JPH04501677A - Pyrolysis detoxification reactor equipment - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

[Detailed description of the invention] Pyrolysis detoxification reactor equipment The present invention relates to a pyrolysis detoxification reactor apparatus. More specifically, the present invention provides improved reactor equipment. and reacting dangerous and toxic compounds with water to produce very high concentrations of such compounds. The present invention relates to a method of operating the above device to achieve a degree of destruction.

Destruction of very highly hazardous toxic compounds is the goal of many types of technology. Danger Hazardous toxic compounds can be harmful to humans and animals when released into the environment even at very low concentrations. It is a compound that represents a possible health hazard. Hazardous waste is typically Contains one or more toxic compounds. Some of these prior art devices are essentially incinerators that rely on high-temperature combustion of toxic compounds to cause destruction. be. Typically, the result of such oxidation reactions is the same or similar to the compounds destroyed. Other compounds are formed that are more toxic. Moreover, such a reaction generates heat. , often unstable, often difficult to control, operating at pressures in excess of ambient pressure to reduce the risk of emitting hazardous substances into the environment in the event of an explosion, runaway reaction, leak, or failure. arise.

So-called pyrolytic detoxification utilizes reactions that are endothermic and avoid the presence of free oxygen. This avoids most of the problems inherent in incineration methods. Such a method is U.S. Patent Application No. 089,573. This method is dangerous and Toxic compounds are gasified and stoichiometrically achieved in a suitable reactor without the presence of free oxygen. React with excess water at high temperature. As a result of this thermal detoxification method, the degree of destruction is 99.9%. and very high - an effluent gas stream containing carbon oxides, carbon dioxide, hydrogen and water. arise. This reaction is more easily controlled than exothermic reactions and virtually It is carried out at atmospheric pressure or below and is therefore highly safe.

Pyrolysis detoxification reactor equipment represents a relatively new technology. The present invention is comparatively easy to maintain. The above methods can achieve a high degree of destruction in an efficient manner with relatively low throughput and high throughput. Constitute improvements in technology. The general spirit of the invention will be understood by those skilled in the art in conjunction with the accompanying drawings. It will become clear from the explanation below.

FIG. 1 is a schematic flow diagram of a pyrolysis detoxification reactor apparatus constructed in accordance with the present invention.

FIG. 2 is a schematic cross-sectional view of a pyrolysis detoxification reactor incorporated into the apparatus of the present invention.

Generally, the pyrolytic detoxification reactor device of the present invention reacts hazardous toxic compounds with water. Achieve a high degree of destruction. This device has a detoxification reactor, which is It has a central hot core region and a cold annulus located coaxially to this core region. are doing. Means are provided for heating the core region. Reaction in core area to circulate the flow of gaseous toxic compounds to the core region and then to the surrounding annulus. means are provided. stoichiometry before the flow of gaseous toxic compounds enters the core region. A theoretical excess of water is introduced into the stream of gaseous toxic compounds to react with the toxic compounds in the core region. let The flow of gaseous toxic compounds just before the flow of gaseous toxic compounds enters the core region. Heat exchange occurs between this and the effluent gas stream leaving the annulus.

With particular reference to the first, a reactor apparatus of the present invention is schematically illustrated. this device It operates to treat gaseous toxic compounds generated by Supply device 11 is toxic Any suitable configuration for gasifying compounds may be used. However, the supply A preferred form of device 11 is shown and described in co-pending U.S. Patent Application No. 092,041. This is an autoclave. In that equipment, a drum of toxic waste is A hot gaseous stream from the pyrolysis detoxification reactor circulates on the side and inside the autoclave. Heat depending on the source. 1. The hot gaseous effluent is then collected to contain liquid toxic waste. circulates to the drum itself. With the circulation of hot gaseous effluent, As a result of the heating of the drum, the liquid toxic waste contained in the drum evaporates and some gasification occurs. do. This gas is then used as a feed source for return to the detoxification reactor.

