than about 1000MPN fecal coliform bacteria per gram total solids on a dry basis.

13. The method of any one of claims 1 or 2, wherein the treated biosolid phase comprises less than about 1 Plaque Forming Unit (PFU) enterovirus per 4 grams total solids on a dry basis.

14. The method of any one of claims 1 or 2, wherein the treated biosolid phase comprises less than about 1 viable worm egg per 4 grams total solids on a dry matter basis, wherein the support adsorbs a standard oxygen uptake of less than about 1.5 milligrams oxygen per gram solids per hour.

15. The method of any one of claims 1 or 2, wherein the treated biosolids phase comprises less than about 41ppm arsenic, less than about 39ppm cadmium, less than about 1,200ppm chromium, less than about 1,500ppm copper, less than about 300ppm lead, less than about 17ppm mercury, less than about 420ppm nickel, less than about 36ppm selenium, and less than about 2,800ppm zinc.

16. The method of any one of claims 1 or 2, wherein the inorganic porous media is selected or modified to adsorb nitrogen and/or phosphorus from the aqueous phase to (i) increase the nutrient concentration of the fertilizer or compost and (ii) reduce the amount of nitrogen and/or phosphorus in the aqueous phase.

17. The process of any one of claims 1 or 2, wherein (i) the solids retention time in the reaction vessel is increased by greater than or equal to about 50%, and/or (ii) the amount of treated biosolid phase is reduced by greater than or equal to 5% while the solids retention time remains constant.

18. A fertilizer or compost produced by the method of any of claims 1-17.

19. A method of producing fertilizer or compost from a wastewater treatment plant, the method comprising:

a) providing a microbial solution comprising at least one microbial species supported on an inorganic porous medium;

b) providing an aeration tank comprising an influent stream, an effluent stream, an aqueous phase, and a biosolids phase, wherein the biosolids phase comprises at least one nutrient source for the at least one microbial species;

c) adding the microbial solution comprising the at least one microbial species supported on the inorganic porous media to the aeration basin, wherein the at least one microbial species consumes a portion of the biosolids phase;

d) separating the effluent stream into a treated aqueous phase and a treated biosolids phase;

e) returning the amount of the treated biosolids phase to the aeration tank, wherein the treated biosolids phase is further consumed by the at least one species of microorganism, and wherein the amount of the treated biosolids phase is reduced;

f) digesting the treated biosolids phase in a digester to produce a digested biosolids phase; and

g) dehydrating the digested biosolids phase to produce a fertilizer or compost.

20. The method of claim 19, wherein the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

21. A process according to any one of claims 19 or 20, wherein the at least one microbial species is aerobic.

22. The method of any one of claims 19 or 20, wherein the at least one species of microorganism is anaerobic.

23. The method of any one of claims 19 or 20, wherein the at least one species of microorganism is facultative.

24. The method of any one of claims 19 or 20, wherein the influent stream comprises residential wastewater, agricultural wastewater, industrial wastewater, runoff wastewater, or any combination thereof.

25. The method of any one of claims 19 or 20, wherein adding the microbial solution comprising the at least one species of microbes supported on the inorganic porous media to the aeration basin reduces the amount of the treated biosolids phase.

26. The method according to any one of claims 19 or 20, wherein adding the microbial solution comprising the at least one species of microorganisms supported on the inorganic porous media to the aeration tank increases the load carrying capacity of the aeration tank.

27. The method of any one of claims 19 or 20, wherein separating the discharged stream into the treated aqueous phase and the treated biosolids phase comprises decanting, filtering, centrifuging, or any combination thereof.

28. The method of any one of claims 19 or 20, wherein dewatering the digested biosolids phase comprises centrifugation or filtration.

29. The method of any one of claims 19 or 20, wherein the digested biosolids phase comprises less than about 3 Most Probable Number (MPN) of salmonella enterica species per 4 grams of solids on a dry matter basis.

30. The method of any one of claims 19 or 20 wherein the digested biosolid phase comprises less than about 1000MPN fecal coliform per gram total solids on a dry basis.

31. The method of any one of claims 19 or 20, wherein the digested biosolids phase comprises less than about 1 Plaque Forming Unit (PFU) enterovirus per 4 grams total solids on a dry basis.

32. The method of any one of claims 19 or 20, wherein the digested biosolids phase comprises less than about 1 viable worm egg per 4 grams total solids on a dry matter basis, wherein the support adsorbs a standard oxygen uptake of less than about 1.5 milligrams oxygen per gram solids per hour.

33. The method of any one of claims 19 or 20, wherein the digested biosolids phase comprises less than about 41ppm arsenic, less than about 39ppm cadmium, less than about 1,200ppm chromium, less than about 1,500ppm copper, less than about 300ppm lead, less than about 17ppm mercury, less than about 420ppm nickel, less than about 36ppm selenium, and less than about 2,800ppm zinc.

34. The method of any one of claims 19 or 20, wherein the inorganic porous media is selected or modified to adsorb nitrogen and/or phosphorus from the aqueous phase to (i) increase the nutrient concentration of the fertilizer or compost and (ii) reduce the amount of nitrogen and/or phosphorus in the aqueous phase.

35. The method of any one of claims 19 or 20, wherein (i) the solids retention time of the wastewater treatment plant is increased by greater than or equal to about 50%, and/or (ii) the amount of treated biosolid phase is reduced by greater than or equal to 5% while the solids retention time remains constant.

36. A fertiliser or compost produced by the method of any of claims 19 to 35.

37. A wastewater treatment facility implementing the method of any one of claims 19-35.

38. A solid fertiliser or composted composition comprising: (i) dehydrated biosolids and (ii) at least about 500ppm of inorganic porous media on a dry basis; and wherein the composition is characterized by at least one of the following five properties: an analytical composition comprising less than about 41ppm arsenic, less than about 39ppm cadmium, less than about 1,200ppm chromium, less than about 1,500ppm copper, less than about 300ppm lead, less than about 17ppm mercury, less than about 420ppm nickel, less than about 36ppm selenium, and less than about 2,800ppm zinc; a concentration of Salmonella enterica species less than about 3 Maximum Probability Number (MPN)/4 grams total solids on a dry basis; a total fecal coliform bacteria concentration of less than about 1000MPN per gram total solids on a dry basis; a density of enterovirus of less than about 1 Plaque Forming Unit (PFU)/4 grams total solids on a dry basis; or a density of viable worm eggs of less than about 1 per 4 grams total solids on a dry basis, wherein the carrier has an adsorption standard oxygen uptake of less than about 1.5 milligrams oxygen per gram solids per hour.

39. The composition of claim 38, wherein the biosolids do not originate from a wastewater treatment plant.

40. The composition of claim 38, wherein the biosolids originate from a wastewater treatment plant.

41. The composition of any one of claims 38-40, wherein the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

42. The composition of any one of claims 38-41, wherein the enteroviruses comprise human astrovirus, human adenovirus, norovirus, human Saporovirus, human parvovirus, non-polio enterovirus, and human rotavirus.

43. The composition of any one of claims 38-41, wherein the composition comprises: an analytical composition containing less than about 41ppm arsenic, less than about 39ppm cadmium, less than about 1,200ppm chromium, less than about 1,500ppm copper, less than about 300ppm lead, less than about 17ppm mercury, less than about 420ppm nickel, less than about 36ppm selenium, and less than about 2,800ppm zinc; a concentration of Salmonella enterica species less than about 3 Maximum Probability Number (MPN)/4 grams total solids on a dry basis; a total fecal coliform bacteria concentration of less than about 1000MPN per gram total solids on a dry basis; a density of enterovirus of less than about 1 Plaque Forming Unit (PFU)/4 grams total solids on a dry basis; and a density of viable worm eggs of less than about 1 per 4 grams total solids on a dry basis, wherein the standard oxygen uptake rate of the carrier is less than 1.5 milligrams oxygen per gram solids per hour.

44. A wastewater treatment facility producing the composition of any of claims 38-43.

45. A method of reducing ammonia and/or denitrifying wastewater, comprising:

a) providing a microbial solution comprising at least one microbial species supported on an inorganic porous medium;

b) providing an aeration tank comprising an influent stream, an effluent stream, and an aqueous phase, wherein the aqueous phase comprises ammonia; and

c) adding the microbial solution comprising the at least one microbial species supported on the inorganic porous medium to the aeration basin, wherein the at least one microbial species consumes the ammonia to produce nitrites, nitrates, molecular nitrogen, or any combination thereof, and thereby reduces the amount of the ammonia and/or denitrifying the wastewater.

46. The method of claim 45, wherein the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

47. A process as claimed in any one of claims 45 or 46, wherein said at least one microbial species is aerobic.

48. The method of any one of claims 45 or 46, wherein the at least one species of microorganism is anaerobic.

49. The method of any one of claims 45 or 46, wherein the at least one species of microorganism is facultative.

50. The method of any one of claims 45 or 46, wherein reducing ammonia does not necessitate the use of chlorinators, ozone, peroxides, bleaches, or ultra-violet light.

