Abstract:
A process for treating sewage containing biological solids including the steps of mixing the sewage with oxygen-containing hydro fluoro ether polymers, retaining the sewage with the hydro fluoro ether polymers for a desired period of time so as to produce oxygenated sewage and carbon dioxide-containing hydro fluoro ether polymers, and separating the carbon dioxide-containing hydro fluoro ether polymers from the oxygenated sewage. Water is separated from the oxygenated sewage so as to produce a sludge. Oxygen is mixed with the carbon dioxide-containing hydro fluoro ether polymers so as to oxygenate the hydro fluoro ether polymers and to remove carbon dioxide therefrom. The sewage is retained with the hydro fluoro etherpolymers at a temperature of between 32° and 140° F. The sewage is dewatered prior to mixing so that the dewatered sewage has a water content of less than 93 percent by weight. The steps of mixing and retaining can be carried in a closed vessel. The hydro, fluoro ether polymers can be an emulsion containing perfluoro-bis-chlorobutyl ether.

Description:
RELATED APPLICATIONS 
     The present application is a continuation-in-part of U.S. patent application Ser. No. 09/092,579, filed on Jun. 5, 1998, and entitled “Process for Treating a Waste Sludge of Biological Solids”, now U.S. Pat. No. 6,056,880, issued May 2, 2000. U.S. patent application Ser. No. 09/092,579 was a continuation-in-part of U.S. patent application Ser. No. 08/910,849, filed on Aug. 13, 1997, and entitled “Process for Treating a Waste Sludge of Biological Solids”. This patent issued as U.S. Pat. No. 5,868,942 on Feb. 9, 1999 to Boss et al. 
    
