• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    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.
    公开号:SU1088648A3
    申请号:SU792843820
    申请日:1979-11-16
    公开日:1984-04-23
    发明作者:Лининджер Макгру Джей
    申请人:Джей Лининджер Макгру (Фирма)；
    IPC主号:
    专利说明:

    hydrostatic fluid column and conducting chemical reactions at well depths at elevated pressures and temperatures, it is equipped with coaxially mounted bore pipes forming the downward and ascending channels to the reaction zone located in the lower part of the well, connected to the channels and as a U-shaped hydraulic shutter.
    8. The installation according to claim 7, which is equipped with a base plate located on the surface of the earth, and the pipes are fixed to the base plate.
    9. Installation according to Claim 7, characterized in that the pipe is made with a diameter that is less than the surface of the earth.
    10. Installation according to claim 7, characterized in that the temperature control device is in the form of a tubular heat exchanger.
    11. The apparatus according to claim 7, wherein it is equipped with a device for creating elongated gas bubbles connected to the descending channel.
    12. Installation by PP. 7-11, characterized by. in that it is provided with nozzles for introducing a gaseous reactant connected to the downstream channel and located one above the other at the height of the well.
    13. Installation on PP. 7-12, which means that the nozzles for introducing the gaseous reactant are installed along the axis of the descending channel with the output end placed in the reaction zone.
    one
    The invention relates to a method for carrying out chemical reactions, in particular, to a new and improved method and apparatus for carrying out accelerated chemical reactions, particularly effective in carrying out wet oxidation of wastewater and similar polluted streams, in water clarification, as well as in the utilization of energy as heat.
    A number of chemical reactions are known, which can be accelerated at a temperature that considerably conditions the ambient temperature above the surface and at a pressure substantially higher than the atmospheric pressure. Until now, most of the reactors designed to perform various chemical reactions at elevated temperatures and pressures usually required the installation of high-pressure liquid pumps, heat exchangers operating under high pressure and high temperature, and pressure vessels with rotating seals, also significant land area.
    The Zimpro method, the Barber-Coleman process and the Navy shipboard installations used for direct wet oxidation of wastewater are known, all of which include the introduction of waste into a reactor operating at high temperature and under high pressure, which is essentially at ground level. Air is injected into the reactor and heated outside. Continuous mechanical stirring is required to mix the oxygen (reactant) with the liquid and to remove the carbon dioxide of the reaction product.
    The closest to the invention to the technical essence is the method of conducting underground chemical reactions by supplying a reagent. combo, at least one of which is liquid, into a vertical well drilled in the ground, downstream channel, creating hydrostatic pressure due to a column of fluid in the well, contacting reagents in the reaction zone located in the lower part of the well, forming reaction products, heating the reaction mixture, and the heated reagents and reaction products emerge to the surface of the earth through the ascending channel, and heat exchange in the descending and ascending channels, as well as controlling the temperature and pressure of the reagent ntov in
    5 well.
    A known installation for carrying out this method includes a vertical well drilled in the ground and located in a well.
    0 a reactor, a device for feeding reagents, connected by pipeline to a reactor, and a device for controlling the temperature, pressure and consumption of reagents 13.
    5, in a known installation, air is introduced into the base of the reactor. Introduced bubbles have minimal dimensions with a large total surface area. Such bubbling increases the pressure difference and limits the rate of reaction due to the restriction of the flow of reagents and products through the boundary layer, resulting in the need for a much larger pumping power to pass liquid through the system than in a system using large bubbles. Excess heat is collected from the dT device by diluting the incoming reagents or by releasing steam. Dilution of the fed reagents reduces the overall performance of the treatment process and increases the specific cost of treatment. In a known installation, additional support is required for the channel for the central stream and a plurality of floats for this purpose. In addition, it has limitations for any oxidation reactions by the amount of oxygen present in the material. Additional air or oxygen is not fed into the waste stream at all. Such a method, wastewater treatment is not desirable, because it leads to the pyrolysis of waste and the resulting, as a result of free carbon and other undesirable products. According to this method, a continuous supply of heat is required to carry out the reaction. The heat input rate regulates the flow and creates a thermal head ensuring that the liquid exits the reactor. Placing the steam line in the drain leads to a loss of energy, which is taken up by the liquid, to an increased energy demand and an increase in the cost of the production process. The aim of the invention is to intensify the process by achieving a maximum chemical reaction rate and eliminating agent boiling down the well, as well as intensifying the process by creating a hydrostatic liquid column and driving chemical reactions to the depths of the well at elevated pressures and temperatures. The goal is achieved by the method of conducting underground chemical reactions by supplying reagents, at least one of which is liquid, into a vertical well drilled in the ground, downstream, creating a hydrostatic pressure due to a liquid column. in the well, contacting the reactants in the reaction zone located in the lower part of the well, with the formation of reaction products, heating the reaction mixture., outputting heated reactants and reaction products to the earth’s surface ascending controlling the temperature and pressure of the reagents in the well; controlling the temperature by heating and cooling the fluid directly in the well and in the reaction zone; the temperature of the reagents in the well and the reaction zone is maintained below boiling points of the liquid, and the pressure is maintained at a higher pressure. At the same time, as one of the reagents, a gas is used which is introduced into a liquid on the surface of the earth into the descending channel with the formation of a successive series of UD. . The gaseous reagent is injected into the fluid below the surface of the earth in the form of jnoTOKOB parallel and located above each other with a height of the gas as the distance from the surface of the earth increases. The fluid pressure on the surface of the earth is maintained at 14 MPa. . In addition, the liquid exiting the upstream channel is recirculated by returning it to the downstream channel, and the liquid coming from the upstream channel is degassed and cleaned of gaseous reaction products before it is recycled. Waste water is used as a liquid, and air with oxygen is used as a gaseous reactant. An installation for carrying out this method, comprising a vertical well drilled in the ground, a reactor located in the well, a device for supplying reagents, a pipeline connected to a reactor, and a device for controlling temperature, pressure and consumption of reagents, is fitted with coaxially installed pipes forming the downhole and the ascending channels and the reaction zone located in the lower part of the well, connected to the channels and made in the form of an i-shaped hydraulic gate. The installation is equipped with a base plate located on the surface of the earth, and the pipes are fixed on the support pin. The pipes are made with a diameter decreasing from the ground surface. .