51. The method of any one of claims 45 or 46, wherein the inorganic porous media is selected or modified to adsorb nitrogen from the aqueous phase to (i) increase nutrient concentration of a solid phase and (ii) reduce the amount of nitrogen in the aqueous phase.

52. An effluent produced using the method of any one of claims 45-51.

53. A wastewater treatment facility implementing the method of any one of claims 45-51.

54. A method of reducing phosphorus in wastewater comprising:

a) providing a microbial solution comprising at least one microbial species supported on an inorganic porous medium;

b) providing an aeration basin comprising an influent stream, an effluent stream, and an aqueous phase, wherein the aqueous phase comprises an aqueous inorganic and organic phosphorus solution; and

c) adding the microbial solution comprising the at least one microbial species supported on the inorganic porous medium to the aeration tank, wherein the at least one microbial species depletes the inorganic and organophosphorus aqueous solutions to reduce the amount of the inorganic and organophosphorus aqueous solutions and prevent eutrophication.

55. The method of claim 54, wherein the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

56. A process as claimed in any one of claims 54 or 55, wherein said at least one microbial species is aerobic.

57. The method of any one of claims 54 or 55, wherein the at least one species of microorganism is anaerobic.

58. The method of any one of claims 54 or 55, wherein the at least one species of microorganism is facultative.

59. The method of any one of claims 54 or 55 wherein reducing the amount of the aqueous inorganic and organophosphorus solutions eliminates the need for addition of iron or alumina compounds.

60. The method of any one of claims 54 or 55 wherein reducing the amount of the aqueous inorganic and organophosphorus solutions eliminates the need for the addition of magnesium chloride or magnesium hydroxide.

61. The method of any one of claims 54 or 55, wherein the inorganic porous media is selected or modified to adsorb the aqueous inorganic and organophosphorus solutions from the aqueous phase to (i) increase the nutrient concentration of the solid phase and (ii) reduce the amount of the aqueous inorganic and organophosphorus solutions in the aqueous phase.

62. An effluent produced by the method of any one of claims 54-61.

63. A wastewater treatment facility implementing the method of any one of claims 54-61.

64. An assembly for treating wastewater, comprising:

an inlet stream comprising an aqueous phase and a biosolids phase;

a reaction vessel comprising at least one feed stream, at least one draw stream, and a microbial solution comprising at least one microbial species supported on an inorganic porous medium; and

a separator comprising at least one feed stream and at least one draw stream, and wherein the separator separates the aqueous phase from the biosolids phase.

65. The assembly of claim 64, wherein the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

66. The assembly of any one of claims 64 or 65, wherein the at least one microbial species is aerobic.

67. The assembly of any one of claims 64 or 65, wherein the at least one species of microorganism is anaerobic.

68. The assembly of any one of claims 64 or 65, wherein the at least one species of microorganism is facultative.

69. The assembly of any one of claims 64 or 65, wherein the assembly does not include a chlorinator.

70. The assembly of any one of claims 64 or 65, wherein the assembly does not include an ozone generator.

71. The assembly of any one of claims 64 or 65, wherein the influent stream comprises residential wastewater, agricultural wastewater, industrial wastewater, runoff wastewater, or any combination thereof.

72. The assembly of any one of claims 64 or 65, wherein adding the microorganism solution comprising the at least one species of microorganism to the reaction vessel reduces the number of biosolids phase.

73. The assembly of any one of claims 64 or 65, wherein the separator comprises a decanter, a filter, a centrifuge, or any combination thereof.

74. The assembly of any one of claims 64 or 65, wherein the reaction vessel comprises an aeration basin, lagoon, oxidation ditch, extended aeration, traditional activated sludge, membrane bioreactor, moving bed biofilm reactor, integrated fixed membrane activated sludge, trickle bed reactor, sequential batch reactor, complete mixing, step-feed, modified aeration, contact stabilization, high purity oxygen reactor, Karus process, or any other reactor for microbial growth.

75. The assembly of any one of claims 64 or 65, wherein the reaction vessel is an aeration tank.

76. An assembled wastewater treatment facility comprising any of claims 64-75.

77. An assembly for treating wastewater, comprising:

an inlet stream comprising an aqueous phase and a biosolids phase;

a reaction vessel comprising at least one feed stream, at least one draw stream, and a microbial solution comprising at least one microbial species supported on an inorganic porous medium;

a separator comprising at least one feed stream and at least one draw stream, and wherein the separator separates the aqueous phase from the biosolids;

a Return Activated Sludge (RAS) line that carries a portion of the biosolids phase from the separator to the reaction vessel;

a Waste Activated Sludge (WAS) line that conveys a second portion of the biosolids phase to a dehydrator that dehydrates the biosolids phase; and

an effluent stream comprising the treated aqueous phase.

78. The assembly of claim 77, wherein the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

79. The assembly of any one of claims 77 or 78, wherein the at least one microbial species is aerobic.

80. The assembly of any one of claims 77 or 78, wherein the at least one species of microorganism is anaerobic.

81. The assembly of any one of claims 77 or 78, wherein the at least one species of microorganism is facultative.

82. The assembly of any one of claims 77 or 78, wherein the assembly does not include a chlorinator.

83. The assembly of any one of claims 77 or 78, wherein the assembly does not include an ozone generator.

84. The assembly of any one of claims 77 or 78, wherein the influent stream comprises residential wastewater, industrial wastewater, runoff wastewater, or any combination thereof.

85. The assembly of any one of claims 77 or 78, wherein adding a microbial solution comprising the at least one microbial species supported on an inorganic porous medium to the reaction vessel reduces the number of biosolid phases.

86. The assembly of any one of claims 77 or 78, wherein the separator comprises a decanter, a filter, a centrifuge, or any combination thereof.

87. The assembly of any one of claims 77 or 78, wherein the reaction vessel comprises an aeration basin, lagoon, oxidation ditch, extended aeration, traditional activated sludge, moving bed biofilm reactors, integrated fixed membrane activated sludge, trickle bed reactors, complete mixing, step feed, modified aeration, contact stabilization, high purity oxygen reactors, Karus process, or any other reactor for microbial growth.

88. The assembly of any one of claims 77 or 78, wherein the reaction vessel is an aeration tank.

89. A wastewater treatment facility comprising the assembly of any of claims 77-88.

Disclosure of Invention

Disclosed herein, in certain embodiments, is a method of producing fertilizer or compost, the method comprising: (a) providing a microbial solution comprising at least one microbial species supported on an inorganic porous medium; (b) providing a reaction vessel comprising an influent stream, an effluent stream, an aqueous phase, and a biosolids phase, and wherein the biosolids phase comprises at least one nutrient source for the at least one microbial species; (c) adding a microbial solution comprising at least one microbial species supported on the inorganic porous medium to the reaction vessel, and wherein the at least one microbial species consumes a portion of the biosolids phase; (d) separating the effluent stream into a treated aqueous phase and a treated biosolids phase; and (e) dehydrating the treated biosolids phase to produce the fertilizer or compost. In some embodiments, the inorganic porous media comprises silica. In some embodiments, the inorganic porous media comprises a zeolite. In some embodiments, the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof. In some embodiments, the at least one microbial species is aerobic. In some embodiments, the at least one species of microorganism is anaerobic. In some embodiments, the at least one species of microorganism is facultative.

In some embodiments, the influent stream comprises residential wastewater, agricultural wastewater, industrial wastewater, runoff wastewater, or any combination thereof. In some embodiments, adding a microbial solution comprising the at least one microbial species supported on the inorganic porous media to the reaction vessel reduces the amount of the treated biosolids phase. In some embodiments, adding a microbial solution comprising the at least one microbial species supported on the inorganic porous medium to the reaction vessel increases the carrying capacity of the reaction vessel. In some embodiments, separating the discharged stream into the treated aqueous phase and the treated biosolids phase comprises decanting, filtering, centrifuging, or any combination thereof. In some embodiments, dewatering the treated biosolids phase comprises centrifugation or filtration.

In some embodiments, the treated biosolid phase comprises less than about 3 Maximum Probability Number (MPN) species of Salmonella enterica (Salmonella enterica) per 4 grams of solids on a dry basis. In some embodiments, the treated biosolid phase comprises less than about 1000MPN fecal coliform bacteria per gram total solids on a dry basis. In some embodiments, the treated biosolid phase comprises less than about 1 Plaque Forming Unit (PFU) enterovirus per 4 grams total solids on a dry basis. In some embodiments, the treated biosolid phase comprises less than about 1 viable worm egg per 4 grams total solids on a dry basis, wherein the standard oxygen uptake rate of the support is less than about 1.5 milligrams oxygen per gram solids per hour. In some embodiments, the treated biosolids phase includes less than about 41ppm arsenic, less than about 39ppm cadmium, less than about 1,200ppm chromium, less than about 1,500ppm copper, less than about 300ppm lead, less than about 17ppm mercury, less than about 420ppm nickel, less than about 36ppm selenium, and less than about 2,800ppm zinc. In some embodiments, the inorganic porous medium is selected or modified to adsorb nitrogen and/or phosphorus from the aqueous phase, thereby (i) increasing the nutrient concentration of the fertilizer or compost, and (ii) decreasing the amount of nitrogen and/or phosphorus in the aqueous phase. In some embodiments, (i) the solids retention time in the reaction vessel is increased by greater than or equal to about 50%, and/or (ii) the amount of treated biosolid phase is reduced by greater than or equal to 5% while the solids retention time remains constant. In some embodiments, a fertilizer or compost is produced by the method.