In FIG. 1, the supply device 11 is connected via a conduit 13 with a valve 15 to a primary heat exchanger 17. is shown as being connected to. This - determined exchanger 17 is a toxic gas The flow is raised to a high temperature and at this high temperature the flow of toxic gas is inserted into the detoxification reactor 19. Enter. The detoxification reactor 19 has a cylindrical interior constituting a high temperature reaction chamber or core region 22. It has a wall portion 21. From this cylindrical wall section 21, a second cylindrical wall coaxial therewith is formed. The sections 23 are spaced apart. The spacing between the walls 21 and 23 is relative to the core area 22. This constitutes a low-temperature ring portion 25 coaxially arranged.

Means are provided for heating the hot core region 22. In the illustrated embodiment, These means are a plurality of elongated resistance heating elements 27. Element 27 is fibrous oxidized atom The support disk 29 may be of suitable ceramic construction, such as aluminum. It extends downward. This disk 29 is supported by a dense structural support disk of thermal insulation. .

The reactor core 22 is thermally insulated from the reactor core 22. Raise the temperature of the core 22 to a high enough level Appropriate electrical connections, not shown in FIG. 1, are made to the resistive heating element for heating.

If the pressure in the cylindrical wall 23 is excessive, the rupture disc 33 will burst and relieve the pressure. Remove through vent pipe 35.

The incoming flow of gaseous toxic compounds is carried out through suitably connected inlet ducts as described below. 37 into the central reactor core area. After flowing upward through the core region, the gas flows into the annulus. via section 25 to the bottom of reactor 19 where the gas passes through conduit 39 to heat exchanger 1 Returned to 7.

Conduit 39 drains accumulated solids that can be disposed of as is known in the art. It has a suitable solids trap 41 for this purpose.

Outflow gas from conduit 39 passes through heat exchanger 17 and then via conduit 43 to another heat exchanger. It flows to the converter 45. This heat exchanger has two further parts where heat exchange occurs as described below. It is connected in series with other heat exchangers 47,48. Heat exchanger 45 is connected via conduit 51. The heat exchanger 47 is connected to the heat exchanger 47 via a conduit 53. It is connected to 49. A turbine 55 is provided in which the reactor effluent undergoes heat exchange. From the vessel 49 it flows through a conduit 57 to this turbine 55. The turbine 55 is for equipment The output of the turbine 55 is optionally routed through conduit 59 to a suitable suffler. 61 or directed straight to absorption tower 85.

A bypass loop 56 with a valve 58 is provided for flow control of the turbine 55. ing. The construction of optional flapper 61 may follow techniques well known to those skilled in the art. vinegar Flappers usually contain significant amounts of halogens, which are dangerous and toxic compounds. Sometimes it is attached as an optional item.

After the turbine 55 and after passing through an optional sflupper 61, if present, the effluent is It flows via conduit 63 to absorption tower 65 . The absorption tower 65 may be of any suitable configuration. stomach. However, in the illustrated embodiment, the absorption tower 65 includes a pair of activated carbon beds 67 and a (SELEXSORB) (trademark) commercially available from Lucoa & Corestal, Inc. and a pair of activated alumina beds 69 of a suitable material such as.

The outlet of plenum 71 is connected to T-junction 73 from which flow is directed to conduit 75. It continues upwardly through the heat exchanger 49 until it returns to the heat exchanger 49 .

Flow from conduit 75 flows from heat exchanger 49 through conduit 77 to heat exchanger 47, and then to heat exchanger 47. from heat exchanger 47 via conduit 79 to heat exchanger 45. Thus, heat In exchanger 45, 47, 49, the hot stream leaving heat exchanger 17 via conduit 43 Heat exchange occurs between the output and the cold effluent from absorption column 65 via conduit 75. . To maintain a suitable controlled flow rate, conduit 75 is equipped with a venturi flow meter section 81. There is.

After leaving heat exchanger 45, the cooler effluent flows via conduit 83 to portion 85. Ru. This part 85 connects via a valve 87 to the conduit 13 between the valve 15 and the heat exchanger 17. It is connected to another part 89. The other leg of part 85 connects to the bench via valve 91. is connected to a catalytic converter 97 via a conduit 93 having a flowmeter section 95. There is.

