METHOD AND APPARATUS FOR EFFECTING SUBSURFACE,CONTROLLED,ACCELERATED CHEMICAL REACTIONS

Abstract: The problem of conducting chemical reactions at elevated temperatures and pressures, such as in the wet oxidation of a waste stream, without excessive expenditures of energy is solved by the method and apparatus for effecting accelerated chemical reactions utilizing a reactor (15) extending into a vertical hole (16) in the earth and having an outer flow passage (21) receiving influent fluid from a supply (38) and supply lines (31 and 33) pumped with air by a pressure pump (29). The fluid undergoes an accelerated oxidation in the hole giving off the products of reaction, heat, and an effluent fluid which flows up an inner flow passage (22) to a settling tank (41) and/or other discharge lines (44, 42). Apparatus for control of temperature, pressure and flow rate are also provided to maximize reaction rates and minimize power requirements.

Description: -1- METHOD AND APPARATUS FOR EFFECTING SUBSURFACE, CONTROLLED, ACCELERATED CHEMICAL REACTIONS Technical Field; This invention generally relates to improvements in effecting chemical reactions and more particularly to a novel and improved method and apparatus for effecting accelerated chemical reactions that is especially effec¬ tive in efficiently carrying out the wet oxidation of sew¬ age sludge and like waste streams, purifying the water content, and also recovering energy in the form of heat. Background Art: There are a variety of chemical reactions that may be accelerated under conditions of a temperature sub¬ stantially above ground surface ambient temperature and a pressure, substantially above atmospheric pressure. A major part of the reactor apparatus heretofore provided for carrying out the various chemical reactions at higher temperatures and pressures typically require high pres¬ sure liquid pumps, high pressure, high temperature heat exchangers and pressure vessels with rotating seals and considerable land surface area. One chemical reaction for which the method and apparatus of the present invention is particularly suit¬ able is for the direct wet oxidation of materials in a waste stream and particularly the direct wet oxidation of sewage sludge. The Zimpro method, Barber-Coleman process and Navy shipboard processors are examples of current methods used to effect direct wet oxidation of sewage sludge and all involve placing the waste in a high temperature, hig pressure reactor at substantially ground surface level. Air is pumped into the reactor vessel and heat is externa applied. Constant mechanical stirring is required to mix oxygen, a reactant, into the liquid and to remove carbon dioxide, a product of the reaction. Some attempt has been made to carry out accelerated chemical reactions below the ground surface level using the increased pressures provided by a hydrostatic column of liquid or fluid. In this connection, particular atten tion is directed to U. S. Patent Nos. 3,449,247 to Bauer, 3,606,999 to Lawless and 3,853,759 to Tit us. DISCLOSURE OF INVENTION A method and apparatus for effecting accelerated chemical reactions utilizes a reactor having a downgoing through-pipe that extends down below the ground surface a substantial distance and back up providing a hydraulic U-tube for a reaction that takes place a substantial distance below the ground surface level. An influent fluid is pumped down the downgoing pipe portion from the ground surface level at a controlled, selected temper ature, pressure and flow rate to a selected depth below the ground surface to form a hydrostatic column sufficien to provide a selected pressure and temperature that causes the reactants to react at an accelerated reaction rate and further down the downgoing pipe portion " through reaction zone for a selected retention time whereby heat is released, reaction products are produced, and the flui is heated in the reaction zone. The heated fluid and reaction products are flowed back up the upgoing pipe por tion in heat exchange relation to the downgoing fluid to effect a substantial cooling before exiting the outlet of the upgoing pipe portion. The temperature of the influent fluid in the reaction zone is controlled by adding or removing heat to maximize the reaction rate and to prevent boiling of the fluid in the reaction zone. Once the operation is under way, heat from the exothermic reaction is removed as useful heat energy. If a gas is used in the reaction, the results are enhanced by introducing a stream of gas under low pres- sure in the form of a series of enlarged bubbles, known as "Taylor bubbles", formed at the top of the reactor. Preferably the gas is introduced in a plurality of streams at more than one elevation to reduce pumping requirements. These enlarged bubbles cause the least amount of pressure differential in the flow passage and thus minimize pumping pressure to maintain a certain flow rate. These enlarged bubbles also provide intense mixing and contacting to increase the flow of reactants and pro¬ ducts to and from the fluid since the fluid flows over the bubble and there is no boundary layer formed as is found in bubbles of smaller size. The quantity, of gas injected is controlled to provide the proper ratios relative to the influent fluid since insufficient gas pro¬ duces undesirable products and excess gas is wasted and reduces the reactor throughput rate. Fluid flow velocities are maintained at a greater velocity than the bubble rise velocity in order to carry each bubble down to the reaction zone. Pressure and flow rate at the out¬ put of the reactor are controlled to maintain the proper flow rates and pressure in the system. Other objects, advantages and capabilities of the present invention will become