Abstract:
A process for the conversion of organic materials raw waste and other marine plants and animals into a stable powder form, without high heat or cooking. A raw waste is ground and then optionally hydrolyzed or enzymatically reduced to form a hydrolysate stabilized by adding acid and heated to separate oil and water, to form a product cake transferred to a blender for nutrient mixing, to form a raw product dried in a high velocity air dryer and micronizer. The finely ground raw fish or animal waste, may be cold pressed to remove the oil and water, or bulked with other organic nutrients to adjust pH, increase nutrient value, then blended with nutrients to satisfy feed and fertilizer requirements. The final product may be further milled, classified, and compacted, to control dust and meet market suspension standards for drip, pivot, and other applications for feeding plants and animals.

Description:
[0001]    This Non-Provisional application is a Continuation-in-Part of Non-Provisional application Ser. No. 11/588,829 filed Oct. 27, 2006, which claimed priority to Provisional Patent Application Ser. No. 60/731,106, filed Oct. 27, 2005, and to Provisional Patent Application Ser. No. 60/794,065, filed Apr. 20, 2006. 
     
    
     FIELD OF INVENTION 
       [0002]    The present invention relates to the conversion of organic waste materials, including raw animal and plant wastes, into a stable small micron particle sized powder and granular forms. 
       BACKGROUND 
       [0003]    Sixteen elements are known to be essential for ideal genetic expression in plants, and for maximizing plant growth. These elements are generally considered to be: carbon, hydrogen, oxygen, nitrogen, phosphorus, potassium, calcium, magnesium, sulfur, boron, chlorine, copper, iron, manganese, molybdenum, and zinc. The Earth is essentially a closed system, in which these sixteen elements are recycled or moved from one location to another, for example; from the top soil to the ocean, or into the atmosphere. In nature, we observe a precise recycling of these critical elements. When we disrupt the natural cycle, we place our sources of food, fiber, and energy in jeopardy. And so, it is vital for humanity to work in harmony with nature&#39;s recycling processes. 
         [0004]    Humanity has in some ways short-circuited nature with large scale agricultural practices. Soil, which provides the nutrients required to grow the healthy crops on which we depend, is quickly depleted. In attempts to industrialize and scale-up farming practices, which include the planting of a rapid succession of nutrient sapping crops that cannot replenish the soil, nature&#39;s replenishing processes are bypassed. To supplement or supplant nature, farmers must turn to industrial sources to provide fertilizers to keep the soil infused with the sixteen required nutrients and vital organic materials. There is a need to economically produce these essential nutrients in a form readily available for use in a feed or fertilizer, resulting in a more commercially viable animal and plant food. 
     
    
     
       BRIEF DESCRIPTION OF DRAWINGS 
         [0005]      FIG. 1A  is a schematic of a preferred process of the present invention; 
           [0006]      FIG. 1B  is a schematic of a preferred alternative process of the present invention; 
           [0007]      FIG. 2  is a schematic of a preferred alternative in a process of the present invention; 
           [0008]      FIG. 3  is a schematic of a preferred alternative in a process of the present invention; and 
           [0009]      FIG. 4  is a schematic of a preferred alternative in a process of the present invention. 
       
    
    
     DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS 
       [0010]    The proper ratios and manipulation of essential nutrients required for ideal plant growth can be facilitated by combining industrial mineral sources with plant and animal materials, to form the ideal ratios and formulations. Previous works of the present inventor, namely found in U.S. Pat. Nos. 6,461,399 and 5,466,273, detail processes for converting manures and farm waste into fertilizer products. A desired result of these conversions is a more commercially viable animal and plant food. The process of the present invention converts raw fish, animal and plant waste materials, into a product preferably having a stable powdered form, without the use of high heat in the digesting or cooking process including composting. Additional organic materials may be added to stabilize or otherwise augment the above product. 
         [0011]    Preferred embodiments of the process of the present invention are schematically shown in  FIGS. 1A through 4 . As shown in  FIG. 1A , a raw waste  10  is initially ground  15  in a grinder  16 , and then hydrolyzed or “enzymatically reduced”  20 , within a process tank  23 . This hydrolyzation is achieved by enzyme additives self-contained, enzyme reactions within the raw waste, to form a hydrolysate  25 . 
         [0012]    To manufacture animal feeds, one would use a variation on the above procedure, and include the initial separation of bone from the tissues in the initial grind  15  of the raw fish and animal waste  10 . As shown in  FIG. 1A , with dashed elements to denote optional procedures or process equipment, this variation is accomplished through gentle stirring and separation of tissue and skeleton of the waste, preferably followed by screening with a conventional screen, filter, or most preferably by use of a de-boner  14 , to maximize the protein and minimize the calcium and phosphorous being separated, which in-turn decreases the ash content. A chopper  13  may also be employed, preferably upstream of the de-boner, to aid in separating the bones prior to grinding. 
         [0013]    Within the process tank  23 , the enzymatic reduction also referred to as hydrolyzation  20  is followed by a stabilization  30 , through the addition of an acid  32 , the acid employed in this biological stabilization may be any appropriate acid employed in feed and fertilizer formulation, most preferably a sulfuric acid, a phosphoric acid, a humic acid, an organic sulfonic acid or a citric acid. The acid is employed to lower the pH of the fish hydrolysate. Most preferably, the pH is not lowered below a pH value of 3.5. 
         [0014]    The hydrolysate  25  is then transferred to a heating tank  33 , where it undergoes a moderate heating  35 . This moderate heating step is preferably a gentle heating of the hydrolysate to approximately 120 to 150 degrees Fahrenheit (to 65.5 degrees Celsius) to achieve an oil and water separation  40 , without boiling the solution. The term “approximately” is used herein to refer to a range of values or relative orientations, understood by a person skilled in the pertinent field or skill, as being substantially equivalent to the herein stated values in achieving the desired results, a range typical to the accuracy and precision of conventional tooling, instrumentation or techniques, or a functionally equivalent range of features that produces equivalent results to those described herein. The oil and water separation within the heating tank may include a decanting of any oils  41  collecting at the top of the heating tank and any waters  42  separating from the hydrolysate, typically as a distinct layer below the oils. This separation is best achieved by minimizing stirring or agitation of the hydrolysate within the heating tank. The moderate heating is followed by injecting the heated substrate into a centrifuge  46 . 
         [0015]    Specifically, in this three-phase separation within the centrifuge  46 , the oils  41  and waters  42  are both separated from a product cake  43 , which is simply referred to herein as a “cake.” The centrifuge is preferably a conventional, three-phase, horizontal decanting centrifuge, as is well known to persons skilled in industrial separation technologies. The waters  42  are generally referred to herein as “stick water,” which is conventionally a tea colored, often brackish and nutrient rich liquid, ideal for use as a sprayed soil amendment. The centrifuge provides for the extraction of the oils and waters  45 , with the extracted oils separate from the stick water, and furthermore retains the cake for additional processing. 