    
     TECHNICAL FIELD 
     The present invention relates to processes for the treatment of waste sludges. More particularly, the present invention relates to processes for the aeration of sewage prior to the treatment of the waste sludge. Additionally, the present invention relates to the use of hydro fluoro ether polymers for the treatment of sewage. Furthermore, the present invention relates to processes that render biological wastes pathogen-free, vector-free and sellable. 
     BACKGROUND ART 
     In the past, various techniques have been developed for the purpose of sterilizing or decontaminating biological sludges and wastes. The most common process is the process of mixing lime with the sludge. The reaction of lime with the water in the sludge serves to elevate the temperature of the sludge to a maximum of 100° C. 
     In the past, various U.S. patents have issued relating to processes for the decontamination and treatment of wastewater sludges. For example, U.S. Pat. No. 4,038,180, issued on Jul. 26, 1977 to N. K. Talbert, describes a process of dewatering sewage sludge in which the sludge from a municipal or industrial sewage treatment facility is mixed with a mineral acid or anhydride thereof to release the entrapped water in the sludge. The resulting mixture of the sludge solids and diluted acid or anhydride is then mixed with a basic material, such as ammonia, such that the heat generated by the reaction of the base and the acid evaporates the water to form either a completely dry mixture of sludge solids and a salt or a mixture having a predetermined moisture content which may be air dried. 
     U.S. Pat. No. 4,500,428, issued on Feb. 19, 1985 to Lynch et al., describes a method for the treatment of a wastewater sludge using a pair of reaction vessels, sequentially, to treat the sludge. Both of the vessels are pressurized. The first vessel has an aerator for aerating the sludge. This vesl receives sulfuric acid and chlorine therein through a port. A dewatering device is provided upstream of the first vessel. The outlet of the first vessel is coupled to an inlet of the second vessel through another dewatering device. The second vessel creates a final-treatment chamber in which the sludge is exposed to ozone, air and lime. 
     U.S. Pat. Nos. 4,781,842 and 4,902,431, issued to Nicholson, teach processes for the decontaminating of wastewater sludges to a level which meets or exceeds U.S. E.P.A. process standards. The process mixes sludge with an alkaline material sufficient to raise the pH of the end product to  12  or higher for at least one day. This process will raise the temperature to 50° C., but will not sterilize the sludge nor does it eliminate the pathogenic organisms. 
     U.S. Pat. No. 4,306,978, issued to Wurtz, relates to a process of lime stabilization of wastewater treatment plant sludge. This patent discloses the dewatering of the sludge and intimately mixing calcium oxide to raise the temperature so as to produce a stabilized sludge particle. 
     U.S. Pat. No. 5,482,528, issued on Jan. 9, 1996 to Angell et al., teaches a pathogenic waste treatment process for the processing of solid waste and for the converting of such solid waste into useful products. This is accomplished by combining the waste with an acid, such as concentrated sulfuric acid, and a base, such as fly ash. These exothermically react and thermally pasteurize the waste and add mineral value to the product. Pozzolanic materials, such as fly ash, agglomerate the product. The calcium oxide in the fly ash reacts with sulfuric acid to form calcium sulfate dihydrate. 
     None of these prior art patented processes are capable of achieving temperatures, when mixed with the sludge, of greater than 100° C. None of the prior art techniques allow for the shorter drying times as required by 40 C.F.R. Subchapter  0 , Part 503.32. 
     U.S. Pat. No. 5,635,069 issued on Jun. 3, 1997 to the present inventors. This patent described a process for treating a waste sludge of biological solids which included the steps of mixing the sludge with an oxide-containing chemical and sulfamic acid so as to elevate the temperature of the sludge, pressurizing the mixed sludge to a pressure of greater than 14.7 p.s.i.a., and discharging the pressurized mixed sludge. The oxide-containing chemical could be either calcium oxide, potassium oxide, or potassium hydroxide. The sludge has a water content of between 5 and 85 percent. The oxide-containing chemical and the acid are reacted with the sludge so as to elevate the temperature of the sludge to between 50° C. and 450° C. The pressurized mixed sludge is flashed across a restricting orifice or passed into a chamber having a lower pressure. The evaporated liquid component can be condensed and used as part of the process or external of the process. 
     Typically, there are various problems associated with the treatment of sewage. It is fundamental that the sewage be aerated so that the aerobic microorganisms can be suitably supplied with oxygen such that they can consume the waste. In municipal applications, very large aerator assemblies are provided which continually bubble airthrough the sewage. It is desirable to introduce as much oxygen as possible into the liquid of the sewage. Through bubbling air techniques, a maximum of 9 parts per million of dissolved oxygen can be achieved in the liquid at about 75° F. Frequently, the oxygen content of the liquid will fall to such a level that the process becomes anaerobic. Under such circumstances, a horrible smell will be emitted by the waste processing facility. Since these municipal systems are open to the environment, when the process becomes anaerobic, there will be serious complaints by neighboring residents. Furthermore, these open top municipal treatment systems introduce enormous amounts of carbon dioxide and other hazardous air pollutants into the environment. The aerobic microorganisms consume the waste by converting it into carbon dioxide. Some of this carbon dioxide is emitted into the environment. This can exacerbate the “greenhouse effect”. 
     The metabolic rate of the aerobic microorganisms is only limited by the nutrients (the sewage) and by the oxygen uptake rate. As such, if greater amounts of oxygen could be introduced to the sewage, then the aerobic microorganisms would process the waste with greater rapidity. 