    The device for temperature control is made in the form of a tubular heat exchanger.
    The installation is equipped with a device for creating Taylor elongated gas bubbles connected to the descending channel.
    In addition, the installation is equipped with nozzles for introducing a gaseous reagent connected to the downstream channel and located one above the other along the height of the well.
    Reagent inlets for the gaseous reactant are installed along the axis of the descending channel with the outlet end placed in the reaction zone.
    The gas inlet device is made in the form of a pipe located along the axis of the descending channel with the output end placed in the reaction zone, the coaxial pipes form several reactors connected in series.
    The incoming liquid stream is pumped through the downstream part of the pipe from the level of the zeipi surface at selected controlled temperatures, pressures and flow rates to a selected depth below the ground surface to create a hydrostatic column sufficient to provide the selected pressure and temperature at which the reactants interact with each other. speed, and then the downward part of the pipe passes through reaction zone B during the selected residence time, as a result of which heat is generated in this zone, forming with reaction products and the heated liquid. The heated liquid and the reaction product enter the upstream part of the pipe, exchanging heat with the downward liquid to cool it down before leaving the upstream part of the pipe. The temperature of the liquid entering the reaction zone is controlled by introducing or removing heat to maintain the maximum reaction rate and to prevent boiling of the liquid in the reaction zone. The process is carried out in such a way that the heat of the exothermic reaction is recovered as useful thermal energy.
    If gas is used in the reaction, the results are improved by introducing a low-pressure gas stream B in the form of a series of elongated bubbles (Taylor bubbles) formed at the top of the reactor. In a preferred embodiment, the gas is introduced as multiple streams at several elevations in order to reduce heating costs. These elongated bubbles cause the smallest pressure drop in the channel and thereby minimize the discharge pressure.
    to maintain a certain flow rate. These enlarged bubbles also provide vigorous stirring and contacting to increase the flow of reagents and products into and out of the liquid, as the liquid flows over the belly and no boundary layer is formed, then the formation of a boundary layer takes place for smaller bubbles. The amount of injected gas is regulated to ensure accurate relations to the incoming liquid, since a lack of gas leads to the formation of undesirable products, and an excess of gas is cleared and reduces the productivity of the reactor. The flow rates of the flow are maintained higher than the speed of the bubble rise so that each bubble can descend into the reaction zone. The pressure and productivity of the reactor are regulated in order to maintain the corresponding values of these parameters in the system.
    Figure 1 presents the scheme of the proposed device when using gas as the sole reagent; Fig. 2 is a schematic of the device showing the method for introducing pressurized gas into the fluid flow to form enlarged bubbles passing down through the outer cannula and upwards through the internal channel; Fig. 3 is a diagram showing channels and bubbles whose movement is opposite to that of the bubbles in Fig. 2; FIG. 4 is a diagram of the reactor with the designation of different depths; FIG. 5, the upper part of the reactor, section; FIG. 6, section A-A ya of FIG. 3 of FIG. 7, the reactor hour, the vertical section; Figure 8 shows the lower part of the reactor, vertical section; figure 9 is a cross section of figure 7; figure 10 is a section bb In figure 9; in fig. 11 section GGD 7; in Fig.12, the section DD in Fig.7; on Fig section E - E on Fig; in fig.
    14- section Ж-Ж on Fig; in fig.
    15 - section 3 - 3 in FIG. in fig. 16 is the fluid flow between the casing and the current line, vertical section (as shown in FIG. 13); FIG. 17 is a sectional view of FIG. eight; in Fig. 18, the cross section K-K in Fig. 17; Fig. 19 shows the bottom of the reactor shell, an axonometric projection; on Fig - side view of the bubble Taylor; on fig.21to, bottom view; on Fig - diagram of the three reactors connected in series and placed in one outer casing.