The catalytic converter 97 converts carbon monoxide, halogens, methane, etc. in the effluent into less harmful It may be of any configuration suitable for converting carbon dioxide and water into carbon dioxide and water. suitable A preferred embodiment has an outer annular portion 160 containing an automotive-style bicatalyst 161. . The catalytic converter 97 is provided with an air inlet vent 99 via a valve 101. There is. Carbon monoxide, halogens, and methane are extracted from this exhaust gas before it is released. from part 73 through conduit 103 and valve 105 to remove An inlet to the catalyst section 160 is provided. The treated gas is transferred to the catalytic converter 9 A vent 107 is provided for discharging from 7 through a venturi section 109. Ru.

The output stream from the catalytic converter 97 is heated by the heat generated from the air oxidation reaction. , to the supply device 11 via a conduit for returning the heated effluent gas to the supply device. high The purpose of flowing hot gas from conduit 93 through catalytic converter 97 is to heat the catalyst to 400°C ( 650° F.). As mentioned earlier, the catalyst The heat recovered from converter 97 is used to remove liquid toxic compounds from the supply system. The effluent gas can be used to volatilize at a high rate.

As mentioned earlier, the pyrolysis detoxification reactor apparatus of the present invention reacts for the pyrolysis detoxification reaction. A stoichiometric excess of water is used in the reaction vessel. For this purpose, a secondary Two alternating means are provided.

A first means is positioned in conduit 59 between turbine 55 and flapper 61. a water inlet conduit 153 having a valve 155;

A second inlet location for adding water to the device is provided via inlet conduit 157 and valve 159. I'm being kicked.

During operation of the apparatus shown in FIG. A gaseous toxic compound is produced by a supply device 11 and is passed through a conduit 13 and a valve 15. and sent to the primary heat exchanger 17.

There, the gas stream is further heated by heat exchange with the gaseous effluent from reactor 19. be done. The gas stream is then sent to reactor 19 via a conduit. water conduit 15 3 (or 157) and introduced into the gas flow through valve l55 (or l59) do. Typically, this water is in the form of hot superheated steam. The water is cooled by the turbine 55. cooling coil (not shown), then a cooling coil of the reactor turret (FIG. 1), which will be described later. Superheated steam can then be produced by introducing it into conduit 153.

Once the toxic compounds enter the hot core region 22, they are destroyed as described below. high temperature core area The effluent from the area 22 then flows to the upper edge of the cylinder 2I in the space below the insulation disc 31. The water flows above and enters the ring portion 25. The flow through the annulus 25 is downward, where it collects. and is circulated via conduit 39 to heat exchanger 17. The effluent is then divided into three through the secondary heat exchanger 45.47.49 and into conduit 57 via conduit 43.51.53. where it passes through turbine 559 and conduit 59 to optional flapper 61. It is circulated. When the effluent gas leaves the optional suffleper 61, it removes any of the toxic compounds. The material is recycled through conduit 63 to absorption column 65 for further removal of residual molecules.

When the effluent gas leaves the absorption tower 65 via the planar j, 71 and the T-connection 73, it enters the conduit. 75 and back through heat exchangers 49, 47, 45 from conduit 75 to conduit 83. increases the temperature of the effluent gas.

In typical operation, valve 87 is closed and valve 91 is opened to direct the effluent to conduit 93 and the catalyst. It flows through the central heat exchange pipe of converter 97. With this catalytic converter 97 , gas is converted to carbon dioxide and water (steam), heat is generated, and this heat leads to The gas in tube 111 is further heated. Any excess heat is exhausted through vent 107. Served. The heated gas in the conduit tit is then fed to the typically liquid gas in the supply device 11. through conduit 111 to supply device l] for further heating and gasification of the toxic compounds. be returned.

Valve 87.15 allows the effluent to bypass the feed device 11 from the heat exchanger 45 and directly to Recirculated to heat exchanger 17. This configuration is utilized during startup and shutdown.

When valve 105 is opened, a portion of the clean detoxified effluent from absorption tower 65 is directly is discharged to the outside.