more apparent as the descrip¬ tion proceeds, taken in conjunction with the accompanying drawings in which like parts have similar reference numerals and in which: DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic diagram of apparatus embody¬ ing features of the present invention which utilizes a gas as one reactant; Figure 2 is an enlarged schematic diagram of the apparatus of Figure 1 showing in more detail the manner of introducing a gas under pressure into the fluid stream to produce enlarged bubbles which flow down the outer flow passage and up the inner flow passage; -^URE Figure 3 is an enlarged schematic diagram showing the passages and bubbles with the flow in the opposite direction from that of Figure 2; Figure 4 is a schematic diagram of the reactor with designations at various depth locations for reference to the structure shown in more detail in Figures 5-19; Figure 5 is a vertical cross-sectional view of an upper portion of the reactor; Figure 6 is a cross-sectional view taken along lines 6-6 of Figure 5; Figure 7 is a vertical cross-sectional view of an intermediate portion of the reactor; Figure 8 is a vertical cross-sectional view of a lower portion of the reactor; Figure 9 is a vertical sectional view taken along lines 9-9 of Figure 7; Figure 10 is a sectional view taken along lines 10- 10 of Figure 9; Figure 11 is a sectional view taken along lines 11- 11 of Figure 7; Figure 12 is a sectional view taken along lines 12-1 of Figure 7; Figure 13 is a sectional view taken along lines 13- 13 of Figure 8; Figure 14 is a sectional view taken along lines 14-14 of Figure 8; Figure 15 is a sectional view taken along lines 15- 15 of Figure 8; Figure 16 is an enlarged vertical cross-sectional view of Figure 13 showing in more detail the flow of fluid between the jacket and flow line; Figure 17 is a sectional view taken along lines 17-17 of Figure 8; Figure 18 is a sectional view taken along lines 18-18 of Figure 17; Figure 19 is a perspective view of the bottom of the jacket of the reactor; Figure 20 is an enlarged side elevational view of a Taylor bubble; gure s a o om v ew o e n Figure 20; and Figure 22 is a diagrammatic view showing three reactors connected in series and placed in one outer casing. DESCRIPTION OF THE PREFERRED EMBODIMENTS Referring now to Figure 1, the schematic diagram shows a reactor 15 constructed and arranged in accordance with the present invention that extends into a vertical hole 16 in the earth to a substantial extent below the ground surface level designated 17. The reactor 15 shown in general has an outer pipe portion 18 and an inner pipe portion 19 in spaced concentric relation with the outer pipe portion 18 defining an outer flow passage 21 between the outer and inner pipe portions and an inner flow passage 22 through the inner pipe portion 19. The outer pipe portion 18 has a closure cap 24 covering the lower end thereof and the inner pipe portion 19 terminates a selected distance above the closure cap 24 to form a subsurface, hydraulic U-tube structure within hole 16. The reactor 15 shown further has an upper portion projecting above the grovjnd surface level 17 provided with a port 26 in flow communication with the outer flow passage 21 through which an influent fluid is shown as flowing, as indicated by arrows,and a port 27 in flow communication with the inner flow passage 22 through which the effluent fluid is shown as flowing, as indicated by arrows. While the direction of the arrows shows the flow of the influent fluid down the outer flow passage 21 and up the inner flow passage 22, this provides a greater input flow capacity for influent fluids, which usually have a greater viscosity than effluent fluids, but it is understood that the direction of fluid flow can be reversed as illustrated in Figure 3. A low-pressure pump 29 at the ground surface level is provided to pump the influent fluid supplied from a suitable supply indicated at 38 via a supply flow line 31 with a pressure control valve 32 at a selected pressure through port 26 via a flow line 33 coupled O PI age 21, as indicated by arrows. A bypass control valve 34 in a bypass line 35 bypasses the pump 29 for flow directly from flow line 31 to flow line 33 since, after the fluid is flowing through the U-tube structure, in man instances no pumping pressure will be required to sustain a continuous flow therethrough. A back pressure control valve 36 in an outlet flow line 37 from outlet 27 control the flow rate and pressure ' of the effluent fluid flowing up through flow passage 22 by virtue of the size of the orifice therethrough. A supply of influent fluid is indicated at 38, and the flow therefrom into flow line 31 is controlled by control valve 32. The pump 29 controls the pressure and flow rate through flow line 33 during start-up and valves 34 and 36 control the pressure and flow rate during operation. The apparatus shown in Figure 1 is suitable for carrying out the direct wet oxidation of a waste stream and particularly aerobic sewage treatment plant sludge waste, although it is understood that the present inventi is capable of carrying out a variety of high-temperature, high-pressure chemical reactions. In the illustrated flow diagram where a sewage slud stream is being processed, the effluent fluid passing through flow line 37 is passed into an ash settling tank 41 with clean water being recycled back as a clean or purified diluent to the feed flow line 31 via a flow line 42 with a control valve 43 to control the concentration of the influent fluid so that the settings of valves 39 and 43 achieve a blend of influent fluid having a selected C.O.D. The mass of oxygen required to complete the oxidation reaction is termed the "chemical oxygen demand" (C.O.D) of