    Reactor 1 is installed in a well drilled in the ground, and is below level 3 of the surface of the earth. The reactor 2 has an outer pipe part 4 and an inner pipe part 5 concentrically located with respect to the outer pipe part 4, a channel b between the outer and inner pipe parts and the inner channel 7 in the entire inner pipe part 5. The outer pipe part 4 has a cap 8, covering its lower part, and the inner pipe part 5 ends at a selected distance above the plug 6 to form a deep hydraulic structure of the i-shaped hydraulic pipe in the borehole 2. The reactor 1 also has an upper part, ayuschuyu above the level 3 zem hydrochloric surface with an opening 9 associated with the passage b through kotoryy.te Thu The incoming liquid, and openings 10 associated with the inner channel 7 through which the flow .otvodits 1zhidkosti. The flow of the incoming flow. As the liquid flows down to the channel b and to the top of the internal channel 7, it provides greater flow through the input streams, which usually have a greater viscosity than the output streams, however, the direction of the flow can be reversed (Fig. 3). A low pressure pump 11 is installed at the ground level for pumping feed liquid from the feeder 12, through line 13 with pressure regulator 14 at selected pressure through port 9, through line 15 between the pump and. hole 9, the fluid is descending through channel b, as indicated by the arrows. A bypass valve 16 installed in the bypass line 17 bypasses the pump 11 to remove the flow directly from line 13 to line 15, since after the liquid passes through the u-tube, in many cases pressure is not required to maintain a constant flow through the pipe. A check valve 18 on the outlet line 19 controls the flow and pressure of the outgoing fluid flow through the valve 7, using the size of the valve opening. The feed fluid from the feeder 12 is withdrawn via line 13, and its flow is controlled by the regulator 14. Pump 11 controls the pressure and flow during the start-up period, and valves 16 and 18 control the pressure and flow rate during the operation of the device. The device (Fig. 1) is suitable for carrying out direct wet oxidation of polluted streams and, in particular, for installing aerobic wastewater treatment, applicable for a series of high-temperature chemical reactions proceeding under high pressure. in a scheme where wastewater is processed, a bypass stream (fluid from line 19 enters the sump 20, from where the purified water is recirculated back as pure or purified diluent and feed line 13 through line 21 with valve 22 to adjust the concentration of feed liquid. By setting valves 23 and 22 receive a mixture of feed fluid having a selected amount of SOD. The amount of oxygen needed to complete the oxidation reaction is called chemical oxygen consumption (soda) with waste water. The line 24 for the removal of purified water and the line 25 for the removal of ash .. The device for adjusting the apparatus is designed to control the temperature of the incoming liquid in the reaction zone 26. This device for adjusting the temperature includes a cooling pump 27 installed at ground level, which pumps the cooling the liquid stored in the corresponding tank 28 at ground level, through the heater 29 (at ground level) into the lower part of the jacket 30 through the pipe 31 with the regulator and is discharged from the jacket along pipe 32 with a regulator. Heater 29 may have different shapes, but as shown schematically, it is an electric heater, which is supplied with electrical power from a power source 33 with an adjustable rheostat 34 to control the voltage applied to the heating element 35 to change the set heating temperature and thereby the temperature coolant flowing through pipe 31. Shirt 30 is a hollow annular cylindrical structure that is almost the same length as reaction zone 26 and, besides It exchanges heat with channel 6. Pipe 32 is connected to the upper part of the reaction zone jacket, reaches the ground level and is brought to tank 28 in the form of return line 36 with a regulator for supplying heat to the flow in pipes 31 and 32. Chain to remove heat, it includes a line 37 with a regulator attached to the pipe 32 descending to the top of the jacket 30, and a pipe 38 with a regulator above the ground surface attached to the heat exchanger 1ku 39, which in turn is connected to the vessel 28 with the creation of a closed temperature controlled chains bones. The regulator in the pipe 38 controls the flow rate in this circuit.
    By adjusting the temperature of the coolant in the jacket 30 and the pipes 31 and 32, the temperature of the incoming liquid in the reaction zone 26 is controlled. This is achieved by adding or removing heat from the coolant, which is adjusted so as to achieve almost the maximum reaction speed. the vapor of the incoming liquid at a local temperature maintained always below the local pressure to prevent the incoming liquid from boiling, the temperature of the incoming liquids are raised by the addition of heat produced by the heater 29, which heats the cooling fluid, passing through the pipe 31 into the jacket 30 with the help of the pump 27. The flow rate of the cooling liquid is controlled by installing a regulator in the pipe 31
    The upper limit of the temperature of the incoming liquid in the reaction zone is controlled by the amount of heat removed from the heat exchanger 39, and the flow rate controlled by installing the valve in the pipe 38. The amount of heat removed is directly related to installing the valve in the pipe 38. A turbine 40 is connected to the heat exchanger 39 with the help of the .41 line with a regulator for utilization of energy and, in particular, the heat produced as a result of the reaction, with the conversion of thermal energy into mechanical energy. In another embodiment, a load 42 is connected to the heat exchanger via a line with a regulator, which may be a heated room.
    A pressure sensor for measuring the distance at the upper boundary or at the beginning of the reaction zone 26 includes a small diameter pipe 43, such as a stainless steel tube, passing downward through the inner tube portion of line 15 to the upper boundary of the reaction zone 26. A vessel 44 is installed at the surface of the earth air under the selected pressure down through the tube 43 by means of the discharge valve 45. An air pressure gauge and a pressure regulator 47 are installed between the vessel 44 and the tube 43. To measure the pressure, the tube 43 is flushed out; the water and the discharge valve -45 are closed. The gauge 48 reading is the pressure inside the reactor at the top or top of the reaction zone, which is an important part of the temperature and pressure in the reactor.