The operating temperature within the equipment varies depending on the desired degree of destruction and the type of workpiece; The operating temperature is as follows.

Conduit 39 1850°F Conduit 37 1275°F Conduit 43 1215 °F Conduit 51 935 °F Conduit 53 665 °F Conduit 57 400°F Conduit 59 400°F Conduit 75 200°F Conduit 83 950°F The pressure within the apparatus, particularly within the reactor 19 itself, is generally near or above atmospheric pressure. is kept slightly lower. The pressure in conduit 37 is typically -38.1 ann of water ( -15 inches) (-0.5 psi), and the pressure in conduit 39 is typically The column is -76,1 an (-30 inches) (-1,0 psi). In front of turbine 55 The subsequent pressure drop is typically +96.2 AO (+38 inches) to -142 inches of water, 2 an (-56 inches).

Referring to FIG. 2, a specific configuration of a pyrolytic detoxification reactor is shown. Figure 1 As mentioned above, the reactor 19 includes a hot core region 22 and a cold annular plenum 2. having inner and outer coaxial cylinders 21 and 23 arranged to form a There is. Heating of the core region is provided by an elongated heating element 27. The top of the reactor is Protected against flow erosion by dense insulating discs 31, commercially available from Luker. protected ceramic insulation board 29 (also commercially available from Zilker) is closed by. The heating element 27 is mounted on the plate 29 with a suitable configuration. It is supported by a plurality of electrical fixtures 113. The upper part of the reactor is attached to the top plate 117. It is surrounded by a more covered turret top closure 115. Turret top wall and inside the top plate from water circulation from the turbine 55 cooling coil (not shown). A copper cooling coil 119 is arranged for superheating the resulting steam. for superheating elements A woven electrical cable 121 is connected to the turret top 115 by a suitable electrical thread 123. It has been passed.

The reactor is a 316-L stainless steel (or any suitable (alloy) is enclosed in an evacuation container 125.

The lower end of this container has a central opening 129 and a plurality of circumferential openings 1 extending from the ring 25. 31 and 321 stainless steel (or any other suitable alloy) plate 127 with Therefore it is closed. A base 13 made of castable alumina is provided on the surface of the plate 127. 3 is supported.

This base has an opening aligned with the boat 129,131. boat 12 The openings aligned at 9 are flushed at 134 to provide enhanced flow distribution of the incoming gas. It's becoming rare. Port 129 is connected to conduit 37 (FIG. 1) and 131 is manifold connected to conduit 39 (FIG. 1). Typically, Four mouth boats 131 are provided.

The stainless steel container 125 is made of Kao, commercially available from Babcock & Wilcock. optionally with walls made of suitable insulation material such as KAOWOOL(TM). surrounded by. Between the ceramic tube 23 and the stainless steel wall 125, there is a , a lightweight alumina fiber layer 139 is disposed. The inner surface of the ceramic tube 21 is Impermeable mullite (trademark) tube 141 commercially available from Ruto (Germany) protected by. For the high-temperature core region 21, a material commercially available from Silka Co., Ltd. A plurality of reticulated foam highly porous ceramic discs 143 are filled. this These disks are stacked in the area above the base 133, and the disks 143 is provided with a passage for receiving and simultaneously supporting the heating element. high temperature to provide adequate gas flow mixing and residence time in area 22. Other passageways may be provided in the ceramic disc 143 as desired. high temperature core area A thermocouple tube 149 extends downwardly at its center to monitor the temperature of 22 .

Within the alumina tube 149 passing through plate 29.31 is a suitable thermocouple 151, typically A double junction platinum-rhodium thermocouple is provided.

The inlet gas circulating from conduit 37 to reactor 19 enters through port 129 and enters the ceramic flows upward through the disc. In the hot core region 22, these gases (Toxic compounds react with superheated steam and potash to form substantial carbon monoxide and hydrogen.) The mixture is mixed and heated so that the These gases are located at the upper edge of the cylinder 21 below the plate 31. The hot core region exits above the . The effluent gas then undergoes some further reactions. It circulates downwardly through an annular plenum 25. Next, is the leaked gas from boat 131? and is routed to conduit 39 as previously described.