Disclosed herein in certain embodiments is a method of producing fertilizer or compost from a wastewater treatment plant, the method comprising: (a) providing a microbial solution comprising at least one microbial species supported on an inorganic porous medium; (b) providing an aeration tank comprising an influent stream, an effluent stream, an aqueous phase, and a biosolids phase, and wherein the biosolids phase comprises at least one nutrient source for the at least one microbial species; (c) adding a microbial solution comprising the at least one microbial species supported on the inorganic porous media to the aeration basin, and wherein the at least one microbial species consumes a portion of the biosolids phase; (d) separating the effluent stream into a treated aqueous phase and a treated biosolids phase; (e) returning the amount of the treated biosolids phase to the aeration tank, wherein the treated biosolids phase is further consumed by the at least one species of microorganism, and wherein the amount of the treated biosolids phase is reduced; (f) digesting the treated biosolids phase in a digester to produce a digested biosolids phase; and (g) dehydrating the digested biosolids phase to produce a fertilizer or compost. In some embodiments, the inorganic porous media comprises silica. In some embodiments, the inorganic porous media comprises a zeolite. In some embodiments, the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof. In some embodiments, the at least one microbial species is aerobic. In some embodiments, the at least one species of microorganism is anaerobic. In some embodiments, the at least one species of microorganism is facultative.

In some embodiments, the influent stream comprises residential wastewater, agricultural wastewater, industrial wastewater, runoff wastewater, or any combination thereof. In some embodiments, adding a microbial solution comprising the at least one microbial species supported on the inorganic porous media to the aeration basin reduces the amount of the treated biosolids phase. In some embodiments, adding a microbial solution comprising the at least one microbial species supported on the inorganic porous media to the aeration tank increases the load bearing capacity of the aeration tank. In some embodiments, separating the discharged stream into the treated aqueous phase and the treated biosolids phase comprises decanting, filtering, centrifuging, or any combination thereof. In some embodiments, separating the discharged stream into the treated aqueous phase and the treated biosolids phase comprises decanting, filtering, centrifuging, or any combination thereof. In some embodiments, dewatering the digested biosolids phase comprises centrifugation or filtration.

In some embodiments, the digested biosolid phase comprises less than about 3 Maximum Probability Number (MPN) salmonella enterica species per 4 grams of solids on a dry basis. In some embodiments, the digested biosolid phase comprises less than about 1000MPN fecal coliform bacteria per gram total solids on a dry basis. In some embodiments, the digested biosolids phase comprises less than about 1 Plaque Forming Unit (PFU) enterovirus per 4 grams total solids on a dry basis. In some embodiments, the digested biosolid phase comprises less than about 1 live worm egg per 4 grams total solids on a dry basis, wherein the support has an adsorption standard oxygen uptake of less than about 1.5 milligrams oxygen per gram solids per hour. In some embodiments, the digested biosolids phase comprises less than about 41ppm arsenic, less than about 39ppm cadmium, less than about 1,200ppm chromium, less than about 1,500ppm copper, less than about 300ppm lead, less than about 17ppm mercury, less than about 420ppm nickel, less than about 36ppm selenium, and less than about 2,800ppm zinc. In some embodiments, the inorganic porous media is selected or modified to adsorb nitrogen and/or phosphorus from the aqueous phase to (i) increase the nutrient concentration of the fertilizer or compost and (ii) decrease the amount of nitrogen and/or phosphorus in the aqueous phase. In some embodiments, (i) the solids retention time in the reaction vessel is increased by greater than or equal to about 50%, and/or (ii) the amount of treated biosolid phase is reduced by greater than or equal to 5% while the solids retention time remains constant. In some embodiments, a fertilizer or compost is produced by the method. In some embodiments, a wastewater treatment facility implements the method.

Disclosed herein, in certain embodiments, is a composition of a solid fertilizer or compost comprising: (i) dehydrated biosolids, (ii) at least about 500ppm of inorganic porous media on a dry basis; and wherein the composition is characterized by at least one of the following five properties: an analytical composition comprising less than about 41ppm arsenic, less than about 39ppm cadmium, less than about 1,200ppm chromium, less than about 1,500ppm copper, less than about 300ppm lead, less than about 17ppm mercury, less than about 420ppm nickel, less than about 36ppm selenium, and less than about 2,800ppm zinc; a concentration of Salmonella enterica species less than about 3 Maximum Probability Number (MPN)/4 grams total solids on a dry basis; a total fecal coliform bacteria concentration of less than about 1000MPN per gram total solids on a dry basis; a density of enterovirus of less than about 1 Plaque Forming Unit (PFU)/4 grams total solids on a dry basis; or a density of viable helminth eggs of less than 1 per 4 grams total solids on a dry basis, wherein the standard oxygen uptake rate for carrier adsorption is less than 1.5 milligrams oxygen per gram solids per hour. In some embodiments, the biosolids do not originate from a wastewater treatment plant. In some embodiments, the biosolids originate from a wastewater treatment plant.

In some embodiments, the inorganic porous media comprises silica. In some embodiments, the inorganic porous media comprises a zeolite. In some embodiments, the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof. In some embodiments, the enteroviruses include human astrovirus, human adenovirus, norovirus (norovirus), human sapovirus (human sapivirus), human parvovirus, non-polio enterovirus, and human rotavirus (human rotavirus). In some embodiments, the composition comprises: an analytical composition containing less than about 41ppm arsenic, less than about 39ppm cadmium, less than about 1,200ppm chromium, less than about 1,500ppm copper, less than about 300ppm lead, less than about 17ppm mercury, less than about 420ppm nickel, less than about 36ppm selenium, and less than about 2,800ppm zinc; a concentration of Salmonella enterica species less than about 3 Maximum Probability Number (MPN)/4 grams total solids on a dry basis; a total fecal coliform bacteria concentration of less than about 1000MPN per gram total solids on a dry basis; a density of enterovirus of less than about 1 Plaque Forming Unit (PFU)/4 grams total solids on a dry basis; and a density of viable worm eggs of less than about 1 per 4 grams total solids on a dry basis, wherein the standard oxygen uptake rate of the carrier is less than 1.5 milligrams oxygen per gram solids per hour. In some embodiments, the composition is produced by a wastewater treatment facility.

Disclosed herein, in certain embodiments, is a method of reducing ammonia and/or denitrifying wastewater comprising: (a) providing a microbial solution comprising at least one microbial species supported on an inorganic porous medium; (b) providing an aeration tank comprising an influent stream, an effluent stream, and an aqueous phase, and wherein the aqueous phase comprises ammonia; and (c) adding a microbial solution comprising the at least one microbial species supported on the inorganic porous medium to the aeration basin, and wherein the at least one microbial species consumes the ammonia to produce nitrite, nitrate, molecular nitrogen, or any combination thereof, and thereby reduces the amount of ammonia and/or denitrifies the wastewater. In some embodiments, the inorganic porous media comprises silica. In some embodiments, the inorganic porous media comprises a zeolite. In some embodiments, the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

In some embodiments, the at least one microbial species is aerobic. In some embodiments, the at least one species of microorganism is anaerobic. In some embodiments, the at least one species of microorganism is facultative. In some embodiments, reducing ammonia eliminates the need for chlorinators, ozone, peroxides, bleaching agents, or ultra-violet light. In some embodiments, the inorganic porous media is selected or modified to adsorb nitrogen from the aqueous phase, thereby (i) increasing the nutrient concentration of the solid phase, and (ii) decreasing the amount of nitrogen in the aqueous phase. In some embodiments, the method is used to produce an effluent. In some embodiments, a wastewater treatment facility implements the method.