    In chemical reactions, where gas is used as a reagent, and especially when
    wet oxidation of wastewater, which requires the presence of oxygen in the air, the operation of the facilities and the results are significantly improved. When using, the Taylor gas bubbles 49 are enlarged. These pu ri have a spherical upper part 50, a cylindrical part 51 and a truncated lower part 52. The cross section of the bubble is em is a circle. The main part of the bubble diverges from the top downwards along a curved line. These bubbles are often called Taylor bubbles. Taylor bubbles are compressed as they flow through the outer channel, and after reaching the reaction zone, the delivered oxygen reacts, which causes intense mixing, contacting and rapid oxidation of the wastewater, and the bubbles return through the inner channel.
    The principal advantages of using these bubbles, as compared to the mass of very small bubbles, are that the pressure drop per unit length of the Taylor bubble tube is much smaller, thereby reducing the pressure for pumping fluid and bubbles deep into the earth, and the high rate of mass transfer between the gas and the liquid phase in the reaction zone 26. This leads to improved mixing in the gas-to-liquid system with a large frying of the gas in the liquid and to a greater extraction from the liquid such as are for reaction.
    The device for producing enlarged bubbles is an air compressor 53 mounted on the surface of the earth, which, through one or a number of lines, injects one or more npii air flows at a certain pressure into the upper 4aqTb of the outer channel for. fluid connections from feed line 15. A series or chain of enlarged Taylor bubbles 49 is formed, which travel downwardly with the incoming fluid.
    For this purpose, a valve 54 installed on a line 55 entering line 15 near the surface of the earth, and a valve 56 in line 57 submerged to a certain depth below the level of the surface of the earth, and a valve 58 in line 59 passing deeper from surface of the earth. The end portions of each of Li, 59, 57, and 55 extend longitudinally inward into the descending channel, and the outlet of these lines is open in the direction of flow in the downward channel, so that air flow with a selected pressure and flow rate is introduced into the incoming flow
    fluid. By appropriate selection of pressure, temperature and flow rate with respect to the flow rate and pressure of the incoming fluid, the bubbles merge into a chain of Taylor bubbles 49 that are spaced from each other and located in channel b,
    These enlarged Taylor bubbles rise at the same rate. in relation to water. Their relative velocity with respect to water is expressed by the equation
    , 46l9cr,
    where, 2 ft / sj
    t- is the inner radius of the pipe,
    feet
    In the device, the flow rate of the contaminated liquid should be maintained higher than the rate at which the bubbles rise, so that each bubble reaches the reaction zone 26. The incoming liquid flows over the bubble and increases the mass transfer between the liquid and gas phases in the reaction zone. Since the oxidation reaction as a whole is of the first order, the reaction rate is directly proportional to the amount of products and reagents in the liquid. Taylor blisters provide less pressure loss inside the channel compared to a mass of smaller puzelray, blah. This reduces the amount of energy required to push a material at a certain speed through an i-shaped tube. Smaller bubbles create large pressure losses in the hydraulic column. In addition, small bubbles have a boundary layer of water, which slows down the mass transfer between two phases. In this way, the Taylor bubbles are maximized, or the reaction speed, minimizing the power required to inject fluid through the piping system.
    To minimize the power consumed by the compressor 53, air is introduced at the top of the channel b at several elevations (Figures 1 and 21. At the highest elevation, air is introduced at the lowest pressure equal to one volume of air per fluid volume. As the fluid lowers the pressure increases and the air is compressed. Additional air is introduced at the lowest mark and, correspondingly, at higher pressures, but in an amount equal to one volume of air per fluid volume. increasing depths minimize the power requirements of the compressor and provide the system with the oxygen needed to oxidize the reagents in a liquid.
    The pressure at any point of the reactor depends on the mass of liquid above this point. When using water alone, the pressure gradient will be about 0, 43 pS per foot, 10.1 feet / m. Depth. However, channel 6 contains a substantial amount of gas that is compressed and heated by
    as you move down.
    In general, due to the introduction of air at different elevations below ground level, less pressure is required, and
    installation operation, the downward flow of the incoming liquid material moves without the need to install a liquid pump. This Taylor bubble shape reduces to
    minimum power requirement
    the compressor creates the smallest pressure drop and increases the flow of reagents and products into and out of the liquid as the liquid flows over the bubble, and there is no boundary layer present in smaller sized bubbles.
    The reactor shown in FIGS. 5 to 10 is located in a well, lined from the inside by a casing pipe, which consists of pipe 60 and pipe 61 with external cement filling 62, which is located in pipes 61 and 60 and has a cement plug 63 that closes and seals the bottom casing. The upper end of the casing is attached, for example by welding, to a circular plate 64 mounted flush with the surface 3 of the earth. Usually external 4 and internal
    5, the tubular portions are independently suspended with respect to the plate 64 so as to expand and contract against the casing with temperature changes.