     The cost for aerating the sewage is enormous. For a five million gallon per day facility, the energy cost for operating the aerators is approximately $80,000 dollars per month. Additionally, there is a relatively large capital cost associated with the installation of such aerating systems. Furthermore, because of the relatively small amount of oxygen that can be mixed into the water of the sewage, the processing facility must take up a considerable area. As a result, sewage is pumped into enormous open top tanks. Ultimately, the processed sewage will be discharged into the environment. 
     Importantly, there have been significant developments in the creation of artificial blood. Artificial blood is used by the military for emergency use, in place of plasma, in field conditions. This artificial blood is a hydro fluoro ether polymer which contains long carbon chains. Oxygen molecules are connected to these carbon chains by a relatively weak bond. As result, when the artificial blood is passed through the human body, the blood is oxygenated by the substitution of carbon dioxide molecules for the oxygen molecules in the polymer. Since the carbon dioxide is attached to the carbon chains with a weaker bond than the oxygen molecules, the carbon dioxide molecules can be easily removed from the polymer and substituted with oxygen molecules. The carbon dioxide can be removed from the polymer by simply passing oxygen intimately with the polymer. As a result, carbon dioxide will be discharged from the polymer. 
     This artificial blood, consisting of hydro fluoro ether polymers, is described in U.S. Pat. No. 5,567,765, issued on Oct. 22, 1996 to Moore et al., and in U.S. Pat. No. 5,785,950, issued on Jul. 28, 1998, to Kaufman et al. Each of these patents is owned by Minnesota Mining and Manufacturing Company of St. Paul, Minn. Each of these patents describes highly fluorinated chloro-substituted, non-cyclic organic compounds having 7 to 12 carbon atoms. Importantly, it has been found that this hydro fluoro ether polymers can absorb an excess of 48 percent by weight of oxygen. As such, unlike the 9 parts per million achieved through the use of bubbling air through sewage, hydro fluoro etherpolymers can contain approximately 480,000 parts permillion of oxygen. 
     It is an object of the present invention to provide a process for treating sewage which maximizes the amount of oxygen available to the aerobic microorganisms. 
     It is another object of the present invention to provide a process for treating sewage which causes a processing of the sewage as completely and rapidly as possible. 
     It is a further object of the present invention to provide a process for treating sewage which allows the treatment process to be carried out in a closed container. 
     It is a further object of the present invention to provide a process for treating sewage which eliminates the need for aerators in the sewage tank. 
     It is still a further object of the present invention to provide a process for treating sewage which allows for the containment of carbon dioxide and other hazardous air pollutants. 
     It is still a further object of the present invention to provide a process for treating sewage which minimizes the capital and operating costs associated with the treatment of such sewage. 
     It is still a further object of the present invention to provide a process which renders the sewage pathogen-free and vector-free. 
     It is another object of the present invention to provide a process that converts the biological waste sludge into a sellable end product. 
     It is still a further object of the present invention to provide a process for the treatment of sewage that is cost effective, easy to use and easy to install. 
     These and other objects and advantages of the present invention will become apparent from a reading of the attached specification and appended claims. 
     SUMMARY OF THE INVENTION 
     The present invention is a process for treating sewage containing biological solids including the steps of: (1) mixing the sewage with oxygen-containing hydro fluoro ether polymers; (2) retaining the sewage with the hydro fluoro ether polymers for a desired period of time so as to produce oxygenated sewage and carbon dioxide-containing hydro fluoro ether polymers; and (3) separating the carbon dioxide-containing hydro fluoro ether polymers from the oxygenated sewage. The water is separated from the oxygenated sewage so as to produce a sludge. Oxygen is mixed with the carbon dioxide-containing hydro fluoro ether polymers so as to oxygenate the hydro fluoro ether polymers and to remove carbon dioxide therefrom. The carbon dioxide can be passed to a scrubber so as to separate residual oxygen therefrom. This residual oxygen can be introduced into the hydro fluoro ether polymers so as to oxygenate the hydro fluoro ether polymers. 
     In the process of the present invention, the sewage is retained with the hydro fluoro ether polymers at a temperature of between 32° and 140° F. The sewage can be dewatered prior to mixing such that the dewatered sludge has a water content of less than 93 percent by weight. The steps of mixing and retaining can be carried out simultaneously in a closed vessel. 
     The process of the present invention further includes the steps of: (1) blending the sludge with an acid; (2) mixing an oxide-containing chemical with the blended sludge so as to cause a reaction which elevates a temperature of the sludge; (3) pressurizing the mixed sludge to a pressure of greater than 14.7 p.s.i.a for a period of time of no less than 15 seconds; and (4) discharging the pressurized mixed sludge. The sludge will have a solids content of greater than 7 percent. The oxide-containing chemical can be calcium hydroxide, sodium hydroxide, potassium hydroxide, lithium hydroxide, calcium oxide, sodium oxide, potassium oxide or lithium oxide. The mixing of the sludge can be carried as a flow through a pipe. A pipe can be used so as to maintain the mixed sludge at a pressure of greater than 14.7 p.s.i.a. The pipe should have a length and diameter such that the flow of the mixed sludge will take longer than 15 seconds to pass through the pipe. The step of discharging can include the steps of flashing the pressurized mixed sludge across a restricting orifice and evaporating a liquid component of the sludge. 
     In the preferred embodiment of the present invention, the hydro fluoro ether polymers can be an emulsion including perfluoro-bis-chlorobutyl ether. Alternatively, the hydro fluoro ether polymers can be an aqueous emulsion of a saturated C 8  to C 12  perfluorocarbon ether hydride selected from hydroperfluoroaliphatic ether, hydroperfluoroaliphatic ether substituted with a perfluoroalicyclic group, or a hydroperfluoroalicycloaliphatic ether and mixtures thereof, with water and a surfactant. 
    