Disclosed herein, in certain embodiments, is a method of reducing phosphorus in wastewater comprising: (a) providing a microbial solution comprising at least one microbial species supported on an inorganic porous medium; (b) providing an aeration basin comprising an influent stream, an effluent stream, and an aqueous phase, and wherein the aqueous phase comprises an aqueous inorganic and organophosphorus solution; and (c) adding a microbial solution comprising the at least one microbial species supported on the inorganic porous medium to the aeration tank, and wherein the at least one microbial species consumes the inorganic and organophosphorus aqueous solutions to reduce the amount of the inorganic and organophosphorus aqueous solutions and prevent eutrophication. In some embodiments, the inorganic porous media comprises silica. In some embodiments, the inorganic porous media comprises a zeolite. In some embodiments, the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

In some embodiments, the at least one microbial species is aerobic. In some embodiments, the at least one species of microorganism is anaerobic. In some embodiments, the at least one species of microorganism is facultative. In some embodiments, reducing the amount of the inorganic and organophosphorus aqueous solutions eliminates the need for addition of iron or alumina compounds. In some embodiments, reducing the amount of the aqueous inorganic and organophosphorus solutions eliminates the need for the addition of magnesium chloride or magnesium hydroxide. In some embodiments, the inorganic porous media is selected or modified to adsorb the inorganic and organophosphorus aqueous solutions from the aqueous phase, thereby (i) increasing the nutrient concentration of the solid phase, and (ii) reducing the amount of inorganic or organophosphorus aqueous solution in the aqueous phase. In some embodiments, an effluent is produced by the method. In some embodiments, a wastewater treatment facility implements the method.

Disclosed herein, in certain embodiments, is an assembly for treating wastewater comprising: an inlet stream comprising an aqueous phase and a biosolids phase; a reaction vessel comprising at least one feed stream, at least one effluent stream, and at least one microbial species supported on an inorganic porous medium; and a separator comprising at least one feed stream and at least one draw stream, and wherein the separator separates the aqueous phase from the biosolids phase. In some embodiments, the inorganic porous media comprises silica. In some embodiments, the inorganic porous media comprises a zeolite. In some embodiments, the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

In some embodiments, the at least one microbial species is aerobic. In some embodiments, the at least one species of microorganism is anaerobic. In some embodiments, the at least one species of microorganism is facultative. In some embodiments, the assembly does not include a chlorinator. In some embodiments, the assembly does not include an ozone generator. In some embodiments, the influent stream comprises residential wastewater, agricultural wastewater, industrial wastewater, runoff wastewater, or any combination thereof. In some embodiments, adding a microorganism solution comprising the at least one species of microorganism to the reaction vessel reduces the amount of the biosolids phase. In some embodiments, the separator comprises a decanter, a filter, a centrifuge, or a combination thereof. In some embodiments, the reaction vessel comprises an aeration basin, lagoon, oxidation ditch, extended aeration, traditional activated sludge, membrane bioreactor, moving bed biofilm reactor, integrated fixed membrane activated sludge, trickle bed reactor, sequential batch reactor, complete mixing, step-feed, modified aeration, contact stabilization, high purity oxygen reactor, Karus process, or any other reactor for microbial growth. In some embodiments, the reaction vessel is an aeration tank. In some embodiments, a wastewater treatment facility includes the assembly.

Disclosed herein, in certain embodiments, is an assembly for treating wastewater comprising: an inlet stream comprising an aqueous phase and a biosolids phase; a reaction vessel comprising at least one feed stream, at least one effluent stream, and at least one microbial species supported on an inorganic porous medium; a separator comprising at least one feed stream and at least one draw stream, and wherein the separator separates the aqueous phase from the biosolids; a Return Activated Sludge (RAS) line that carries a portion of the biosolids phase from the separator to the aeration tank; a Waste Activated Sludge (WAS) line that conveys a second portion of the biosolids phase to a dehydrator that dehydrates the biosolids phase; and an effluent stream comprising the treated aqueous phase. In some embodiments, the inorganic porous media comprises silica. In some embodiments, the inorganic porous media comprises a zeolite. In some embodiments, the inorganic porous media comprises silica, zeolite, aluminosilicate, silicate, diatomaceous earth, or any combination thereof.

In some embodiments, the at least one microbial species is aerobic. In some embodiments, the at least one species of microorganism is anaerobic. In some embodiments, the at least one species of microorganism is facultative. In some embodiments, the assembly does not include a chlorinator. In some embodiments, the assembly does not include an ozone generator. In some embodiments, the influent stream comprises residential wastewater, agricultural wastewater, industrial wastewater, runoff wastewater, or any combination thereof. In some embodiments, adding a microbial solution comprising the at least one microbial species supported on an inorganic porous medium to the reaction vessel reduces the amount of the biosolid phase. In some embodiments, the separator comprises a decanter, a filter, a centrifuge, or a combination thereof. In some embodiments, the reaction vessel comprises an aeration basin, lagoon, oxidation ditch, extended aeration, traditional activated sludge, membrane bioreactor, moving bed biofilm reactor, integrated fixed membrane activated sludge, trickle bed reactor, sequential batch reactor, complete mixing, step-feed, modified aeration, contact stabilization, high purity oxygen reactor, Karus process, or any other reactor for microbial growth. In some embodiments, the reaction vessel is an aeration tank. In some embodiments, a wastewater treatment facility includes the assembly.

Drawings

The novel features believed characteristic of the invention are set forth with particularity in the appended claims. A better understanding of the features and advantages of the present invention will be obtained by reference to the following detailed description that sets forth illustrative embodiments, in which the principles of the invention are utilized, and the accompanying drawings of which:

fig. 1 shows microorganisms supported on an inorganic porous medium.

Fig. 2 shows an exemplary wastewater treatment plant for microorganism delivery and sample extraction with labeled locations.

Figure 3 shows the amount of bleach used in the test facility during the test period and the control period.

Fig. 4 shows the specific oxygen uptake rate (source) in the test facility during the test period and the control period.

Figure 5 shows the percentage of phosphate removed from raw sewage to secondary treatment effluent.

Figure 6 shows the percentage of phosphate removed from the raw sewage to the tertiary treatment in the wastewater tank.

Fig. 7 shows the total mass of gas produced by the microorganisms supported on the zeolite and the microorganisms in the liquid culture.

Fig. 8 shows the acid produced by the microorganisms supported on the zeolite and the microorganisms in the liquid culture.

Figure 9 shows the carbohydrate uptake of microorganisms loaded on zeolite and microorganisms in liquid culture.

Detailed Description

Reaction vessels are widely used in industrial processes including, but not limited to, biofuel production, water treatment, food preparation and processing, and bioproduct production. Industrial reaction vessels operate in batch mode, continuous process mode, or a combination of batch and continuous process modes. For example, in the preparation of therapeutic biological proteins, batch processing is used to obtain high titers of stable clinical products. Continuous bioprocessing is used, for example, in processes that require the continued evolution of mixed cell populations that can consume large amounts of variable feedstocks throughout the year. Continuous bioprocessing is also used, for example, to produce products that adversely affect cell growth or products that are unstable and degrade under batch processing conditions.

Water, land and energy resource management has been an urgent challenge. Process optimization in batch, continuous and mixed bioprocessing modes is therefore critical to conserve resources and to gain maximum value from current processes that utilize global resources. Process optimization includes increasing operating efficiency, increasing the load-bearing capacity of the reactor vessel system, and maximizing yield while minimizing raw material consumption and cost.

For example, water management involves the collection, treatment, and recycling of both clean water and wastewater. Wastewater treatment involves a series of processes such as simple wastewater impoundment followed by discharge of the untreated but screened wastewater stream directly into a body of Water and Wastewater Treatment Plant (WWTP) using advanced treatment reactors. The products of the treatment process are mainly clean effluent and solids in the form of sludge. Biological treatment of wastewater is achieved by growing microbial species in a continuous reactor mode under aerobic conditions. The wastewater treatment model looks at the overall growth rate without regard to the relative abundance of individual species present within the reaction vessel because it is difficult to separate and accurately classify all species present. Because of the large number of microbial species present in wastewater treatment processes, the wastewater treatment industry provides the most common example of complex mixed microbial culture interactions.

Process optimization of wastewater treatment processes includes, but is not limited to, reducing the total amount of sludge obtained or produced in the wastewater system that needs to be disposed of or post-treated after dewatering, which improves the quality of the resulting biosolids and improves the quality of the effluent. Techniques for reducing sludge in wastewater treatment systems include treatment with products containing enzyme mixtures, liquid-based microbial cultures, or nutrient-based microbial cultures. However, these techniques have been unsuccessful in reducing sludge, which consists mainly of water (typically 70-85%). Sludge disposal means transporting large amounts of water on earth every day and using land resources such as energy and fuel. Furthermore, sludge reduction means a substantial saving of water resources, as the water content can be returned to the groundwater supply instead of being evaporated, resulting in an increasingly pressing water shortage.

Key performance indicators commonly used in the WWTP industry include: mixed Liquor Suspended Solids (MLSS), Waste Activated Sludge (WAS), Volatile Suspended Solids (VSS), Total Suspended Solids (TSS), recycle ratio, Return Activated Sludge (RAS), Biological Oxygen Demand (BOD), Dissolved Oxygen (DO) level and sludge blanket height. The key performance indicators of WWTP are focused on suspended and sedimented solids. One such indicator is Solids Retention Time (SRT). If the SRT is too short, the active microorganisms or microorganisms in the log phase can be flushed out. If the SRT is too long, multicellular organisms or unwanted microorganisms become deeply rooted and adversely affect the system. Table 1 shows key performance metrics for systems employing various wastewater treatment systems. The values shown in the table are from the WWTP Operator manual (Division of Compliance assistance. Water treatment plant Operator verification Manual. Frankfort, Kentucky Department of environmental Protection,2012 obtained on 23.2.2017).