    The upper end of the outer pipe
    Part 4 is attached, for example by welding,
    to the round plate 65, resting on
    plate 64, to reinforce the outer
    tubular part 4 is suspended relative to the casing. Two pipes 31 and 32 pass through the hole in the plate between the casing and the outer pipe part for supplying and discharging fluid from the jacket 30.
    In addition, above the ground level to extend the outer pipe portion 4, a straight sleeve 66 is provided, dressed on the outer thread of the upper part, pipe
    Part 4, attached to the plate 65, is at rest. on the plate 64, the nipple 67, the tee 68 and the pipe 69 with a flange 70 attached, for example by welding, to the upper end and with the lower end,
    screwed into the tee 68. A flange 70 is installed on the flange 70, to which the rifle is fixed to the upper part of the inner pipe part 5, for example by welding, such as; the inner pipe part) is installed in the suspension of the 1st socket from Vc; the gelg1 of the outer pipe of part 4, which in turn rests on the plates 64 and 65, and a / 1 has the third pp 72, which is screwed Nitpo-Gb 73 with a prigreglyonno vtop-pP 74 dpm 1; 1) and the connection of line 19, through which the OTXcr.riiuo fluid flows, Kip N56, between flanges 70 and 71 is installed iipOKJ: aj.Kn 5, and between flanges 71 and 72 - proyu.tska 76 together with a fastening bolt 77 to: hold fanyek pmesgge uplet een and Heirpoin. :: -; :::; ; .tcpt tube 43 yes, Trubna chastg, 5 in the hour and to and d and in l with i: vi. overhead; / Earthen ground with ilijraiiuGM 7, for the air from the surface through the plate 65, two pipes 31 and 32 fixed on Hapiy are provided: xHof; The surfaces of the tubing are 5- and (T), 9 and 10. Each line of the cooling fluid has a number of sections, liOKasaHiiux in a very rigid pipe; ; ; i order 30 i 5 m and ggb1; I. hose 79 is not shown ;: 5 / d1; -; ь: l yuritska 0.7:.;:: - and.: H; ji are between the ends of the SOTOR; -L: 30 "ytny. using J..TV.i-: i; i rigid trub; 78 OTiipae C4 on bearing G; lake; ; ; lg e IO to PC J; jj ti - by 31, r; p.; - n - jCij: et mugo to the outer tubular SShTD: -1. Support Kpotr-TOiu; 82 slides along the top: towards the end of the outer pipe part 4 in the direction of M and has an opening 83, which, in turn, has an elastic sleeve 84. The hard tube 7B has an axial movement in an elastic groove and thus this line can axially displace with temperature changes. The sleeve 80 pas the lower end slides along the tube 78 and the upper end, the sleeves 80 is held by the bracket 81. The flexible pipe 85 can be: 3roTOB: iefia from bellows-like: covered pipe with a heat-resistant coating. The outer pipe part 4 (fkg.7 and 8), passage: gave from the surface of the grain to the well, consists of a plurality of connecting shafts; i 36, which are made using sleeves 87. These bushings have a cut part on every; end and are standard tube sleeves for the sk; The pipe sections forming p) are in the outer part 4 above the reaction one, manufactured 1 {b; from dark-gray cast iron with OSL 1 stainless steel; oi1, e1 o tmbinx, 88 I, bjHi.li and 12 pass from the reaction zone up to a depth below the surface of the segchi, an example of 152 g - / .. prevents corrosion. In the same way, the inner tube part 5 is made of the pipe valve section 89, which are connected by welding, Dnil:;, e 1; the outer pipe part 4 .5f is 3ai-j; yiu-8 in the shape of a hemisphere for the avoidance. blocking p-: l3.iва,; -; the great one directs the flow upwards through r: morning 0 pipe part 5. There is no pressure drop across the wall inside; -1he: san..ala ripHi.iennett thin-walled pipe that the mind : - ;. It values the cost and improves the hot flow o: i; i go HOCjie 1: ;; liquid ejection and cold one i raw untreated 1; |, it; oi, og. 30 on the outer pipe line; -1 is located at a selected depth below the ground-level surface permeability, which is located at the top or at the beginning of the reaction zone 26. On this city there are both}: -; b as well as inside: pipe parts are reduced in size to provide a McAlcoBoiO pro-active constant. As the IPR and the outer channel flow, the gas with:} -: imaesl, and as a result, the ratio of gas to liquid decreases with c. с о п у т about t r y; с ;;; i m u n it e n i eat fast t ;; i liquid. To maintain the grief of the liquid more; close to constant, non-impersonal in the area of the reaction zone, the size of the outer and inner pipe parts is reduced. This. Umenhesh-; e increases the yield of non-capital investment; and also maintains at least the speed that is required to push the gas down to the bottom of the gas. At some distance above the reagay zone (Fig. 11), the pipe to section 5 as section 90 has a sleeve 91, in KOTOpyic; -, O7; avlena of the inner pipes; -; ai se1, h;, and: 92 I am of the last 11 meters. The external tubular section 93 (FIG. 12 | below the sleeve 91 and above the reaction zone has a sleeve or sleeve 94, which in turn has an inner hole in which the outer pipe section 95 has a smaller diameter, and preferably the outer pipe section 93 made of dark gray cast iron, lined with stainless tubing -; 88 over sleeve 94, which passes through up to 152 m below the overhead, was closed. Reducing sleeves are made of stainless steel and treated to a smooth rsonusny entrance surface to prevent Without clogging, the large tubular section 96 is fastened along the outer ring of sleeve 94 at some distance about section 95, forming a shirt 30 passing to the