         [0016]    In an alternative to, or in addition to the preferred use of the centrifuge  46 , the oil concentration within the hydrolysate  25  can be diluted by addition of other waste streams to absorb the excess oils. For example, a bulking agent  47  may be blended into the hydrolysate. A most preferred bulking agent is chicken feathers, preferably pulverized or otherwise comminuted into a pulp or finely shredded consistency. Chicken feather are an ideal bulking agent in that they have a high pH and readily absorb oils, while adding solids to the hydrolysate mixture. In addition dry animal manures can act as bulking agents to absorb the excess oils and water from the hydrolysate. Other slaughter wastes from poultry, spent hens, hogs and cattle mortalities and slaughter waste could also be utilized, to provide increased nutrient levels, pH control and slow nitrogen release qualities. With the high pH of the chicken feathers, base additives are minimized or not required, as would be needed to neutralize the cake from the prior addition of the acid  32 . 
         [0017]    The cake  43  is the residual substrate of the fish hydrolysate  25 , after the oils  41  and stick water  42  are extracted. From the centrifuge  46 , the cake is transferred to a blender  48 . A primary purpose of the blender is for a nutrient mixing  50  into the cake to form a raw product  55 . Specifically, the nutrient mixing includes the blending of an essential nutrient  58  into the cake. The essential nutrient can include any material that serves in some way to add to or supplement the cake with the nutrients generally recognized as essential, or other attributes needed for ideal plant and animal growth, such as pH adjustment, buffering, or balancing. 
         [0018]    The raw product  57 , which is essentially the cake  43  as amended with the essential nutrients  58  and now substantially dewatered and oil free, is ready to be dried and micronized  60 , The dryer  61  is preferably a high velocity air dryer and micronizer, with sonic vibration capability, or an electric dryer used alone or in combination with the sonic air dryer, commercially available from Marion of Marion Iowa. Most preferably, the blender is employed to meter the raw product into the dryer  55 . The high velocity air dryer and micronizer are employed for particle size reduction, mixing and drying of the raw product, converting it into a product  67 , preferably capable of further size reduction to meet drip and pivot irrigation suspension standards. 
         [0019]    In an optional alternative of the present process, if the essential nutrient  58  additives are in a soluble powder form, they may be blended  70  into the finished product  67  following the drying and micronizing  65  of the raw product, to form an amended finished product  72 . A mixer  74  is preferably employed to perform this blending. As preferred, the mixer may also granulate  75  the amended finished product. The finished product  67 , or the amended finished product  72  is ready for distribution and use in feed or fertilizer activities. A bagging  75  of the products in either powder or granular form is preferably performed to better manage the bulk product. 
         [0020]    In an additional alternative embodiment of the present process, as detailed in  FIG. 2 , certain marine plants and animals such as crab, oyster, kelp and shrimp, which are a raw waste  10  all referred to herein as non-enzyme reduced or hydrolyzed waste  82 , may be ground to a size that allows direct entry into the dryer  61 , uniquely configured for high air velocity drying followed by micronizing  65 , without any prior enzymatic hydrolysis and acid preparation. Additionally, spent hen chicken processing wastes are also ideally suited for use with the present invention. A mill  66 , such as the model “1101GH” of the AUTIO brand of grinder, as manufactured by the Autio Company, of Astoria Oreg., USA, or alternatively, a comparable “Fitz” or Fitzpatrick brand of mill, discussed later herein, can be employed for an initial milling of the non-hydrolyzed waste. These powder forms of marine plant and animal waste can be blended with the fish hydrolysate formed by the process shown in  FIG. 1A , and preferably in the form of the raw product  57 . This blending provides the desired nutrient levels in a powdered mixed product  87 , or the essential nutrients  58  may be added and blended  50  in the blender  48 . 
         [0021]    From the blender  48 , the non-hydrolyzed waste  82  can be introduced into a screen  18 , which may be a standard industrial ‘classifier’, as shown in  FIG. 3 , to obtain a uniformly grained powdered mixed product  87 . Again, the essential nutrients  58  introduced into the blender can include acids and various other nutrients, from the known roster of essential elements, to form complete nutrient quantities and ratios for distribution into the feed and fertilizer markets. As indicated in the coarse fraction recycle  88  from the screen, as shown in  FIG. 2 , some hard-shelled marine animals my need two passes through the mill  66 , and the high air velocity micronizing  65  of the dryer  61 , to obtain adequately preparation for the future micron milling for irrigation application. 