Table 1: design parameters of the activated sludge process.

Most WWTPs are designed to have a circulation ratio of 50% to 150% of the influent flow rate. A typical range of dissolved oxygen (i.e. the amount of oxygen present in the water in mg/L) is typically from 2 to 3.5mg/L in an aeration tank. In most systems, control is achieved by maintaining a constant MLSS or constant solids retention time. MLSS typically ranges from 2500 to 3500 mg/L. The solids retention time typically ranges from 10 to 20 days. The operator changes the reject rate, which is the fraction of the clarifier underflow that maintains a steady state population, measured as MLSS in the tank. The operator keeps the sludge blanket in the clarifier constant by changing the RAS or the recycle ratio, increasing the RAS flow rate as the blanket height increases, and decreasing the RAS flow rate if the blanket begins to drop.

Most of the VSS (80-90%) entering the WWTP is organic food products such as carbohydrates, lipids and proteins. A small portion of VSS entering the WWTP consists of non-biodegradable VSS (nbVSS). Into the WWTPAbout 10% of the TSS consists of inorganic materials such as metals and sludge. neither nbVSS nor inert minerals are consumed by biological activity. These solids are not the target of activated sludge treatment. Non-biodegradable solids pass through the WWTP, where most of the solids are discharged from the resulting sludge and a small amount remains suspended and is discharged at the discharge outlet as regulated by the Environmental Protection Agency (EPA). Part f of VSS generated in WWTP_dAre still "cell fragments" that are not biodegradable. This cell debris is the major part of nbVSS, which together with inert inorganic matter constitutes sludge and is discharged from the WWTP.

Total Organic Carbon (TOC) fraction (1-f) in fully biodegradable VSS_d) Leaving as carbon dioxide, wherein f_dIs a non-biodegradable part. The process of wastewater stabilization involves the oxidation of organic matter by bacteria to produce carbon dioxide and water. Thus, about 50% of the inbound BOD is converted to gas (CO) according to the following equation₂And N₂) And water. This is known as "combustion" or "conversion of matter to gas". Thus, biomass synthesis yields are typically less than 1 (unity).

In some embodiments, the yield is defined as

The yields vary widely, but the most efficient WWTPs will produce about half a ton of sludge for each ton of biodegradable material they receive. The observed yields may be greater and in some cases approach or exceed 1 (unity).

The incoming biodegradable material and RAS become nutrients for the microorganisms in the WWTP. Bacteria use nutrients for growth (replication) or for cell maintenance. The small population, which is predominantly in stationary phase, will use the nutrient to maintain cell function (catabolism). A large population, mainly in logarithmic growth, will use this nutrient to generate a larger population of cells (anabolism). Due to the limited supply of nutrients, larger populations will undergo more endogenous decay (reciprocal predation) and the decay rate per unit time increases.

By modeling the organic matter as protein casein, the BOD required for conversion of the organic matter to cellular biomass can be estimated. Casein has the chemical formula C₈H₁₂O₃N₂. The following equilibrium chemical equation (reaction 1) is the conversion of BOD and organic matter to cellular biomass:

C₈H₁₂O₃N₂+3O₂→C₅H₇O₂N+3CO₂+H₂O+NH₃

the treated biomass produced 113 grams of biomass per 184 grams of organic material. This produces a stoichiometric oxygen demand, equivalent to three moles of oxygen per mole of organic material being treated. This reaction produced approximately 0.61 grams of biomass per gram of treated organic material. In contrast, 1.42 grams of organic material was consumed per 1 gram of biomass produced. Microbial growth to produce CO₂And N₂And produces water.

The complete oxidation of biomass to carbon dioxide, water and ammonia is accurately represented by the second equilibrium chemical equation (reaction 2):

C₅H₇O₂N+5O₂→5CO₂+2H₂O+NH₃

the first reaction is substantially complete (i.e., 100% of the inbound BOD has stabilized and is converted to biomass during cell growth). However, the second reaction occurs to consume the biodegradable portion (1-f) of VSS generated in reaction 1_d) To the extent of (c). It is the second reaction that converts the VSS species to a gas, thereby further reducing the observed outbound solids yield to below the 60% biosolids yield of the above equation. The mass fraction of TOC in BOD was 96/184 or 52%, indicating that carbon represents more than 50% of the total BOD mass to be treated. Similarly, BOD contains available oxygen. The mass fraction of oxygen in BOD is 48/184 or 26%.

Carbon does not accumulate, but leaves the WWTP as a gas or sludge. The fraction of TOC in BOD leaving as gas was 36/96 or 37.5%. The balance of TOC captured in the biomass in BOD was 60/96 or 62.5%. The remaining biomass may be further reduced to gas. Almost 10% of the BOD mass entering the reactor is reduced to liquid water in the tank. A large amount of water is produced during the growth of the microorganisms. The organic nitrogen accounts for 28/184 or 15% of the BOD mass load. In reaction 1, half of the organic nitrogen is converted to molecular nitrogen by nitrification/denitrification. Including TOC and nitrogen leaving the WWTP in gaseous form, only about 45% of the total inbound organic load of the WWTP is lost in gaseous form due to the first reaction. An approximately 45% reduction in the BOD mass input indicates that only the stabilization process (reaction 1) achieves a biomass synthesis yield of around 55%. Since the resulting biomass is further oxidized and gasified by reaction 2, an improvement in the yield reduction of the process occurs. Reaction 2 describes the endogenous decay of biomass produced in WWTP. If reaction 2 is completed all of the biomass produced will be converted to gas, water and ammonia. In the case of such complete conversion, the sludge will contain only inert inorganics and inert VSS in the influent entering the WWTP. Influent streams and streams with higher inerts in the influent, which have widely different compositional characteristics, such as higher loading concentrations of BOD and Chemical Oxygen Demand (COD), may exhibit much higher biomass synthesis yields than the 50% -60% range described herein.

Disclosed herein, in certain embodiments, are compositions, methods and assemblies for improving effluent and biosolids quality in reaction vessels and wastewater treatment facilities using microbial species or consortiums (consortium) of microbial species supported on porous media.

Certain definitions

As used herein, "reaction vessel" refers to any system containing a microorganism in which a substance is transformed by the microorganism, a product is produced by the microorganism, or in which an increase in a population of cells is achieved. The reaction vessel used herein may be one or more of: single or series batch reactors, fed-batch reactors, semi-continuous reactors, continuous stirred tank reactors, continuous flow stirred tank reactors, and plug flow reactors; ebullated bed (i.e., "bubbling and boiling") reactors; and a fluidized bed reactor. In certain embodiments, the reaction vessel may be an aeration basin or an oxidation pond. In some embodiments, the reaction vessel may be one or more of: trickle bed reactors, percolation reactors, fluidized reactors, plug flow reactors, reverse flow reactors, sequential batch reactors, rotating biological contactors, oxidation channels, extended aeration, traditional activated sludge, membrane bioreactors, moving bed biofilm reactors, integrated fixed membrane activated sludge, trickle bed reactors, sequential batch reactors, complete mixing, step-wise feeding, modified aeration, contact stabilization, high purity oxygen reactors, or Karus processes.

As used herein, "wastewater treatment" refers to the process of converting contaminated water or water unsuitable for consumption by plants or animals into effluents and biosolids that can be reused for other purposes or returned to water circulation.

As used herein, the phrase "inorganic porous medium" refers to an inorganic support having a porous structure. In some embodiments, the inorganic porous media is precipitated silica particles, superabsorbent silica polymers, crystalline silica, fused silica, fumed silica, silica gel, aerogel, colloidal silica, zeolites, aluminosilicates, silicates, diatomaceous earth, or alumina. In some embodiments, the zeolite comprises andalusite, kyanite, sillimanite, analcime, chabazite, clinoptilolite, mordenite, natrolite, heulandite, phillipsite, or stilbite. In some embodiments, the inorganic porous media is a mixture of different types of inorganic porous media. In some embodiments, the porous structure is loaded with at least one species of microorganism.

As used herein, "delivered microorganism" refers to bacteria, viruses, mycoplasma, fungi, and protozoa supported on an inorganic porous medium. In some embodiments, the microorganism supported on the inorganic porous medium is a bacterium. In some embodiments, the microorganism comprises a single species of microorganism or a consortium of microorganisms. In some embodiments, the microorganism is selected based on the intended use, available nutrient sources, and the desired operating conditions of the reaction vessel.

As used herein, "carrying capacity" refers to the maximum population that a particular reaction vessel system can support. The load-bearing capacity is measured as Total Suspended Solids (TSS), Mixed Liquor Suspended Solids (MLSS) or Volatile Suspended Solids (VSS) in a continuous reactor system such as the WWTP. In some examples, the carrying capacity is measured by an increase in the rate of consumption of glucose or other sugars. In a batch reactor system, the load bearing capacity is measured by the peak population density of the microorganisms or by measuring the growth rate of the microorganisms and the consumption rate of nutrients.