reactor wall. Heat of reaction is collected in jacket 30 and removed from it, the heat can be supplied in the form of a heated fluid:; a liquid and / or steam to start the reactor; at the top of the jacket 30 there is a 9/7 fitting, at the fanning on the pipe section 96. shirts. At the bottom of the outer pipe section 96, which forms the jacket, the bottom 98 attached to it by welding or a threaded connection has a vertical hole 99. The fitting (, FIGS. 17 - 19) is attached, for example by welding, to the bottom 98 and protrudes outside of one side of the plug . The fitting 100 has a crochet opened in the bottom of the shirt, and a hole 101 at one end, attached to the pipe 31, the Shirt with the bung and fitknot ends at a certain distance over G3, which provides them with a return-slip movement relative to the plugs 63 at the extension and compression. temperature control on; - outer pipe 1; oh part: 11 there are temperature sensors in the form of o / Ermo par 102 (Fig. 4) with an i-slot about 76 m, which are attached / dip; to temperature index 103 vro uroane surface. The presence of water inside the pipes 60 and 61 causes great heat loss. This water will evaporate and reach levels of the refrigerator where it condenses and flows down the outer surface of the wall of the reactor. until it evaporates again. This refluxing reduces the overall energy efficiency and process capability. To prevent this problem, the internal cavity of the casing can be dried by calcining or blowing, or it can be insulated with an insulation layer 104 (Figures 8, 17 and 18). Effective insulation for this purpose can be a plastic-coated fiberglass sheet, i.e. intrinsic silicate wool or ceramic felt, which serve as a barrier to prevent heat loss by conduction and convection. The device works as follows. The incoming liquid is a sewage flow, pumped from feeder 1 through lines 13 and 15 into channel 6. Air pressure under pressure is injected into the outer channel to form a chain of Taylor 49 bubbles spaced from each other, and the pressure provided by pump 11 is sufficient to move down both the incoming fluid and the bubbles through channel 6. As the material descends below the surface of the earth, tampere; yy and pressure increase j; The reach of the point at which SA.i-lele n: ;; C, comes at a higher speed, -. smeared at line 105, towards pro j.ei ;;;. to peairropa 106. In the reaction zone — ood -.-.:;); and, with an increased Tui / iUopaType, oxygen is rapidly mixed with water; retiring the rapid glazing of the mountains; and: their solids and expression: .. l: Ea heat to heat the liquid ::,. liquid and reconnaissance products;:;; Calibrated outgoing liquid, then enter the inner rope; 7 and are warmly agglutinated (flow through the incoming liquid stream. After leaving the reactor, the effluent liquid passes through the sludge, nickname, and then either is used as a diluent inlet g: –Telee gas flow meter; Sy1, c-th SOD value, or is reset on line 24, - The mixture or concentration of reagents is dependent; ;; of soda, stan: m of liquid (lod:) in the incoming liquid is controlled by setting kg; ApanoB 58, and 54 each other. and DG; -1Y from the regulators is adjusted ussganagli-li: chaegs at surface level traction of the earth.When starting up to the resi; the dionnsezke usually supplies heat to the hydraulic fluid of the incoming fluid by pumping the cooling fluid from 28 through the heater: - 29 through the pipe 31 through the jacket and back up through the pipe 32. O 4 C at the B eir of the reaction zone boundary and W1;; from the exothermic reaction, the direction — flow of coolant is pipes 31 and 32 is reversed (reversed), and OHfi is pumped out of the jacket — up the pipes 31 to 38 in the heat exchanger 39, of which t The unit can be retracted to heat the load example of a room, or discharged as heat or PC bots operated by a turbine 40. The temperature at the beginning of the reaction is controlled by changing the setting of the rheostat 34 and the flow rate in the tube 31; liquids at a local temperature are large; .e low than local dilation
    Preventing boiling at maximum reaction rates.
    FIG. 22 shows the proposed device in which three underground reactors 106-108 are installed in one outer casing 109 for greater productivity in a single vertical shaft of a shallower depth than would be required for a single long reactor. The 06-saddle pipe also has a cement lining inside the well and a cement sealing plug 110 at the bottom. The space of the reactors and the common pipe is insulated with a single pipe 111,
    Each reactor has an outer tube section and an inner tube section to which devices are connected for inlet and outlet above the surface of the plug. In the proposed device, there are a tank 112 for the reactor 106, a tank 113 for the reactor 107 and a tank 114 For the reactor 108, For each reactor a pump 115 for a fluid is connected and an inflation compressor 116. The incoming liquid, shown by line 117, is pumped under pressure into the tank 112, from where it is sent to the reactor
    106 in countercurrent with the liquid flowing out of the reactor 106 entering the vessel 113. The liquid entering the CS and vessel 113 and the gas is fed to the reactor 107 and the waste; - 1, rk from the reactor
    107 liquid is pumped into vessel 114. Finally, the outgoing liquid and gas under pressure are pumped out of vessel 114 into reactor 108, and the liquid flowing out of reactor 108 is directed to the point of use.