the sewage sludge. The settling tank 41 has a purified water discharge flow line 44 and an ash flow line 45. Temperature control apparatus is provided for controlling the temperature of the influent fluid in the reaction zone designated R. This temperature control apparatus includes a coolant pump 51 at the ground surfac eve a pumps a coo an u s ore n a groun level coolant tank 52 through a heater 53 at the ground surface level down to the bottom of a heat exchange jacket 55,through a valve-controlled flow line 54, and back up the hole through a valve-controlled flow line 56. The heater 53 may take a variety of forms but, as illustrated schematically, is an electric heater supplied electric power from a power source 53a with a control rheostat 53b for regulating the voltage applied -to a heating element 53c to change the heater temperature setting and thereby the temperature of the coolant fluid flowing in flow line 54. The jacket 55 is of a hollow, annular, tubular construction that is substantially coextensive with the reaction zone R and further is in heat exchange relation with the outer flow passage 21, as is described more fully hereinafter. The other flow line 56 is coupled to and extends from the top of the jacket at the top of the reactor zone up to the ground surface level and is coupled to tank 52 by a return valve-controlled flow line 56a to add heat to a fluid in lines 54 and 56. A heat removal circuit includes a valve-controlled flow line 56b coupled to line 56 down to the top of the jacket 55 and a valve-controlled flow line 54b above the ground surface coupled to a heat exchanger 58 which in turn is coupled to tank 52 to pro¬ vide a closed-loop, fluid flow ' temperature control circuit. The flow control valve in flow line 54b controls the rate of flow in this fluid flow circuit. By means of regulating the temperature of the coolant fluid in the jacket 55 and flow lines 54 and 56, the tem¬ perature of the influent fluid in the reaction zone R is controlled. This is accomplished by adding or removing, heat to and from the coolant fluid and is controlled to accomplish substantially a maximum reaction rate with the vapor pressure of the influent fluid at the local tempera¬ ture being maintained always lower than the local pressure to prevent boiling of the influent fluid. The temperature of the influent fluid is increased by adding heat pro¬ vided by the heater 53 that heats the coolant fluid passing OMP throug ow l ne 4 an own nto ac et y t e pres sure supplied by pump 51, with the flow rate of the coo ant fluid controlled by the setting of the control valve in line 54. The upper limit of the temperature of the influent fluid in the reaction zone is controlled by regulating t heat removed from the heat exchanger 58 and the flow rat which is controlled by " the setting of the valve in line 54b. The amount of heat removed is directly related to the setting of the valve in line 54b. A turbine 60 is shown coupled to the heat exchanger 58 via a flow line with a control valve 66 as an illustration of the utilization of the energy, and specifically- the heat produced by the reaction,to convert heat energy to mecha iσal energy. Alternatively, a load 67 is shown coupled to the heat exchanger via a flow line with a control valve which couldbe a room heated by the heat produced by the reactor. A pressure sensor for measuring the pressure at the upper limit or beginning of the reaction zone R. includes a small-diameter tube 61, such as a 1/8 inch stainless steel tube, that extends down through the inner pipe portion 19 to the upper limit of the reaction zone R. At the ground surface level a pressurized bottle 62 provides a selected air pressure to flow air down through the tube 61 via a delivery valve 63. Between the bottle 62 and tube 61 there is coupled a delivery air pressure gauge 64 and a pressure regulator 65. To make a pressure read¬ ing, water is flushed out of the tube 61 and the delivery valve 63 is closed. The reading on the pressure gauge 66 is the pressure inside the reactor at the upper limit or top of the reaction zone which is a critical part of the temperature and pressure for the reactor. In chemical reactions where a gas is used as a reactant,and specifically in carrying out the wet oxida¬ tion of sewage sludge where the oxygen content of air is required, it has been found that the operation and results are significantly enhanced by the use of enlarged gas bubbles 78. With specific reference to Figures 20 n , e es c a ac ze y a e a has a generally spherical cap portion 78a, a generally cylindrical main body portion 78b, and a truncated bottom portion 78c. The transverse cross section is circular. In the enlarged view, it is shown that the body portion diverges from the top portion to the base portion along a curve. This bubble is frequently referred to as the "Taylor bubble" after G. J. Taylor who is credited for accomplishing their original investigation. The Taylor bubbles are compressed as they flow down through the outer flow passage and, upon reaching the reaction zone, the oxygen carried therein is a reactant in a reaction which causes an intense mixing, contacting and a rapid oxidation of the sewage sludge with smaller bubbles returning via the inner passage. The principal advantages of the use of these bubbles as compared to a swarm of very fine bubbles are that the pressure drop per length of pipe for the Taylor bubble is considerably less, thereby reducing the pumping re- quirements to pump the fluid and bubbles down into the earth, and further there is accomplished a greater total mass transfer between the gas and the liquid phase in the reaction zone R. This results in an increased gas- liquid mixing with greater dissolving of the gas