         [0022]    As shown in  FIG. 1B , in an alternative embodiment of the present invention, especially useful when processing certain raw wastes  10  that are reasonably well homogenized, either from prior chopping  13  and de-boneing  14 , or as found with certain raw chicken processing waste, the raw wastes do not require treatment in the process tank  23  for enzymatic reduction  20  and stabilization  30 , as previously discussed herein, and shown in  FIG. 1A . 
         [0023]    The alternative process of  FIG. 2  eliminates the step of enzymatic reduction  20  and instead the raw fish  10  by grinding  15  and preferably an oil  41  and “stick” water  42  pressing in a press  45 B, rather than the alternative centrifuge  45 , to extract the oil and water  46 B. This alternative process preferably employs the bulking agent  47 , as discussed above, to adjust pH, increase nutrient value, and reduce water and oil concentration. Again, a preferred bulking agent is found to be chicken feathers, chicken litter and other carbon manure sources. The raw product material  10  is then dried using the drier  61 , which is a high velocity gas engine with or without a commercial burner  181  prior to introduction into a product mill  205 , as shown in  FIG. 3 . 
         [0024]    Where economics dictate, an electric dryer may be used for the dryer  61 , as manufactured by Marion Mixers of Marion, Iowa. A preferred product mill  205 , used to further reduce particle size, is manufactured by Fitzpatrick Company, of Elmhurst, Ill. The blender  48  can then be used, to add essential nutrients  58 , such as additional organic material. The finished product  67  is a fine mesh, dry powder useful as a fertilizer or feed. 
         [0025]    A alternative preferred process of the present invention, essentially as shown in  FIG. 2 , may additionally include a micronizing CORENCO brand disintegator  150 , discussed above, as the mill  66  for the initial milling  70 . The disintegrator act as the mill and feeder of the non-hydrolyzed waste  82  into the dryer  61 . As shown in  FIG. 1B , the disintegrator may used with a shear pump  151 , such as “Boston Shearpump” brand of pumps, as manufactured by Admix, of Manchester N.H. 
       Example 1 
       [0026]    Raw waste  10  can include fresh, whole or waste fish and related fishing wastes, which are a byproduct of fishing operations and processing of wild and farm fish, and additionally from operations, such as the processing of crab, krill, shrimp, sea weed and kelp; all provide an excellent feed stock source for the manufacture of plant and animal food. As shown in  FIG. 1 , the entirety of the raw waste, including all fleshy and bony parts, is pre-processed by manually or mechanically chopping it into preferably one to two cm diameter chunks, in a chopper  13 , and then de-boning the raw waste in a de-boner  14 . The de-boner is most preferably a pressure de-boner, as is well known in fish de-boning technologies. The chopper and de-boner are optional, in that certain wastes do not require bone removal. The optional pre-processing chopping and de-boning may already have been accomplished in the processing that first utilized the fish material, such as canning or packing operations. After the optional chopping and de-boning operations, the raw waste is pre-ground  11  in the initial grind  15 . Again, for precise particle size reduction, the initial grind is preferably achieved with a conventional 1101GH model of AUTIO brand of grinder which includes a high speed pulverizing head, alternatively, a FitzMill® comminutor, as manufactured by Fitzpatrick of Elmhurst, Ill., or alternatively a Silverson mixer-homogenizer, as manufactured by Silverson Machines LTD., of Chesham Bucks, U.K, could be utilized. Again, the initial grind promotes tissue disintegration of the raw waste, and facilitates the release of natural enzymes present within the waste. These natural enzymes break down fish proteins into their simpler amino acid forms, releasing the oils  41  and water  42 . 
         [0027]    The acid  32 , added to the process tank  23 , is most preferably a sulfuric, a phosphoric, a humic, a sulfonic, or an acetic acid, each selectively added separately or in combination, as needed to provide stabilization through pH reduction, down to approximately 3.5 pH. A combination of acids may be employed, which may be useful to provide essential nutrients  58  to the hydrolysate  25 . The resulting fish hydrolysate is excellent for use the manufacture of certified organic fertilizers, as formed in the finished product  67 . 
         [0028]    Additionally, after treatment in the process tank  23 , the filter  24  may be used to remove any bone material  22  still present in the hydrolysate  25 . This option is preferred, especially if the raw waste  10  includes bony fish, and is most preferably use with the optional chopper  13  and de-boner  14 , discussed above. 