    on line 118,
    Such a device of three series-connected reactors increases the reduction of SOD (reduces chemical oxygen demand,) compared with one reactor, due to the fact that the resulting reaction can remove CO through tanks 11.2 and 113. 5 In general, we offer The method and the device are a description of a chemical reaction at high temperature and high pressure, such as wet oxidation of wastewater and other contaminated liquids, requiring only low pressure equipment. The initial investment, as well as the operating costs, is significantly2 less, than for other known methods and devices that provide the same end results. In addition, the proposed method and device require minimum qualification and provide energy in the form of high quality steam. The invention provides essentially 100% destruction of all living organisms and approximately
    , 98% reduction in SOD is not accompanied by odor and gives an easily dehydrated ash product. All control is carried out on the surface, a minimum of energy is spent on pumping relative to
    0 large quantities of fluid and obes-. It produces continuous downstream and upstream fluid flow rates. The proposed method and device are suitable for
    5 performing chemical reactions at high temperature and under high pressure, for example, during cracking of petroleum products and for carrying out hydrogenation at high
    0 temperature and high pressure, for example, v ep in the production of ammonia, for which there is no E eCo, in enlarged bubbles.
    S8 S3
    FIG. five
    Aa
    2
    Bb
    5 78
    AT
    h
    32

    li
    AT
    32
    ZV
    100
    and.
    Mr. Io
     ,
    .B FIG. 15, Rig, 1d. 17 D-D US, FIG. IS 73 FIG. 21
    FIG. 22
    77S //
    // f
     Bb / xuff
    权利要求:
    Claims (13)
    [1]
    1. A method of conducting underground chemical reactions by supplying reagents, at least one of which is a liquid, to a vertical well drilled in the ground through a downward channel, creating hydrostatic pressure due to a column of liquid in the well, contacting the reagents in the reaction aeon located in the lower part of the well, with the formation of reaction products, heating of the reaction mixture, the withdrawal of heated reagents and reaction products to the earth's surface along the ascending channel, the heat exchange between onents in the descending and ascending channels and regulating the temperature and pressure of the reagents in the well, characterized in that, in order to intensify the process by achieving the maximum rate of a chemical reaction and eliminating boiling reagents in the well, temperature control is carried out by heating and cooling the fluid directly in the well and in reaction aeon, and the temperature of the reagents in the well and in the reaction zone is kept below the boiling point of the liquid, and the pressure is maintained above the boiling pressure I fluid.
    [2]
    2. The method of pop. ^ characterized in that as one of the reagents, a gas is used that is introduced into the liquid on the earth's surface in the downward channel in the form of a series of elongated gas bubbles, which together with the liquid are fed into the reaction aeon.
    [3]
    3. The method according to PP. 1 and 2, characterized in that the gaseous reagent is injected into the liquid below the surface of the earth in the form of parallel streams c.
    increase in gas pressure with distance from the surface of the earth.
    [4]
    4. The method according to claim 1, with the fact that the liquid pressure in the upper part of the reaction zone is maintained at 14 atm.
    [5]
    5. The method according to PP. 1 - · 4-, ό t l and arising from the fact that they recirculate the liquid leaving
    SB with
    - from the ascending channel, by returning it to the descending channel, and the liquid coming from the ascending channel is subjected to degassing and purification from gaseous reaction products before recirculation.
    b.
    [6]
    The method according to PP. 1 to 5, which is characterized in that wastewater is used as the liquid, and air with oxygen is used as the gaseous reagent
    [7]
    7. Installation for conducting underground chemical reactions, including a vertical well drilled in the ground, a reactor, a reagent supply device located in the well, connected by a pipeline to the reactor, and a device for controlling the temperature, pressure and flow of reagents, characterized in that, in order to intensify the process by creating a hydrostatic column of fluid and conducting chemical reactions at the depth of the well at elevated pressures and temperatures, it is equipped with coaxially installed in the well cuttings forming the descending and ascending channels into the reaction zone located in the lower part of the well, connected to the channels and made in the form of a U-shaped hydraulic shutter.
    [8]
    8. The installation according to claim 7, wherein the installation is provided with a base plate located on the surface of the earth, and the pipes are fixed to the base plate.
    [9]
    9. Installation pop. 7, characterized in that the pipes are made with decreasing diameter from the surface of the earth.
    [10]
    10. Installation according to claim 7, characterized in that the device for controlling the temperature is made in the form of a tubular heat exchanger.
    [11]
    11. The apparatus according to claim 7, characterized in that it is provided with a device for creating elongated gas bubbles connected to downstream channels.
    [12]
    12. Installation according to paragraphs. 7-11, characterized in that it is equipped with nozzles for introducing a gaseous reactant connected to the downward channel and located one above the other along the height of the well.
    [13]
    13. Installation according to paragraphs. 7-12, which means that the nozzles for introducing a gaseous reactant are installed along the axis of the descending channel with the outlet end placed in the reaction zone.