    
     BRIEF DESCRIPTION OF THE DRAWINGS 
     FIG. 1 is a flow diagram showing the process of the present invention. 
     FIG. 2 is a flow diagram showing the step of dewatering the sewage. 
     FIG. 3 is a diagrammatic illustration of the BIOSET (TM) process for the treatment of the sludge produced from the sewage. 
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
     FIG. 1 is a flow diagram showing the process  10  in accordance with teachings of the preferred embodiment of the present invention. In the process shown in FIG. 1, the sewage  12  is initially introduced into a mixing chamber  14 . The sewage  12 , being raw sewage, will typically have a solids content of between 0.5 and 3 percent. Oxygenated hydro fluoro ether polymers  16  are also introduced into the mixing chamber  14  so that the oxygenated hydro fluoro ether polymers  16  can be intimately mixed with sewage  12  within the mixing chamber  14 . The mixed sewage and hydro fluoro ether polymers are then passed along line  18  to a retention chamber  20 . The retention chamber  20  serves to retain the mixture of hydro fluoro ether polymers and sewage in intimate contact for a desired period of time so that the aerobic microorganisms can effectively process the sewage. 
     As stated previously, the hydro fluoro ether polymers can contain 480,000 parts per million of oxygen. As such, a relatively small amount of the hydro fluoro ether polymers can be used so as to effectively provide oxygen to the microorganisms in the sewage. Relatively large amounts of oxygen turn the microorganisms into a virtual “incinerator” of the waste. Since the hydro fluoro ether polymers contain the oxygen for use by the aerobic microorganisms, the present invention does not require the use of aerators in the mixing chamber  14  or in the retention chamber  20 . In fact, the mixing chamber  14  and the retention chamber  20  can be completely sealed to the external environment. The creation of carbon dioxide is effectively retained within such closed or sealed containers. As such, there is no discharge of carbon dioxide or other hazardous air pollutants to the external environment. 
     In effect, the mixing chamber  14  and the retention chamber  20  can be the same item. For example, it is possible to introduce the sewage  12  and the hydro fluoro ether polymers  16  through a pipe, having a sufficient diameter and length along with static or dynamic mixers, so that the sewage  12  is maintained in intimate contact with the hydro fluoro ether polymers  16  for the desired period of time. The size of the retention chamber  20 , if it is a pipe, can be set in accordance with the following formula:        τ   =         (     π                   r   2        L     )        ρ     F                            
     where ρ is the density of the sewage/hydro fluoro ether polymers mixture, F is the pounds per hour of processing, r is the radius of the retention chamber  20 , and L is the length of the retention chamber  20 . Under certain circumstances, the hydro fluoro ether polymers may be diluted with water or the sewage dewatered. As such, the length of the retention chamber should be properly set relative to the constraints of the system. For example, the retention chamber  20  can be of a shorter length or of a smaller diameter if purer hydro fluoro ether polymers or higher solids content sewage are processed. 
     As can be seen in FIG. 1, the mixed hydro fluoro ether polymers and sewage are passed from the retention chamber  20  to a settling tank  22 . Alternatively, the settling tank  22  could be in the form of a centrifugal separator or other form of separator. As can be seen in FIG. 1, the settling tank  22  allows the mixture to reside therein such that the hydro fluoro ether polymers  24  reside at the bottom of the tank  22 . The sludge  26  will reside as a layer above the hydro fluoro ether polymers  24 . Water  28  will reside above the sludge  26 . In other words, the materials of greater density will settle toward the bottom of the setting tank  22 . 
     The hydro fluoro ether polymers  24  will have released their oxygen and be saturated with carbon dioxide after mixing with the sewage. The oxygen molecules on the polymer chain will be replaced with carbon dioxide. The aerobic microorganisms have absorbed the oxygen molecules from the polymer chains from the hydro fluoro ether polymers  24 . As can be seen, the hydro fluoro ether polymers  24  will pass as carbon dioxide-containing hydro fluoro ether polymers along line  30  to an oxygenating chamber  32 . 