in the liquid and a greater.removal of the reaction products from the liquid. The apparatus shown that is utilized for forming these enlarged bubbles is an air compressor 71 at the ground surface which, through one or more flow lines, delivers one or more streams of air at a selected pressure into the upper portion of the outer flow passage to combine with the influent fluid from the input flow line 33. A series or train of enlarged or Taylor bubbles 78 are formed that are carried down with the influent fluid. For this purpose, there is shown a control valve 76 in a flow line 77 that extends into flow line 33 at ground level and a control valve 74 in flow line 75 extending to one depth below the earth's surface, as well as a control valve 72 in line 73 extending yet further into the earth's surface. A terminal pipe section or portion of each of the flow lines 73, 75 and 77 extends in a longitudinal relation to and within the downgoing flow passage with an outlet opening toward the downstream end of the down- going flow passage so that a stream of air is introduced under a selected pressure and flow rate into the influent fluid stream. By the proper selection of pressure, temperature and flow rate in relation to the flow rate and pressure of the influent fluid, bubbles coalesce into a train of Taylor bubbles 78 arranged at spaced intervals along the outer flow passage 21. These enlarged or Taylor bubbles will rise at a uniform rate with respect to water. Their relative veloc with respect to water is given by: where: r = pipe inside radius (ft.) In the apparatus shown the flow velocity of the influent fluid waste stream must be maintained at a great value than the bubble rise velocity in order to carry each of the bubbles down to the reaction zone R. The influent fluid flows over the bubbie and maximizes the mass transfer between the liquid and gas phases in the reaction zone. Since the oxidation reaction is overall first order, the rate of reaction is directly proportiona to the amount of products and reactants in the liquid. The Taylor bubble provides a smaller hydrodynamic pressur loss inside the flow passage as compared to a swarm of smaller bubbles, thereby reducing the amount of energy required to flow the material at a certain rate through the U-tube structure. Smaller size bubbles create a larg hydrodynamic pressure loss throughout the hydraulic colum Also a smaller bubble has a boundary layer of water assoc ted with it which impedes the mass transfer between the two phases. Thus, the Taylor bubble maximizes reaction rates while minimizing horsepower required for pumping th fluid through the pipe system. — / ^£\ To minimize the horsepower required by compressor 71, air is introduced at the top of the outer flow passage 21 at more than one elevation, as shown in Figures 1 and 2. Air is introduced at the highest elevation at the lowest pressure in an amount equal to one volume of air per volume of liquid. As the fluid descends, the pres¬ sure increases and the air is compressed. Additional air is injected at a lower elevation and at successively higher pressures, again at an amount equal to one volume of air per volume of liquid. This sequential injection of air at successively greater depths minimizes the com¬ pressor requirements and provides the oxygen necessary to oxidize the reactants in the liquid. The pressure at any point in the reactor depends upon the mass of the fluid above. If only water were used, the pressure gradient would be approximately .43 psi per foot of depth. However, the downgoing flow passage 21 contains a substantial volume of gas which is compressed in volume and heated as it travels downwardly. In summary, by introducing the air at different elevations below the earth's surface, less pumping pres¬ sure is required and,once the process is in operation, the downflowing influent fluid material will draw the liquid in without the necessity of a liquid pump. This Taylor bubble configuration minimizes compressor require¬ ments, creates the least amount of pressure differential and increases the flow of reactants and products to and from the fluid, since the fluid flows over the bubble, and there is no boundary layer formed as found in bubbles of smaller size. The reactor shown in more detail in Figures 5-1 is located inside a well hole, lined with a well casing comprised of an enlarged upper section 81 and a smaller diameter lower section 82 that has grout at 83 outside section 82 throughout the vertical extent of sections 81 and 82, and has a grout plug 84 closing and sealing the bottom of casing section 82. The upper end of well cas¬ ing section 81 is secured as by welding to a circular base plate 86 recessed to be flush with the ground surface 17 . In general, the outer pipe portion 18 and inner pipe portion 19 are supported in a suspended depending manner from the base plate 86 in such a way as to allow for expansion and contraction thereof relative to the wel casing due to temperature changes. The upper end of the top pipe section of the outer pipe portion 18 is secured as by welding to a circular baseplate 87 that rests on base plate 86 to support the outer pipe portion 18 in a suspended depending manner in the casing 82. Two flow ' pipes 54 and 56 for conveying fluid to and from the coolant jacket 55 extend down throu a bushing in the base plate between the well casing and the exterior of the outer pipe portion. There is further provided above the ground surface level an extension of the outer pipe portion 18 including a straight coupling 89 threaded on external threads of th top subsurface pipe section of outer pipe portion 18 affixed to plate 87 that rests on plate 86, a pipe nipple 91, a tee coupling 92 and a pipe 93 having a flange