       Example 2 
       [0029]    In a proposed embodiment of the present invention, a typical hydrolysate  25 , approximately 15% oil, 60% water, and 25% solids, could be formed from typical raw waste  10 , depending on fish type and stage of fish development. After the enzymatic reduction  20  and stabilization  30  in the process tank  23 , the hydrolysate could then be transferred to the heating tank  33 , where it is heated to a moderate non-protein denaturing temperature of approximately 140 degrees F. (60 degrees C.) to facilitate the separation  40  of the oil  41  and water  42  from the hydrolysate solids. The oil, water and hydrolysate solids are extracted  45  with the three phase horizontal decanting centrifuge  46 . The hydrolysate solids are then transferred to a specially designed blender  48 , for addition of essential nutrients  58  and introduction into the high velocity air micronizer and dryer  61 . 
         [0030]    After the oil and water extraction  45  of the centrifuge  46 , the cake  42  or fish hydrolysate solid, still would contain approximately 60% water, by weight. At this stage of the process, the cake exhibits a consistency similar to wet clay. If desired, the cake is then mixed or supplemented with essential nutrients  58 , to form the raw product  57 , and is then processed by the dryer  61  for high velocity air drying and initial micronizing  65 . This process step preferably includes a metering of the raw product into the dryer  55  through a specially designed injector, prior to entry into the acceleration tube  160 . A cooling jacket  186  can be utilized to cool the exhaust stream as it travels through the work chamber  166 C, as shown in  FIG. 4 . The acceleration tube consists of a pipe with a diameter of approximately six to 12 inches (15-30 cm), and a length of approximately ten feet to thirty feet (three meters to nine meters), through which is flowing a high velocity air stream or the dryer exhaust stream  170 . The acceleration tube is preferably made of stainless steel or a high density plastic, or alternatively a steel pipe that is most preferably glass lined to reduce friction. The hydrolysate solids of the cake are preferably accelerated in the dryer exhaust stream to an approximate velocity of over 450 miles per hour (725 kilometers per hour), or approximately 40,000 feet per minute (12,000 meters per minute), before entering a comminution chamber within the dryer. Alternatively, a multiple of chambers may be employed. The hydrolysate admixture is at this time subject to physical forces that affect the ability of the water, because of the different densities of water and organic matter of the hydrolysate, to remain physically and chemically bound to each other. The air speed, along with the acceleration tube diameter and configuration, and the pressure. Additionally, the internal comminution chamber air stream obstacles, or lack of them, and proper venting of the water-organic matter separation chamber, all play a critical roll in the effectiveness of the micro-aerosol water and organic matter separation. The particle disintegration that also occurs during the high velocity impaction inside the comminution chamber allows the separation of free water, and bound water. Typical air velocities necessary to accomplish this drying and particles size reduction should be in the approximate range of 40,000 feet per minute (12,200 meters per minute). This is subsonic velocity is developed with system static pressure as high as approximately 15 psig (103 kPa). 
       Example 3 
       [0031]    In a proposed embodiment of the present invention, a raw waste  10  containing 70% water by weight, could be chopped  13  and initially ground  15 , then centrifuged and processed with a pre-dryer  180 , as shown in  FIG. 3 , or bulked with dryer waste material  46  and metered  55  into the primary dryer  61 . The pre-dryer is most preferably a rotary drum type of dryer, as is well known in the field of bulk material drying. 
         [0032]    The metered introduction into the primary dryer  61  may be supplemented with a pressurized injection, as shown in  FIG. 4 , preferably employing an auger or similar forcing mechanism. The dryer is an in-line, pulse type of engine, either alone or utilized in combination with a conventional gas burner  181 , served by a propane tank  183 , or other fuel source. It is predicted that this source material would pass through the system with a final result of 12-15% moisture, by weight. The approximately 27 cubic inch, or about 0.015 cubic foot pulse engine should run at approximately 750 firings per minute to produce approximately eleven cubic feet of hot, high speed air per minute, at around 300 psig of impact force. The in-line pulse engine is preferably wrapped in a sound proofing insulation  190 , as is well known in the field. 