     When the carbon dioxide-containing hydro fluoro ether polymers reside in the oxygenating chamber  32 , air or oxygen can be bubbled up through the carbon dioxide-containing hydro fluoro ether polymers  34  so as to release gases  36  therefrom. A supply of air or oxygen  38  is connected to the oxygenating chamber  32  so as to allow for the bubbling up of air or oxygen through the carbon dioxide-containing hydro fluoro ether polymers. In this manner, the carbon dioxide molecules are displaced from the polymer chains and replaced with oxygen molecules. The oxygenating chamber  32  is a closed container so as to avoid the release of carbon dioxide, and other gases, into the environment. The gases  36  are released along line  40  into a scrubber  42 . The scrubber  42  can be used so as to remove the gaseous byproducts  44 . Additionally, the scrubber  42  can be used so as to pass excess oxygen along line  46  back to the oxygenating chamber  32 . 
     In the process of the present invention, some of the hydro fluoro ether polymers will deteriorate in their oxygen-containing capacity over time. Other hydro fluoro ether polymers will be lost during the processing of the sewage. As such, a hydro fluoro ether polymers supply  48  can be connected along line  50  to the oxygenating chamber  32  so as to replenish any lost hydro fluoro ether polymers. 
     The oxygenated hydro fluoro ether polymers  52  are then passed from the oxygenating chamber  32  back along line  54  to be introduced as an input to the mixing chamber  14 . As a result, the process provides a closed loop for the hydro fluoro ether polymers used in the system. Since hydro fluoro ether polymers are relatively expensive, it is desirable to minimize the loss of hydro fluoro ether polymers during the processing. 
     In FIG. 1, the settling tank  22  has sludge  26  residing above the hydro fluoro ether polymers  24 . This sludge  26  can be passed along line  56  to a dewatering system  58 . In the dewatering system  58 , it is common to use a conveyor belt onto which the dewatered sludges are placed Various other dewatering techniques can also be employed so as to reduce the water content of the sludge to less than 93 percent. After dewatering, the dewatered sludge can be passed along line  60  to the BIOSET (TM) process  62 . The BIOSET (TM) process  62  is described in association with FIG.  3  and is presently the subject of U.S. Pat. No. 5,635,069. The product of the BIOSET (TM) process can be passed outwardly therefrom along line  64  as a pathogen-free and vector-free product. 
     Water resides as the top layer  28  in the settling tank  22 . The water from the processed sewage  12  can be passed outwardly of the settling tank  22  along line  66  into the environment. Typically, the water will be discharged into a river or stream or into a tank for treatment. A disinfectant  68 , such as chlorine, can be used so as to assure that the water  28  is sufficiently pure for discharge. Similarly, the water  70  resulting from the dewatering system  58  can be passed outwardly along line  72  into the environment  74 . Similarly, the water  76  resulting from the BIOSET (TM) process  62  can be discharged along line  78  to the environment. 
     FIG. 2 shows a variation on a process illustrated in FIG.  1 . Within the concept of the preferred embodiment of the present invention, it may be desirable to dewater the sewage  80  prior to mixing with the hydro fluoro ether polymers. In the dewatering stage, the sewage  80  can be passed along a conveyor so as to separate much of the water from the sewage  80 . The dewatering stage  82  should be sufficient such that the dewatered sewage passing therefrom will have a water content of less than 93 percent by weight. The dewatered sewage is passed along line  84  into the mixing chamber  86 . In the mixing chamber  86 , the dewatered sewage can be appropriately mixed with the hydro fluoro ether polymers  88 . Also, as illustrated in FIG. 2, it can be seen that the hydro fluoro ether polymers  88  can be maintained with the dewatered sewage and retained therein for a sufficient time so as to carry out the proper processing of the sewage. The mixing chamber  86  can be the same item as the mixing chamber  14  and the retention chamber  20  (as illustrated in FIG.  1 ). The mixed hydro fluoro ether polymers and dewatered sewage will pass outwardly of the mixing chamber  86  along line  89  to the settling tank  22  (as illustrated in FIG.  1 ). 