    类似技术:
    公开号 | 公开日 | 专利标题
    US4272383A|1981-06-09|Method and apparatus for effecting subsurface, controlled, accelerated chemical reactions
    KR920002068B1|1992-03-10|Apparatus and method for effecting chemical reactions
    US3606999A|1971-09-21|Method of and apparatus for carrying out a chemical or physical process
    US4416781A|1983-11-22|Treatment of biologically-degradable waste
    NL8602374A|1987-11-02|METHOD AND EQUIPMENT FOR CONTROLLED CHEMICAL REACTIONS.
    US4792408A|1988-12-20|Method and apparatus for enhancing chemical reactions at supercritical conditions
    EP0281302B1|1992-05-20|Process for effecting chemical reactions
    US4869833A|1989-09-26|Method and apparatus for controlled chemical reactions
    SU1088648A3|1984-04-23|Method and arrangement for conducting underground chemical reactions
    US4774006A|1988-09-27|Fluid treatment method
    CA2623036C|2011-12-20|Thermally autogenous subsurface chemical reactor and method
    US20040144019A1|2004-07-29|High pressure extraction
    FI89772C|1993-11-25|CHEMICAL REACTION FOR CHEMICAL REQUIREMENTS
    IE60659B1|1994-08-10|Method and reaction apparatus for effecting controlled chemical reactions
    RU2096076C1|1997-11-20|Apparatus for liquid-phase isoprene synthesis
    同族专利:
    公开号 | 公开日
    CA1115496A|1982-01-05|
    AU525800B2|1982-12-02|
    JPS5921655B2|1984-05-21|
    IL56838A|1982-05-31|
    AU4510779A|1979-11-22|
    EP0018366A1|1980-11-12|
    DK157445C|1990-06-05|
    IT1114579B|1986-01-27|
    WO1979000791A1|1979-10-18|
    EP0018366B1|1983-06-01|
    DK157445B|1990-01-08|
    JPS55500161A|1980-03-21|
    DE2965561D1|1983-07-07|
    DK484679A|1979-11-15|
    EG14326A|1983-09-30|
    MX6100E|1984-11-13|
    IL56838D0|1979-05-31|
    EP0018366A4|1980-06-23|
    IT7948395D0|1979-03-16|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    WO2012151447A2|2011-05-03|2012-11-08|The Administrators Of The Tulane Educational Fund|Underground reactor system|
    RU2490441C1|2012-02-21|2013-08-20|Открытое акционерное общество "Научно-исследовательский институт по нефтепромысловой химии" ОАО "НИИнефтепромхим"|Downhole reactor for oxidation of light hydrocarbons|US895229A|1908-03-30|1908-08-04|Cecil C E Beddoes|Method of treating sewage.|
    US1291130A|1915-09-29|1919-01-14|Arthur William Purchas|Education-pipe for air-lift pumps.|
    US2315577A|1939-07-07|1943-04-06|Infilco Inc|Treatment of sludge|
    US2665249A|1950-03-27|1954-01-05|Sterling Drug Inc|Waste disposal|
    US2773026A|1953-07-02|1956-12-04|Stora Kopparbergs Bergslags Ab|Removal of dissolved or dispersed organic material from aqueous solutions and suspensions|
    US3174733A|1961-04-14|1965-03-23|Fmc Corp|Swing diffuser|
    US3246761A|1962-10-30|1966-04-19|Bryan John Gordon|Liquid treating apparatus|
    US3449247A|1965-10-23|1969-06-10|William J Bauer|Process for wet oxidation of combustible waste materials|
    US3464885A|1966-04-05|1969-09-02|Halliburton Co|Methods for effecting continuous subterranean reactions|
    US3606999A|1967-08-04|1971-09-21|Harold L Lawless|Method of and apparatus for carrying out a chemical or physical process|
    US3853759A|1968-06-06|1974-12-10|J Titmas|Dynamic hydraulic column activation method|
    US3804255A|1972-10-18|1974-04-16|R Speece|Recycling gas contact apparatus|
    US4042510A|1976-09-02|1977-08-16|Canton Textile Mills, Inc.|Liquid aeration device|
    CH627146A5|1978-02-16|1981-12-31|Locher & Cie Ag|
    US4272383A|1978-03-17|1981-06-09|Mcgrew Jay Lininger|Method and apparatus for effecting subsurface, controlled, accelerated chemical reactions|EP0228755B1|1986-01-06|1992-01-02|James C. Burleson|Method and apparatus for disposal of a broad spectrum of waste featuring oxidation of waste|
    DE4337402A1|1993-10-26|1995-04-27|Mannesmann Ag|Probe for measuring pressure and temperature profiles|
    DE19508784C2|1994-03-10|1996-12-05|Mannesmann Ag|Process for cleaning a deep well reactor and deep well reactor with electronic control|
    DE19508785C2|1994-03-10|1997-06-05|Mannesmann Ag|Process and plant for the treatment of residual waste|
    AUPR544601A0|2001-06-04|2001-06-28|Exergen Pty Ltd|High pressure extraction|
    AU2011200090B2|2008-06-12|2016-01-07|Winwick Business Solutions Pty Ltd|System for cultivation and processing of microorganisms, processing of products therefrom, and processing in drillhole reactors|
    US10920152B2|2016-02-23|2021-02-16|Pyrophase, Inc.|Reactor and method for upgrading heavy hydrocarbons with supercritical fluids|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US88750678A| true| 1978-03-17|1978-03-17|
    [返回顶部]