         [0033]    The fertilizer source material  10  is fed into the acceleration tube and processed through the work chamber in the preferred form of a coil tube, as shown schematically in  FIG. 3 , having an overall length of approximately thirty feet or more, comprising of twelve to eighteen inch pipe, or larger. Preferably, the single spiral coil would be approximately twelve feet or more in diameter. The pipe is preferably insulated and the dried raw product  164  contents empty into a receiving bin  187  fitted with power bin filters  40 , for separation of condensed water from within the holding bin environment. 
         [0034]    A hot air recycle  194  can be utilized to return moist hot air from the receiving bin  187  to the pre-dryer  18 , as shown in  FIG. 3 . Additionally, a compressed air  196  can be introduced into the receiving bin to remove caked finished product  67  from the filters  40  or cool the product. A flapper  192  is employed to regulate the recirculation of the drying material around the flash drying coil  190 . The flapper is a standard type of hinged control valve, which is preferably controlled by from input received from a set of sensors  202 , denoted as ‘S’ in  FIG. 3 . The sensors monitor the temperature, humidity and particle size in the flash drying coil at the exit and in the recirculation loop of the coil, as shown schematically. 
         [0035]    The finished product  67  from flash drying coil  190  should measure approximately 15% moisture by weight and is ready to be transferred to the receiving bin  187  and then to the micronizing product mill  205 , preferably by way of an airlock  204 . Additionally, beyond segregating and screening the finished product with the classifier  18 , a compactor  206  can be used to granulate the finished product, as needed. 
       Example 4 
       [0036]    In actual pilot runs of different potential raw wastes  10  for use with the processes of the present invention, a 1:1 mixture of waste and discarded wheat, as an organic material essential nutrient  58  referred to in Table 1, below as Fish/Wheat; a blended mix of fish bones referred to in Table 1, below as FishBones; a mix of discarded crab processing waste referred to in Table 1, below as Crab; a mix of fish bone meal processing waste referred to in Table 1, below as BoneMeal; and a mix of discarded fish and crab processing waste referred to in Table 1, below as Fish/Crab, were each individually processed employing the system essentially as schematically shown in  FIG. 2 . All of these products were under 100 standard mesh, with phosphate analyzed as P 2 O 2 , potassium as K 2 O, and other than pH, all values are reported as weight percent to weight of total finished product  67 . The following results were obtained: 
         [0000]    
       
         
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
             
           
               
                   
                 TABLE 1 
               
               
                   
                   
               
               
                   
                 Nitrogen 
                 Phosphate 
                 Potassium 
                 Calcium 
                 pH 
                 Moisture 
               
               
                   
                   
               
             
             
               
                   
               
             
          
           
               
                 Fish/ 
                 4.6 
                 3.5 
                 0.4 
                 — 
                 6.5 
                 10 
               
               
                 Wheat 
               
               
                 FishBones 
                 6.03 
                 3.7 
                 0.6 
                 3.9 
                 7.8 
                 5 
               
               
                 Crab 
                 5.9 
                 4.2 
                 0.6 
                 3.2 
                 7.6 
                 12 
               
               
                 BoneMeal 
                 10.2 
                 4.1 
                 1.5 
                 — 
                 5.9 
                 15 
               
               
                 Fish/Crab 
                 6.7 
                 4.4 
                 0.7 
                 — 
                 7.2 
                 10 
               
               
                   
               
             
          
         
       
     
         [0037]    Having now described my invention, to those skilled in the art to which it pertains, it may become apparent that the need to make modifications without deviating from the intention of the design as defined by the appended claims.