Delivered microorganisms

Disclosed herein, in certain embodiments, are methods of delivering a microorganism. Figure 1 shows an inorganic porous medium with suitable microbial loading characteristics. In some embodiments, the microbial loading characteristics include, but are not limited to, loading capacity, mineral content, pore size, chemical inertness, and porosity. In some embodiments, a microbial solution comprising a single microbial species and nutrients necessary for growth of the microbial species is supported on an inorganic porous medium. In some embodiments, a microbial solution comprising a consortium of microbial species and nutrients necessary for growth of the microbial species is supported on an inorganic porous medium. In some embodiments, the addition of the microorganism solution to the inorganic porous media produces a dry-to-the-touch substance, thereby producing a dry mode for delivering the microorganisms. In some embodiments, the inorganic porous medium comprises a zeolite. In some embodiments, the zeolite includes, but is not limited to, andalusite, kyanite, sillimanite, analcime, chabazite, clinoptilolite, mordenite, natrolite, heulandite, phillipsite, or stilbite. In some embodiments, the inorganic porous media comprises an aluminosilicate, silicate, or diatomaceous earth. In some embodiments, the inorganic porous media is a mixture of different types of inorganic porous media. In some embodiments, the inorganic porous medium comprises precipitated silica particles. In some embodiments, the precipitated silica particles are highly porous and contain large surface areas both within their volume and on their surface. In some embodiments, the one pound silica particles have a surface area of about 700,000 square feet. In some embodiments, the surface area provides a substrate that can accelerate the reaction. In some embodiments, the precipitated silica particles are also superabsorbent polymers capable of absorbing organic nutrients to serve as building blocks for new bacterial cells and maintain cellular function. In some embodiments, when microorganisms reach an exponential growth phase within the inorganic porous media, they experience a crowding effect within the media and occupy the surrounding environment.

In some embodiments, the microorganism comprises a mixed culture of beneficial microorganisms. In some embodiments, the microorganisms comprise consortia of natural non-pathogenic microbial species desirable for wastewater applications. In some embodiments, the microbial species is not a genetically modified strain. In some embodiments, the microbial species belongs to group 1 of microorganisms according to the World Health Organization (WHO), wherein group 1 of microorganisms are microorganisms that are unlikely to cause disease. In some embodiments, the microorganisms supported on the inorganic porous media produce the propagation of beneficial bacteria when placed in an aqueous environment containing a nutrient source in the form of biomass or dead cells.

In some embodiments, the microorganisms supported on the inorganic porous media are delivered to a reaction vessel. In some embodiments, the microorganism, nutrients required for optimal growth, and inorganic porous medium are delivered to the reaction vessel independently. In some embodiments, the microorganisms supported on the inorganic porous media are delivered to a batch reactor. In some embodiments, the microorganisms supported on the inorganic porous media are delivered to a continuous reactor. In some embodiments, the microorganisms supported on the inorganic porous media are delivered to a mixture of batch and continuous reactors. In some embodiments, the reaction vessel is operated under aerobic or anaerobic conditions, depending on the reaction and microorganism involved. In some embodiments, the biofuels are produced using microorganisms supported on inorganic porous media, including but not limited to methanol, ethanol, or butanol. In some embodiments, biogas is produced using microorganisms supported on an inorganic porous medium. In some embodiments, wastewater treatment is enhanced with microorganisms supported on inorganic porous media. In some embodiments, the amino acid is produced using a microorganism supported on an inorganic porous medium. In some embodiments, therapeutically important peptides are produced using microorganisms supported on inorganic porous media.

Delivery of microorganisms to WWTP

Disclosed herein, in certain embodiments, are methods and compositions for the production of fertilizer or compost from a reaction vessel. In some embodiments, the microorganisms supported on the inorganic porous media are delivered to a reaction vessel. In some embodiments, the microorganism is aerobic, anaerobic, or facultative. In some embodiments, the reaction vessel comprises an influent stream, an effluent stream, an aqueous phase, and a biosolids phase. In some embodiments, the biosolid phase comprises nutrients for the microorganism. In some embodiments, the effluent stream is separated into an aqueous phase and a biosolids phase. In some embodiments, the biosolids phase is dehydrated to produce fertilizer or compost. In some embodiments, the biosolids phase is digested in a digester prior to dewatering. In some embodiments, the influent includes, but is not limited to, residential wastewater, agricultural wastewater, industrial wastewater, runoff wastewater, or any combination thereof. In some embodiments, adding the microorganism supported on an inorganic porous medium to the reaction vessel increases the load bearing capacity of the reaction vessel. In some embodiments, adding the microorganism supported on the inorganic porous medium to the reaction vessel reduces the amount of the biosolids phase. In some embodiments, separating the discharged stream into an aqueous phase and a biosolids phase includes, but is not limited to, decantation, filtration, centrifugation, or any combination thereof. In some embodiments, dewatering the biosolids phase includes centrifugation and filtration.

In some embodiments, the reaction vessel is part of a WWTP. In some embodiments, the reaction vessel is an aeration basin, pond, or lake. In some embodiments, the WWTP is modeled as a chemical stabilizer. In some embodiments, the microorganism is a bacterium. In some embodiments, the WWTP must produce as many bacteria as there are bacteria scoured in the effluent stream. In some embodiments, the washout bacteria causes a WWTP to lack beneficial bacteria. In some embodiments, the growth rate of a single microbial species within the WWTP is described by Michaelis-Menten kinetics. In some embodiments, the bacteria will grow exponentially until the food source is exhausted and aggregation occurs (growth). In some embodiments, exponential growth is log-linear and corresponds to a very short doubling time of the microbial population. In some embodiments, nutrient consumption during exponential growth is very fast. In some embodiments, the microorganism enters the stationary phase when the reaction vessel carrying capacity is reached. In some embodiments, during the stationary phase, the number of microorganisms produced is equal to the number of microorganisms consumed and the entire population remains unchanged. In some embodiments, substrate uptake corresponds to a "maintenance" need during the stationary phase. In some embodiments, the bacterial population in the WWTP consists essentially of microorganisms in the stationary phase. In some embodiments, the nutrients have been depleted and the population of microorganisms begins to die by endogenous decay. In some embodiments, endogenous decay includes cell lysis and conversion of dead cell material to nutrients for other living microorganisms. In some embodiments, the activated sludge is recycled to the aeration tank to allow dead cells to become nutrients for the young microorganisms. In some embodiments, microbial flooding supported on inorganic porous media causes greater endogenous decay of WWTPs and results in more material exiting as a gas. In some embodiments, the more microbial activity means a higher degree of water treatment.

In some embodiments, the inorganic porous media is selected or modified to adsorb nitrogen, phosphorus, or both nitrogen and phosphorus from the aqueous phase of the reaction vessel. In some embodiments, the phosphorus is an organic or inorganic phosphorus aqueous solution. In some embodiments, adsorption of nitrogen and/or phosphorus from the aqueous phase of the reaction vessel increases the nutrient concentration of the fertilizer or compost produced from the reaction vessel. In some embodiments, adsorbing nitrogen and/or phosphorus from the aqueous phase of the reaction vessel reduces the amount of nitrogen and/or phosphorus in the aqueous phase. In some embodiments, the inorganic porous media may be chemically or physically modified. In some embodiments, the chemical modification comprises the addition of a chelator, ligand, or salt (e.g., a magnesium salt), which results in the precipitation of a compound that is indicatively bound to ammonia and phosphorus. In some embodiments, the physical modification comprises roughening the surface of the porous medium, increasing the porosity of the porous medium, inducing smaller particles of the inorganic porous medium to form aggregates or agglomerates using a coagulant and a flocculant, or any combination thereof.

In some embodiments, a flocculant is added to the effluent stream to produce an aqueous phase and a filter cake. In some embodiments, the flocculant is one or more of an ionic polymer, a non-ionic polymer, or any combination thereof. In some embodiments, the ionic polymer is a cationic polymer. In some embodiments, the ionic polymer is an anionic polymer. In some embodiments, the flocculant comprises aluminum chloride, ferric chloride, and alum. In some embodiments, the cationic polymer is a copolymer of AETAC (N, N-dimethylaminoethyl acrylate methyl chloride quaternary ammonium salt) or METAC (dimethylaminoethyl methacrylate methyl chloride quaternary ammonium salt) and acrylamide. In some embodiments, flocculants perform a dual function by coagulating their cationic charge and flocculating with their high molecular weight. In some embodiments, the anionic polymer is a copolymer of acrylamide and acrylic acid. In some embodiments, the consumption of the flocculant is reduced by at least about 45% compared to a system that does not employ the delivered microorganism. In some embodiments, the consumption of flocculant is reduced by at least about 40%. In some embodiments, the consumption of flocculant is reduced by at least about 35%. In some embodiments, the consumption of flocculant is reduced by at least about 30%. In some embodiments, the consumption of flocculant is reduced by at least about 25%. In some embodiments, the amount of flocculant consumption is reduced by at least about 20%.