     FIG. 3 is an illustration of the BIOSET (TM) process  62 . In the BIOSET (TM) process  62 , the dewatered sludge is delivered for processing so as to produce apathogen-free and vector-free end product. In the BIOSET (TM) process  62 , the sludge  132 , an acid  134 , and an oxide-containing chemical  136  are delivered together into a feed hopper  138 . The dewatered sludge  132  will have a solids content of greater than 7 percent or a water content of less than 93 percent. It is important for the sludge  132  to have a water content such that the remaining chemicals introduced to the process can properly react with the sludge. 
     Within the present invention, the preferred acid  134  is sulfamic acid. Sulfamic acid is otherwise known as amidosulfonic acid (H 3 NO 3 S). Sulfamic acid is obtained from chlorosulfonic acid and ammonia or by treating urea with H 2 SO 4 . Typically, sulfamic acid is otherwise used in acid cleaning, in nitrite removal, and in chlorine stabilization for use in swimming pools, cooling towers, and paper mills. 
     Importantly, within the concept of the present invention, the acid  134  which is used is not limited to sulfamic acid. Various other acids could possibly be used provided a suitable amount of heat could be imparted to the sludge as it passes a later point in the process of the present invention. For example, carbon dioxide could be substituted for the sulfamic acid. The carbon dioxide would form carbonic acid when reacted with the waste sludge. Although experiments have shown that such carbonic acid would not optimally work in the process of the present invention, it would be possible to use such carbonic acid, or other acids, so as to accomplish the purposes of the present invention. 
     After the sludge  132 , the acid  134  and the oxide-containing chemical  136  are added together into the feed hopper  138 , the mixture is auger fed into the feed section  140  of a screw conveyor  142 . The screw conveyor  142  will rotate so as to transport the mixture of the sludge  132 , the acid  134  and the oxide-containing chemical  136  to a feed section. During the transport of the mixture of the sludge  132 , the acid  134  and the oxide-containing chemical  136 , these materials are mixed together by the screw conveyor. 
     As used in the present invention, the oxide-containing chemical  136  can be either calcium hydroxide, sodium hydroxide, potaasium hydroxide, lithium hydroxide, calcium oxide, sodium oxide, potassium oxide and lithium oxide. In the preferred embodiment of the present invention, the oxide-containing chemical  136  could be calcium oxide. Other ingredients can be added to the feed section  140 , if desired. These other ingredients could be passed along with the oxide-containing chemical  136  or otherwise delivered into the feed section  140 . These materials are then transported to the compression zone  144  of the screw conveyor  142 . This compression zone  144  serves to increase the pressure of the mixed sludge to the desired value. Specifically, the compression zone  144  should increase the pressure of the mixed sludge to a pressure of greater than 14.7 p.s.i.a. Experimentation has found that the desired effects of the present invention are achieved by pressurizing the mixed sludge to a pressure of between 14.7 p.s.i.a. and 120 p.s.i.a. Importantly, the preferred pressure is greater than 20.7 p.s.i.a. At such pressures, water is retained in the mixture and is not flashed from the system. When the water is flashed by pressures of less than 20.7 p.s.i.a., there is a loss of heat of approximately 1,000 BTU per pound of water. As such, to preserve the optimal heating effects in the process of the present invention, it would be desirable to maintain the pressure on the mixture to a level which would prevent the flashing of the water. Furthermore, the higher pressure keeps any ammonia (NH 3 ) from flashing and retains the ammonia for intimate mixing with the pathogens of the waste sludge. The ammonia byproduct produced from the process of the present invention is an effective chemical for the killing of pathogens in the sludge. 
     The adding of the oxide-containing chemical  136  and the increasing of pressure through the motive force of the screw conveyor  142  causes an exothermic reaction along the reaction section  146 . The combination of calcium oxide and the water within the waste sludge produces calcium hydroxide and liberates 235 kcal/mole of heat. This raises the temperature from ambient to 100° C. in 0.5 seconds. The sulfamic acid  134  then reacts with the calcium hydroxide to form calcium salts. This raises the temperature from 100° C. to 140° C. in less than 1 second. 