plate 94 secured as by welding to the upper end with the lower end threaded into the tee coupling 92. A flange plate 95 rests on flange plate 94 and has the upper end of the inner pipe portion 19 secured thereto as by welding so that the inner pipe portion 19 is supported in a suspende depending manner from the outer pipe portion 18 which in turn is supported on plates 86 and 87. Yet a third top flange plate 96 rests on flange plate 95 and has an upper pipe nipple 97 threaded thereto with a top coupling 98 secured thereto to provide the coupling to the flow line 37 through which the effluent fluid is passed. There is further shown a gasket 101 between plates 94 and 95 and a gasket 102 between plates 95 and 96, together with a bolt fastener 103 to hold the flange plates together in a sealed watertight manner. Th pressure sensing tube 61 is shown as extending down throu the center of flange plate 96 and the inner pipe portion which is shown to extend up above the ground surface leve to connect to flange plate 95. The two flow lines 54 and 56 for conducting the cool¬ ant fluid extend from the ground surface down through support plate 87 and are supported on the outer pipe sec¬ tion, as best seen in Figures 9 and 10. Each coolant fluid flow line has a series of alternating pipe sections shown as a relatively long, rigid pipe section 109 on the order of 100 feet and a flexible pipe section or hose 111 on the order of two feet that are joined end-to-end to one another by a coupling 112. The lower end of the rigid pipe portion 109 rests on a support surface provided by a lower bracket 110 clamped to the outer pipe portion 18. A supporting guide bracket 113 guides the upper end portion of the outer pipe portion 18 in an axial sliding movement and has an annulus 114 which in turn carries a resilient sleeve 115. The rigid pipe section 109 is axially movable in the resilient sleeve to allow for axial movement of these flow lines for contraction and expansion due to temperature changes. Each flexible pipe section 111 is shown in a bowed configuration to allow for expansion and contraction. The coupling 112 on the lower end is slidable with pipe section 109 and the coupling 112 on the upper end is held by bracket 110. The flexible pipe section 111 may be made of a bellows- like conduit covered with a heat-resistant braided cover. As best seen in Figures 7 and 8, the outer pipe portion 18 extending from ground surface into the hole is made up of a plurality of end-to-end pipe sections 118 connected at adjacent ends by API (American Petroleum Institute) couplings 116. These couplings have a sub- stantial taper at each end and are standard well-type pipe couplings. The pipe sections making up the outer pipe portion 18 above the reaction zone as shown are made of black iron with a stainless steel liner 108 shown in Figures 11 and 12 and extend from the reaction zone up to a depth below the surface level of about 500 feet. This construction prevents corrosion. In a like manner, the inner pipe portion 19 is made up of a plurality of end-to-end pipe sections 119 connected at adjacent ends by end welds. As shown in Figure 15, the bottom pipe section of the outer pipe portion 18 has a shaped 180 degree turnaround provided by an end cap 24 to prevent plugging by scouring which directs the flow up through the inner pipe portion 19. Since there is no pressure differential across the wall of the inner flow passage, a thin-walled tube is used. Use of a thin-walled tube decreases cost and allows for better heat exchange between the hot reacted effluent fluid and the cool untreated influent fluid. For reference purposes, the inside diameter of the outer pipe portion 18 above the reaction zone is designat Dl, the inside diameter of the inner pipe portion 19 above the reaction zone is designated D2, the inside diameter of the outer pipe portion in the reaction zone is designated D3 and the inside diameter of the inner pipe portion 19 in the reaction zone is designated D4. The jacket 55 is provided on the outer pipe portion beginning at a selected depth below the ground surface level, which is at the top or beginning of the reaction zone R. At this depth both the outer and inner pipe portions are reduced in size, to provide a substantially constant mass flow rate. As the fluid flows down the outer flow passage, the gas is compressed and as a result the volumetric ratio of gas to liquid decreases with a resulting decreas in the velocity of the liquid. To maintain more nearly constant flow velocity, the outer and inner pipe portions are reduced in size in the area of the reaction zone. Th reduction in size increases the amount of production per capital investment and also maintains at least the flow velocity required to sweep the gas bubbles downward. As shown in Figure 11, an inner pipe section 119a a distance above the reaction zone has a reducing sleeve or coupling 121 along the inside which receives a smaller diameter inner pipe section 119b. In a like manner, .as shown in Figure 12, an outer pipe section 118a below coup ing 121 and above the reaction zone carries a reducing coupling or sleeve 122 which in turn has an inside cut into which a smaller diameter outer pipe section 118b is . iron lined with a stainless steel tubing 108 above fitting 122 extending up to about 500 feet below the ground sur¬ face. The reduction couplings are preferably made of stainless steel and machined to have a smooth, tapered entrance surface to prevent plugging. A larger outer pipe section 123 fits over an annular outer cut on sleeve 122 with a space between pipe sections 123 and 118b forming the coolant jacket 55 which extends down to the bottom of the reactor. The heat from the reaction is collected in the jacket 55 