In some embodiments, the concentration of MLSS in the effluent is greater than about 7,000 mg/L. In some embodiments, the concentration of MLSS in the effluent is greater than about 8,000 mg/L. In some embodiments, the concentration of MLSS in the effluent is greater than about 9,000 mg/L. In some embodiments, the concentration of MLSS in the effluent is greater than about 10,000 mg/L. In some embodiments, the concentration of MLSS in the effluent is greater than about 11,000 mg/L. In some embodiments, the concentration of MLSS in the effluent is greater than about 12,000 mg/L. In some embodiments, increasing MLSS is an important measure in determining the load delivered to a solids separator (e.g., clarifier). In some embodiments, the settling characteristics of the MLSS differ from system to system. In some embodiments, the settling characteristics of MLSS determine the upper limit of the solids concentration of MLSS fed to a clarifier or other type of solid-liquid separator. In some embodiments, the solid-liquid separator surface area and the mass rate of suspended solids introduced to the clarifier are used to determine mass flux. In some embodiments, the mass flux is a process design parameter used to determine the operating size of the clarifier. In some embodiments, the higher MLSS also has higher VSS. In some embodiments, higher VSS indicates higher beneficial microbial activity in WWTP operation.

In some embodiments, the SRT is greater than twenty days. In some embodiments, the SRT is greater than thirty days. In some embodiments, the SRT is greater than forty days. In some embodiments, the SRT is greater than forty-five days. In some embodiments, the SRT of the sludge or solids is greater than fifty days. In some embodiments, the SRT is greater than sixty days. In some embodiments, the SRT increase is greater than or equal to about 1%, 2%, 5%, 10%, 20%, 25%, 30%, 40%, 50%, 60%, 70%, 80%, 90%, 100%, 150%, 200%, 250%, 300% or more when the delivered microorganism is used in a WWTP.

In some embodiments, the SRT of the solid remains constant between the WWTP where the delivered microorganism is not used and the system where the delivered microorganism is used. In some embodiments, when the SRT of the solids is kept constant, the resulting solids or sludge is reduced by greater than or equal to 2.5% compared to the same system without the delivered microorganisms. In some embodiments, when the SRT of the solids is kept constant, the resulting solids or sludge is reduced by greater than or equal to 5% compared to the same system without the delivered microorganisms. In some embodiments, when the SRT of the solids is kept constant, the resulting solids or sludge is reduced by greater than or equal to 7.5% compared to the same system without the delivered microorganisms. In some embodiments, when the SRT of the solids is kept constant, the resulting solids or sludge is reduced by greater than or equal to 10% compared to the same system without the delivered microorganisms. In some embodiments, when the SRT of the solids is kept constant, the resulting solids or sludge is reduced by greater than or equal to 15% compared to the same system without the delivered microorganisms. In some embodiments, when the SRT of the solids is kept constant, the solids or sludge produced is reduced by greater than or equal to 20% compared to the same system without the delivered microorganisms. In some embodiments, when the SRT of the solids is kept constant, the resulting solids or sludge is reduced by greater than or equal to 25% compared to the same system without the delivered microorganisms. In some embodiments, when the SRT is kept constant, the resulting solids or sludge is reduced by greater than or equal to 30% compared to the same system without the delivered microorganisms. In some embodiments, when the SRT of the solids is kept constant, the resulting solids or sludge is reduced by greater than or equal to 40% compared to the same system without the delivered microorganisms.

In some embodiments, WWTP produces at least about a 40% reduction in sludge as compared to a system that does not employ the delivered microorganisms. In some embodiments, the reduction in sludge produced by the WWTP is at least about 30%. In some embodiments, the reduction in sludge produced by the WWTP is at least about 25%. In some embodiments, the reduction in sludge produced by the WWTP is at least about 20%. In some embodiments, the reduction in sludge produced by the WWTP is at least about 15%. In some embodiments, the economic benefits of sludge reduction include savings in capital, time, reduction in human resources associated with sludge disposal, reduction in consumption of flocculants such as polymers, extended equipment life, and reduced equipment maintenance costs. In some embodiments, reducing the operating cost of the WWTP includes lower oxygen demand, higher blower efficiency, reduced qualitative and quantitative use of chemicals in sanitation facilities, and extended WWTP life. Key operating parameters of the WWTP system using the delivered microorganisms are shown in table 2.

Table 2: design parameters of the activated sludge process.

In some embodiments, the yield, as measured by the unit mass of waste product produced per unit mass of organic loading, is less than about 40%. In some embodiments, the yield is less than about 30%. In some embodiments, the yield is less than about 20%. In some embodiments, a lower yield indicates minimization or reduction of biosolids in wastewater treatment.

In some embodiments, the dehydrated biosolid phase produced upon addition of the microorganisms supported on the inorganic porous media has enhanced quality compared to the biosolid phase produced without addition of the microorganisms supported on the inorganic porous media. In some embodiments, the enhanced dewatered biosolids contain at least 1,500ppm, 1,250ppm, 1,000ppm, 750ppm, 500ppm, 250ppm, or less of inorganic porous media on a dry basis. In some embodiments, the enhanced dewatered biosolids contain at least about 500ppm of inorganic porous media on a dry basis. In some embodiments, the enhanced dewatered biosolids comprise less than about 150ppm, 125ppm, 100ppm, 75ppm, 50ppm, 25ppm, or less ppm arsenic. In some embodiments, the enhanced dewatered biosolids comprise less than about 41ppm arsenic. In some embodiments, the enhanced dewatered biosolids comprise less than about 150ppm, 125ppm, 100ppm, 75ppm, 50ppm, 25ppm, or less ppm cadmium. In some embodiments, the enhanced dewatered biosolids include less than about 39ppm cadmium. In some embodiments, the enhanced dewatered biosolids comprise less than about 2,500ppm, 2,000ppm, 1,500ppm, 1,000ppm, 500ppm, or less ppm chromium. In some embodiments, the enhanced dewatered biosolids comprise less than about 1,200ppm chromium. In some embodiments, the enhanced dewatered biosolids comprise less than about 3,000ppm, 2,500ppm, 2,000ppm, 1,500ppm, 1,000ppm, 500ppm, or less ppm copper. In some embodiments, the enhanced dewatered biosolids include less than about 1,500ppm copper. In some embodiments, the enhanced dewatered biosolids comprise less than about 1000ppm, 750ppm, 500ppm, 250ppm, or less ppm lead. In some embodiments, the enhanced dewatered biosolids include less than about 300ppm lead. In some embodiments, the enhanced dewatered biosolids comprise less than about 100ppm, 75ppm, 500ppm, 25ppm, 15ppm, or less ppm mercury. In some embodiments, the enhanced dewatered biosolids include less than about 17ppm mercury. In some embodiments, the enhanced dewatered biosolids comprise less than about 1000ppm, 500ppm, 400ppm, 300ppm, 200ppm, or less ppm nickel. In some embodiments, the enhanced dewatered biosolids include less than about 420ppm nickel. In some embodiments, the enhanced dewatered biosolids comprise less than about 150ppm, 100ppm, 75ppm, 50ppm, 25ppm, or less of selenium. In some embodiments, the enhanced dewatered biosolids comprise less than about 36ppm selenium. In some embodiments, the enhanced dewatered biosolids comprise less than about 7,500ppm, 5,000ppm, 2,500ppm, 1,000ppm, or less ppm zinc. In some embodiments, the enhanced dewatered biosolids include less than about 2,800ppm zinc.

In some embodiments, the enhanced dewatered biosolids comprise a concentration of salmonella enterica species that is less than about 10 Maximum Probability Number (MPN), 8MNP, 5MPN, 3MPN, or less. In some embodiments, the enhanced dewatered biosolids comprise less than about 3MPN of salmonella enterica species. In some embodiments, the enhanced dewatered biosolids comprise a total concentration of fecal coliform bacteria of less than about 2,000MPN, 1,500MPN, 1,250MPN, 1,000MPN, 750MPN, or less MPN. In some embodiments, the enhanced dewatered biosolids comprise fecal coliform bacteria at less than about 1000 MPN. In some embodiments, the enhanced dewatered biosolids comprise less than about 10 Plaque Forming Units (PFU), 8PFU, 4PFU, 2PFU, 1PFU, or less PFU enteroviruses per 4 grams of total solids on a dry basis. In some embodiments, the enhanced dewatered biosolids comprise less than about 1PFU of enterovirus per 4 grams of total solids on a dry basis. In some embodiments, the enteroviruses include human astrovirus, human adenovirus, norovirus, human sapovirus, human parvovirus, non-polio enterovirus, and human rotavirus. In some embodiments, the enhanced dewatered biosolids comprise less than about 10, 8, 4, 2, 1, or less viable worm eggs per 4 grams of total solids on a dry basis, and wherein the support adsorbs oxygen at a standard oxygen uptake rate of less than about 5mg, 4mg, 3mg, 1.5mg, or less mg of oxygen per gram of solids per hour. In some embodiments, the enhanced dewatered biosolids comprise less than about 1 live worm egg per 4 grams total solids on a dry basis, and wherein the carrier has an adsorption standard oxygen uptake of less than about 1.5mg oxygen per gram solids per hour.