     In the present invention, the oxide-containing chemical  136  can be produced from any source, such as kiln dust or lime dust. The oxide-containing chemical  136  will make up between 5 percent and 50 percent of the waste sludge  132  by weight. The acid  134  that is added, in any form, whereby the weight ratio of acid  134  to the oxide-containing chemical  136  is between 0.33:1 and 1:1. In general, the temperature of the reaction chamber  146  will be between 50° C. and 450° C. 
     The material which exits the screw conveyor  142  enters pipe  146  having insulation  147  extending therearound. This pipe  146  can contain static mixing elements. The material is continuously mixed as it progresses through the predetermined length of the pipe. The material is continuously under pressure within the pipe  146  so as to prevent a premature flashing of the water within the mixed sludge. The mixed sludge will pass as a flow through the length of the pipe  146 . The pipe  146  should be sized so as to have a length and diameter such that the flow of the mixed sludge will continue through the pipe  146  for a period of no less than 15 seconds. The intimate mixing of the ammonia with the pathogens of the mixed sludge at such an elevated temperature and under such an elevated pressure will effectively destroy any pathogens or vectors which would occur within the mixed sludge. The intimate contact of the sludge with the ammonia provides great disinfecting action to the waste sludge. The pressure within the pipe  146  will prevent the ammonia from flashing. Experiments with the present invention have shown that it will reduce pathogens from 2.2 million colonies per gram to less than 10 colonies per gram. 
     After reacting within the pipe  146 , the mixed sludge is flashed across a restricting orifice  156 . This restricting orifice  156  can be an opening, a die, or a valve. The orifice  156  is positioned generally adjacent to the end of the pipe  146 . The orifice  156  will communicate with a flash chamber  158 . As such, the material is delivered under pressure to the orifice  156  and then released into the flash chamber  158 . A vapor, including water vapor, NH 3 , S 0   2 , and S 0   3 , will exit the flash chamber  158  through the vent  160 . This vapor can then pass to a container  162 . The products of the process can then be sold as valuable byproducts external of the system. 
     In order to properly remove the water from the sludge, it is important that the flash chamber  158  has an interior pressure of between 0 and 14.7 p.s.i.a. As such, when the mixed sludge passes through the orifice  156 , the sludge will be exposed to a lesser pressure. This causes the water and other volatile components of the sludge to be evaporated. As a result, the water content and the temperature of the sludge are appropriately reduced. The heat of vaporization of the flashed material can be passed directly back to the sludge by using heat exchangers, pumps or vapor compressors. After the sludge passes into the flash chamber  158 , the resulting sludge will be a sterile decontaminated product which is pathogen-free and vector-free. This product will meet or exceed U.S. E.P.A. standards. 
     The sterilized sludge then exits the flash chamber  158  through the discharge opening  164 . 
     The geometric configuration of the flash chamber  158  is dependent upon the layout configuration of the facility in which it is used. The flash chamber  158  should have a sufficient diameter and length so as to provide a residence time of the sludge within the chamber of greater than 15 seconds. The insulation  147  is provided so as to eliminate heat loss and to produce an adiabatic reaction. 
     Tests have been conducted with the configuration of the present invention. The experimental data associated with the process of the present invention is identified in Table I hereinbelow. During these experiments, oxalic acid was included in the experiments. However, it was later determined that the oxalic acid is a temperature depressor and can be a poison. As such, oxalic acid should not be included as part of the process of the present invention Other test results have shown that acids such as HN 0   3  acid, acetic acid, and vinegar acid do not achieve the necessary reaction so as to significantly increase the temperature of the waste sludge. 
     