and is passed therefrom, or heat may be input, in the form of a heated coolant fluid and/or steam to assist in starting up the reactor. At the upper end of the jacket 55, there is a fitting 120 mounted on pipe section 123 coupling flow from line 56 to the interior of the top portion of the jacket. At the lower end of the outer jacket 55, there is an end cap 124 that cups over the lower end of the outer pipe section.123 forming the jacket and is secured thereto as by threads or welding. End cap 124 has a vertical aperture 125 in the bottom thereof. A fitting 126 shown in Figures 17, 18 and 19 is secured as by welding to the bottom of the end cap 124 and ex¬ tends laterally out so as to be offset to one side thereof. The fitting 126 has a passage that opens into the bottom of the jacket and has a hole 127 at one end and couples to flow line 54. The jacket with end cap and fitting termin¬ ates a distance above the plug 84 to allow for up-and-down movement thereof relative to plug 84 due to expansion and contraction. To monitor temperature, temperature sensors in the form of thermocouples 131 shown in Figure 4, are placed on the outer pipe portion at approximately 250-foot inter¬ vals and are connected to a temperature indicator T at the surface level. A large heat loss can result from the presence of water inside the well casing 81 and 82. Such water will vaporize and rise to a cooler level, where it condenses and then flows down the external wall surface of the reactor until it is vaporized again. This refluxing action reduc the overall energy efficiency and feasibility of 1he proce To prevent this problem the inside of the casing can be dried by pumping or purging or can be insulated with a layer of insulation indicated at 129, shown in Figures 8, 17 and 18. A plastic-coated fiberglass bat, rock wool or ceramic felt has been found to be effective as an insulation for this purpose which serves as a baffle to prevent conductive and convective heat losses. OPERATION The influent fluid which in the specific applica¬ tion described herein is a streamof sewage sludge is pumped from supply 38 via flow lines 31 and 33 into and down the outer flow passage 21. A stream of air under pressure is pumped into the outer flow passage to form a train of spaced Taylor bubbles 78 and the pressure pro¬ vided by pump 29 is sufficient to move both the influent fluid and bubbles down the outer passage 21. As the two proceed down below the ground surface, the temperature and pressure increase and they reach a point at which oxid tion proceeds at an accelerated reaction rate, indicated at line D, and proceeding to the bottom, indicated at line G. The area between lines D and G is designated R. In the reaction zone R the pressures and temperature rapidly mix the oxygen with the water to cause a rapid oxidation of the combustible solids and a generating of heat to heat the fluid. Some of the reaction products resulting from the oxidation are C0 2 , H-O, N + heat. The heated fluid and reaction products, termed the "effluent fluid", then flow up the inner flow passage 22 in heat exchange relation to the downflowing influent fluid. Upon exiting the reactor, the effluent fluid is flowed through the ash settling tank and then is either used as a diluent for the influent fluid to maintain the proper influent C.O.D. or is discharged via flow line 44. The blend or concentration of the reactants in « relation to one another in relation to the amount of liqui content (water) of the influent fluid is controlled by the settings of valves 72, 74, 76, 43 and 39 relative to one ano er. s ou e no e a eac o ese con ro s is adjustable or settable at or in the area of the ground surface level. During start-up, heat is usually added to the reac- tion zone to heat the influent fluid by pumping a coolant fluid from tank 52 through heater 53, down flow line 54, through jacket 55, and back up flow line 56. After the temperature rises to about 400°F at the upper level of the reaction zone and heat is produced from the ensuing exothermal reaction, the direction of flow of the coolant fluid in lines 54 and 56 is reversed and pumped from the jacket up through flow lines 54 and 54b into the heat exchange unit 58, from which heat or work via a steam turbine generator 60 may be derived or heat may heat the room 67. Temperature at the start of the reaction is controlled by varying the setting of control 53b and by the flow rate in line 54. Temperature during operation is controlled to maintain the vapor pressure of the influent fluid at the local temperature lower than the local pressure to prevent boiling while maximizing the reaction rate. Referring now to Figure 22, there is shown an arrange¬ ment of the present invention wherein three subsurface reactors 135, 136 and 137 are mounted in one outer well casing 138 for greater treatment capacity in one vertical hole of shorter depth than would be required for one long reactor. Again the casing has grout lining the inside of the hole and has a grout plug seal 139 at the bottom. The void between the reactors and casing is shown filled with an insulation 141. As previously described, each reactor has an outer pipe portion and an inner pipe portion with associated input and output ports above the ground surface. In the arrangement shown there is a tank 142 for reactor 135, a tank 143 for reactor 136 and a tank 144 for reactor 137. A fluid pump 148 and an air compressor 149 are associated with each reactor, as previously described. Influent fluid indicated at line 145 and gas under pressure are pumped into tank 142 and from tank 142 down reactor 135 effluent fluid from reactor 135 to the tank 143. Influe fluid from tank 143 and gas are pumped into reactor 136, with effluent fluid out