In some embodiments, the enhanced dewatered biosolids comprise less than about 41ppm arsenic, less than about 39ppm cadmium, less than about 1,200ppm chromium, less than about 1,500ppm copper, less than about 300ppm lead, less than about 17ppm mercury, less than about 420ppm nickel, less than about 36ppm selenium, and less than about 2,800ppm zinc; a concentration of Salmonella enterica species less than about 3 Maximum Probability Number (MPN) per 4 grams total solids on a dry basis; a total fecal coliform bacteria concentration of less than about 1000MPN per gram total solids on a dry basis; a density of enterovirus of less than about 1 Plaque Forming Unit (PFU)/4 grams total solids on a dry basis; and/or a density of viable worm eggs of less than about 1 per 4 grams total solids on a dry matter basis, and wherein the carrier has an adsorption standard oxygen uptake of less than about 1.5 milligrams oxygen per gram solids per hour.

In some embodiments, the enhanced dewatered biosolids comprise no more than 41ppm arsenic, no more than 39ppm cadmium, no more than 1,200ppm chromium, no more than 1,500ppm copper, no more than 300ppm lead, no more than 17ppm mercury, no more than 420ppm nickel, no more than 36ppm selenium, and no more than 2,800ppm zinc; (ii) a concentration of Salmonella enterica species not exceeding 3 Maximum Probability Number (MPN)/4 grams total solids on a dry basis; a fecal coliform bacteria total concentration of no more than 1000MPN per gram total solids on a dry basis; (ii) a density of enterovirus not exceeding 1 Plaque Forming Unit (PFU)/4 grams total solids on a dry basis; and/or a density of viable worm eggs of no more than 1 per 4 grams total solids on a dry matter basis, and wherein the carrier adsorbs a standard oxygen uptake rate of no more than 1.5 milligrams oxygen per gram solids per hour.

In some embodiments, the effluent produced upon addition of the delivered microorganisms is of enhanced quality compared to the effluent produced without addition of the microorganisms loaded on the inorganic porous media. In some embodiments, the effluent has a reduced ammonia concentration. In some embodiments, the ammonia concentration is less than about 1mg/L, 0.75mg/L, 0.5mg/L, 0.25mg/L, 0.1mg/L, or less mg/L. In some embodiments, the ammonia concentration is less than about 0.2 mg/L. In some embodiments, the ammonia concentration is less than the analytical detection limit. In some embodiments, the reaction vessel is operated under aerobic conditions. In some embodiments, the microorganism consumes ammonia under aerobic conditions to produce nitrite and nitrate. In some embodiments, ammonia is converted to nitrite and nitrate. In some embodiments, the concentration of nitrate and nitrite is less than about 50mg/L, 40mg/L, 30mg/L, 20mg/L, 10mg/L, 5mg/L, 2.5mg/L, or less mg/L. In some embodiments, the concentration of nitrate and nitrite is in the range of about 5mg/L to 30 mg/L. In some embodiments, the effluent stream is denitrified. In some embodiments, the reaction vessel is operated under anoxic conditions. In some embodiments, the microorganism consumes nitrate and nitrite under anaerobic conditions to produce molecular nitrogen. In some embodiments, reducing ammonia and denitrification does not require chlorinators, ozone generators, or the use of peroxides, bleaching agents, or ultra-violet light is unnecessary. In some embodiments, the concentration of phosphorus in the effluent is reduced. In some embodiments, the concentration of phosphorus in the effluent is less than about 20mg/L, 10mg/L, 5mg/L, 2.5mg/L, or less mg/L. In some embodiments, the concentration of phosphorus in the effluent is less than about 3 mg/L. In some embodiments, the microorganism consumes phosphorus. In some embodiments, the consumed phosphorus is incorporated into the cellular biomass. In some embodiments, removal of soluble phosphorus reduces or prevents eutrophication. In some embodiments, phosphorus removal does not necessitate phosphate precipitation with calcium, aluminum, iron, or magnesium. In some embodiments, phosphorus removal is achieved under anaerobic conditions. In some embodiments, phosphorus removal is achieved under aerobic conditions.

WWTP Using delivered microorganisms

Disclosed herein, in certain embodiments, is an assembly for treating wastewater using delivered microorganisms. Fig. 2 shows an exemplary WWTP with exemplary locations for addition of delivered microorganisms and locations for extraction of test samples. In some embodiments, the delivered microorganisms are added to the feed stream 201 prior to the aeration tank or to the aeration tank 202. In some embodiments, the test sample is extracted from the incoming stream 210. In some embodiments, a test sample is extracted from effluent 220. In some embodiments, the test sample is extracted from the clarifier overflow 230. In some embodiments, the test sample is extracted 240 after the digester. In some embodiments, a test sample is extracted from filter cake 250. In some embodiments, the test sample is extracted from the aeration tank or after the aeration tank 260. In some embodiments, the test sample is analyzed for total volatile suspended solids, ammonia, COD, TSS, BOD, nitrate and nitrite as elemental nitrogen, phosphorus, and alkalinity. In some embodiments, total Volatile suspended solids are analyzed according to EPA Method 160.4(Environmental Protection Agency. (1971); Method 160.4: Residue, Volatile (Gravimetric, Ignition at 550 ℃) by Muffle Furnace). In some embodiments, ammonia is analyzed according to EPA Method 350.1(Environmental Protection Agency, 1993.) Method 350.1: determination of ammonia nitrogen by Semi-automatic chromatography. In some embodiments, COD is analyzed according to EPA approved method Hach 8000 provided by Hach corporation. In some embodiments, TSS is analyzed according to standard method 2540D (Eaton, A.D., Clesceri, L.S., Greenberg, A.E., Franson, M.A.H., American Public Health Association, American Water Works Association, and Water environmental Federation (2012). In some embodiments, BOD is analyzed according to standard method 5210B. In some embodiments, nitrate and nitrite are analyzed as elemental nitrogen according to EPA Method 300.0(Environmental Protection Agency, 1993.) Method 300.0: determination of organic relationships by chromatography. In some embodiments, phosphorus is analyzed by standard method 4500P. In some embodiments, the alkalinity is analyzed by standard method 2320A.

In some embodiments, an assembly for treating wastewater includes one or more influent streams, one or more aeration tanks or lagoons, one or more separators, and one or more effluent streams. In some embodiments, the inlet stream comprises a water phase and a biosolids phase. In some embodiments, the influent comprises residential wastewater, agricultural wastewater, industrial wastewater, runoff wastewater, or any combination thereof. In some embodiments, the aeration tank includes at least one feed stream and at least one draw stream. In some embodiments, the separator separates the aqueous phase from the biosolids phase. In some embodiments, the delivered microorganisms are added upstream of an aeration tank. In some embodiments, the delivered microorganisms are added to an aeration tank or pond. In some embodiments, the aeration tank is configured to mix wastewater with microorganisms supported on an inorganic porous medium. In some embodiments, the wastewater treatment assembly has increased load bearing capacity. In some embodiments, the effluent stream of the aeration tank has at least twice the biological activity of the feed stream.

In some embodiments, the first separator is configured to receive wastewater from an aeration basin or pond to produce a first fraction comprising biosolids and a treated water stream. In some embodiments, the second separator is configured to receive a first fraction comprising biosolids to produce a second fraction comprising biosolids and a waste product stream comprising biosolids. In some embodiments, the second fraction is recycled to the aeration tank. In some embodiments, the assembly includes a third separator configured to produce a treated water stream and a filter cake. In some embodiments, the biosolids fraction from the first, second, or third separator is directed to a reaction vessel to produce a digested product. In some embodiments, the reaction vessel produces a digested product in a digester. In some embodiments, the digested product is directed to an additional separator configured to remove the aqueous phase from the digested product and produce a filter cake. In some embodiments, the RAS line carries a portion of the biosolids phase from the separator back to the aeration tank. In some embodiments, the portion of the biosolids phase returned to the aeration tank increases the TSS of the aeration tank by 25%. In some embodiments, the portion of the biosolids phase returned to the aeration tank increases the TSS of the aeration tank by 50%. In some embodiments, the portion of the biosolids phase returned to the aeration tank increases the TSS of the aeration tank by 100%. In some embodiments, the concentration of MLSS is greater than 7000 g/L. In some embodiments, the SRT of the aeration tank is greater than twenty days. In some embodiments, the WAS line conveys the second portion of the biosolids phase to a dehydrator that dehydrates the biosolids phase. In some embodiments, the assembly does not include a chlorinator or an ozone generator. In some embodiments, the separator comprises a decanter, a filter, a centrifuge, or a combination thereof.