       
         
               
               
               
               
               
               
               
             
               
               
               
               
               
               
               
             
           
               
                 TABLE I 
               
               
                   
               
               
                   
                   
                 OXALIC 
                 SULFAMIC 
                   
                   
                 TIME TO 
               
               
                   
                   
                 OXALIC 
                 SULFAMIC 
                 WAT- 
                   
                 REACH 
               
               
                 EXP 
                 CaO 
                 ACID 
                 ACID 
                 ER 
                   
                 TEMP 
               
               
                 # 
                 gr. 
                 gr. 
                 εr. 
                 cc. 
                 TEMP F. 
                 mins. 
               
               
                   
               
             
             
               
                   
               
             
          
           
               
                 1 
                 189 
                 75 
                 58 
                 24 
                 300 
                 8 
               
               
                 2 
                 169 
                 75 
                 112 
                 24 
                 607 
                 8 
               
               
                 3 
                 337 
                 153 
                 224 
                 24 
                 619 
                 8 
               
               
                 4 
                 337 
                 308 
                 112 
                 24 
                 580 
                 4 
               
               
                 5 
                 189 
                 75 
                 168 
                 24 
                 400 
                 1 
               
               
                 6 
                 169 
                 75 
                 112 
                 24 
                 667 
                 5 
               
               
                 7 
                 50 
                 40 
                 87 
                 24 
                 250 
                 1 
               
               
                 8 
                 169 
                 0 
                 130 
                 24 
                 840 
                 1 
               
               
                 9 
                 189 
                 130 
                 0 
                 24 
                 370 
                 1 
               
               
                 10 
                 189 
                 0 
                 0 
                 12 
                 213 
                 0.2 
               
               
                 11 
                 0 
                 75 
                 0 
                 12 
                 0 
                 1 
               
               
                 12 
                 0 
                 0 
                 50 
                 12 
                 0 
                 1 
               
               
                 13 
                 189 
                 130 
                 0 
                 24 
                 500 
                 3 
               
               
                 14 
                 189 
                 0 
                 130 
                 24 
                 620 
                 1 
               
               
                 15 
                 85 
                 0 
                 85 
                 24 
                 700 
                 1 
               
               
                 16 
                 189 
                 0 
                 130 
                 24 
                 750 
                 1 
               
               
                 17 
                 189 
                 0 
                 130 
                 72 
                 750 
                 1 
               
               
                 18 
                 169 
                 0 
                 189 
                 24 
                 800 
                 1 
               
               
                   
               
             
          
         
       
     
     The foregoing and description of the invention is illustrative and explanatory thereof. Various changes in the details of the illustrated construction or of the steps of the described method made within the scope of the appended claims without departing from the true spirit of the invention. The present invention should only be limited by the following claims and their legal equivalents.