of reactor 136 pumped into tank 144. Finally, effluent fluid and gas under pressure are pumped from tank 144 into reactor 137 and effluent fluid from reactor 137 is passed to a point of use via line 14 This arrangement of three reactors coupled in seri increases the C.O.D. reduction over a single reactor hav the same retention time, apparently due to the fact that the reaction product CO can be removed via the tanks 14 Some typical ranges are listed in the following ta TABLE Example Range 1. Reactor Above Reaction Zone Diameter Outer Pipe Portion Dl ID 2.465 in. 1 to 24 in Inner Pipe Portion D2 ID 1.560 in. 3/4 to 20 Reaction Zone Diameter Outer Pipe Portion D3 ID 1-870 in. 3/4 to 20 Inner Pipe Portion D4 ID .995 in. 0.5 to 18 Total Depth 1500 ft. 1000 to 60 Depth to Start of Reaction Zone 1000 ft. 500 to 450 Length of Reaction Zone R 500 ft. 500 to 300 Temperature at Top of Reaction Zone 450°F 300 ° to 55 Temperature at Bottom of Reaction Zone 470°F 300 ° to 65 Pressure at Top of Reaction Zone 410 psia 200 to 193 Pressure at Bottom of Reaction Zone 650 psia 433 to 2600 2. Influent Fluid with Reactants Sewage Sludge Waste Stream C . O .D . 7600 mg/liter 0 to 20 , 00 Pressure ( surface) 0 psia 0 to 200 p Temperature Atrros. Ambient Atrros. Ambie Flow rate About 3 gpm 0 to 500 g TABLE (cont'd.) Example Range Air Pressure 100 psia 0 to 200 psia Temperature Atmos. Ambient Atmos. Ambient Flow Rate 1. 52 cfm 0 to 500 cfm Bubble Velocity . 70 f t/sec 0 . 5 to 2.5 ft/sec 3. Effluent Fluid Pressure 80 psia 0 . to 200 psia Temperature Atmos. Ambient Atmos. Ambient Flow Rate About 3 gpm 0 to 500 gpm 4. Output Energy Btu/Day . 67 x 10 6 8 0 to 10 x 10 C.O.D. Reduction 70% 0 to 99% Amount Throughput C.O.D./Day 112 lb/day 100 to 100,000 lb/day C.O.D. Flow Rate 3 gpm 0 to 500 gpm Raw Sewage Equivalent* 72,000 gpd 45,000 to 64x10 gpd * = at 1,5600 Ib/C.O.D. per million gallons of raw sewage INDUSTRIAL APPLICABILITY In summary, the method and apparatus of the present invention accomplish a high temperature, high pressure, chemical reaction including the wet oxidation of sewage sludge and other fluid waste but require only low pressure pumping apparatus. Both the initial costs and the operat¬ ing costs are considerably less than other known methods and apparatus achieving similar end results. In addition, the method and apparatus of the present invention require a minimum of low skill maintenance and produce energy in the form of a high quality steam. The invention achieves essentially a 100% destruction of all living organisms and about 98% reduction in the C.O.D., is odorless, and produces a readily dewaterable ash end product. In the present invention all of the control is in the area of the ground surface, there is a minimum power require- ment for pumping relatively large quantities of fluids, and there is a continuous downflowing and upflowing flui flow throughput. The method and apparatus disclosed is suitable for carrying out high-temperature, high-pressur chemical reactions as, for example, in the cracking of petroleum products and for carrying out high-temperature, high-pressure hydrogenation such as in the forming of am in which case the enlarged bubbles would not be necessar

Claims: WHAT IS CLAIMED IS: 1. In a method for effecting accelerated chemical reactions between at least two reactants, the steps of: flowing an influent fluid with at least two reactants downwardly through a downgoing flow passage at a selected flow rate to a selected depth below the ground surface to form a hydrostatic column of fluid exerting a pressure and provide a temperature sufficient to cause the reactants at said selected depth to react at an accelerated reaction rate and pass further down through a reaction zone extending through said downgoing flow passage a selected distance below said selected depth whereby reaction products are produced and the fluid is heated in said reaction zone, flowing the heated fluid and reaction products from said reaction zone back up to sub¬ stantially ground surface level in an upgoing flow pass¬ age in heat exchange relation to the downflowing fluid as an effluent fluid; and controlling the temperature of the influent fluid in said reaction zone by adding heat to or removing heat from said influent fluid substantially in the -area of said reaction zone to accomplish a maximum reaction rate with the vapor pressure of the influent fluid at the local temperature being maintained always lower than the local pressure to prevent boiling of said influent fluid. 2. In a method as set forth in Claim 1 wherein one of said reactants is a stream of gas introduced under a selected pressure into the influent fluid substantially at the ground surface level through an outlet facing the downstream end of said downgoing flow passage to form a series of enlarged gas bubbles that are carried down with the influent fluid to cause intense mixing and con¬ tacting and maximize the reaction in the reaction zone and reduce pumping requirements. 3. In a method as set forth in Claim 1 wherein on of said reactants is a gas that is introduced at a plurality of selected depth intervals below the ground s face level as successive streams at progressively higher pressures. 4. In a method as set forth in Claim 1 wherein the pressure of the influent fluid at substantially the ground surface level is in the range of about 0 to 200 psia at substantially atmospheric, ambient temperatures with a continuous downflowing and upflowing fluid flow throughput. 5. In a method as set forth in Claim 1 including the step of_ controlling the pressure and flow rate of the influent fluid and effluent fluid at substantially ground surface level. 6. In a method as set forth in Claim 1 including the step of controlling the .concentration of said reac¬ tants in relation to one another and in relation to the amount of liquid content of the influent fluid. 7. ' In a method as set forth in Claim 1 wherein sai effluent fluid is successively recycled back down as influent fluid and up as effluent fluid in a succession of downgoing and upgoing flow passages disposed in a common hole coupled in series for carrying out a succes- sion of chemical reactions on a continuous stream of fluid, the effluent fluid from each successive reactor being passed into a tank " open to the atmosphere to remove gaseous reaction products. 8. In a method as set forth in Claim 1 wherein sai influent fluid is sewage sludge delivered to the downgoin flow passage at a selected flow rate and selected pressur and one of said reactants is air with oxygen to perform the wet oxidation of sewage sludge. 9. In a method as set forth in Claim 1 including adding heat to said influent fluid substantially in the area of said reaction zone to initiate the reaction. 10. In apparatus for effecting accelerated chemical reactions, the combination comprising: a reactor including first and second pipe portions defining a downgoing flow passage and an upgoing flow passage in heat exchange relation to the downgoing flow passage, said downgoing flow passage extending from substantially the ground surface to a depth sufficient to cause a downflowing- fluid therein to form a hydrostatic column of fluid to exert a pressure and provide a tempera¬ ture sufficient to cause two reactants in the fluid at said selected depth to react at an accelerated rate, said down- goingflow passage extending down from said selected depth to form a reaction zone whereby reaction products are produced and said fluid is heated in said reaction zone; means for pumping an influent fluid with at least two reactants from substantially the ground sur- face level through said downgoing and upgoing passages whereby an effluent fluid with reaction products is passed from said reactor; and means for controlling the temperature of the influent fluid in said reaction zone by adding heat to or removing heat from the influent fluid in the area of the _eaction zone to maintain a substantially maximum reaction rate without boiling of the fluid in said reaction zone. 11. In apparatus as set forth in Claim 10 wherein said first and second pipe ' portions are arranged with one in concentric spaced relation within the other with the outer pipe portion being closed at the bottom forming a hydraulic flow-through ϋ-tube. fr IPO 12. In apparatus as set forth in Claim 10 wherein said reactor-is disposed in a subterranean cased hole providing a subterranean housing for but separate from said reactor. 13. In apparatus as set forth in Claim 10 wherein said first and second pipe portions are supported in a depending manner from a common support plate at the grou surface level. 14. In apparatus as set forth in Claim 10 wherein said pipe portions are reduced in size at a selected dep below the ground surface substantially at the upper limi of the reaction zone to maintain a substantially constan velocity through said pipe portions. 15. In apparatus as set forth in Claim 10 includi pumping means in the area of the ground surface level fo flowing the fluid through said upgoing and downgoing flo passages in a continuous throughput flow. 16. In apparatus as set forth in Claim 10 wherein said means .for controlling the temperature of the influe fluid includes a jacket with an inner annular passage surrounding and in heat exchange relation to the outer of said pipe portions through which a coolant fluid is pumped and further includes a pair of flow lines coupled to said jacket and extending up to the ground surface level to circulate a fluid to and from said jacket to th ground surface level. 17. In apparatus as set forth in Claim 10 includi a tank, a pump, a heat exchanger, a control valve, and a heat source in the area of the ground surface level coup in a fluid flow circuit with said jacket and flow lines for heating and pumping a heated fluid into said jacket in one mode of operation and for pumping heated fluid fr the jacket through said heat exchanger in another mode o operation to control the temperature of the fluid in said reaction zone. 18. In apparatus as set forth in Claim 10 including means for introducing a stream of gas under a selected pressure into the downgoing flow passage in the area of the ground surface level to form enlarged gas bubbles commonly known as Taylor bubbles, characterized by a generally cylindrical main body portion, a generally spherical cap portion, and a truncated portion opposite said cap, that are pumped down with the influent fluid. 19. In apparatus as set forth in Claim 18 including a plurality of inlets for said stream of gas located at spaced selected distances below the ground surface level. 20. In apparatus as set forth in Claim 18 wherein said means for introducing a stream of gas includes a terminal pipe section in the downgoing flow passage arranged longitudinally of the passage with an outlet opening toward the downstream end of said downgoing flow passage. 21. In apparatus as set forth in Claim 10 including a plurality of reactors disposed side-by-side in a single well casing, said reactors being flow-coupled in a series relationship with the influent fluid passed into one of said reactors and the effluent fluid from said one reactor into the next reactor to successively recycle the fluid back down for further reaction for carrying out a succession of chemical reactions on a continuous stream of fluid. - JRE OMPI

Inventors: MCGREW J
Applicants: MCGREW J
Application year: 1979
Main classification: C02B3
IPC codes: B01J3, B01J19, C02F1, C02F11