A particular advantage of the reactor apparatus of the invention described above is that the vapor of the effluent gas from the reactor is very is hot and therefore capable of delivering significant heat to the supply equipment. That is the point. Any carbonaceous material when the gas passes through the conduit 13 from the supply device 11 As a result of the kimono reaching a high temperature in the heat exchanger 17, it is turned into steam and gas. Also, the reaction Using the heat exchanger 17 to exchange heat between the reactor feed gas and the effluent gas Helps remove any problems with ash or carbonaceous deposits. This kind of adhesion material can be easily removed by the trap 41, thereby blocking the internal baffle in the reactor. The need for frequent cleaning is avoided.

Another advantage of the device of the invention is that ceramic coking is used to achieve proper mixing of gases. or eliminates the need for lashing rings, ceramic balls, or similar materials for ponds. Is Rukoto. The desired preheating and mixing takes place in the heat exchanger 17, and also in the hot core. This is done by a ceramic disc within the area itself.

Therefore, the present invention provides an improved pyrolytic detoxification reactor system for reacting hazardous toxic compounds. You will see that it provides a location. This device is efficient, compact and Easy to operate. Other advantages of the invention will be apparent to those skilled in the art from the above description. Probably. From the foregoing description and accompanying drawings, it will be apparent to those skilled in the art that the In addition, various modifications of the invention will become apparent. An example of such a change is attached falls within the scope of the claims.

FIG2 Submission of translation of written amendment (Article 184-8 of the Patent Act)

Claims (15)

[Claims] 1. In pyrolysis detoxification reactor equipment for reacting dangerous and toxic compounds, having a central hot core region and a cold ring coaxially disposed with respect to the core region. a detoxification reactor, a means for heating said core region, and a means for heating said core region, and means for circulating flow to the core region and then to the annulus for reaction; gas before entering the core region due to reaction with toxic compounds in the core region. means for introducing a stoichiometric excess of water into the stream of toxic compound; Flow of gaseous toxic compounds just before entering the core region and effluent gas flow leaving the annulus. and a primary heat exchange means for exchanging heat with the pyrolysis detoxification reactor. reaction equipment. 2. The water introduction means introduces water between the primary heat exchange means and the core region. 2. A reactor device according to claim 1, characterized in that the reactor device is positioned in the device as follows. . 3. Said water introduction means introduces water into a stream of gaseous toxic compounds before said primary heat exchange means. 2. The device according to claim 1, wherein the device is positioned so as to be introduced into the device. Reactor equipment. 4. a supply device, wherein at least some of the effluent gas from the reactor is supplied to the supply device; be circulated to the feeder, mixed with the gaseous toxic compound, and circulated to the reactor. The reactor apparatus according to claim 1, characterized in that: 5. The flow of effluent gas immediately after leaving said primary heat exchange means and recycled to said reactor. It is characterized in that it is equipped with a secondary heat exchange means for exchanging heat with the effluent gas stream before being 5. The reactor apparatus according to claim 4, characterized in that: 6. Catalytic converter means may be provided between the secondary heat exchange means and the supply device. The reactor apparatus according to claim 5, characterized in that: 7. Means for maintaining the pressure within the reactor substantially at or below atmospheric pressure The reactor apparatus according to claim 1, characterized in that it comprises: 8. The reactor contains sufficient gas to produce a substantially fine mixture of gases in the core region. characterized by having ceramic means in the core region for providing a dispersed flow of The reactor apparatus according to claim 1. 9. The means for heating the core region includes a plurality of axially extending means for heating the core region. a number of elongated resistance heaters, the ceramic means being adapted to support the heaters; 9. The reactor apparatus according to claim 8, characterized in that it is configured as follows. 10. The claim is characterized in that the primary heat exchange means is positioned within the annulus. The reactor apparatus according to claim 1. 11. a central high-temperature core region and a low-temperature ring disposed coaxially with respect to the core region; In a method of operating a pyrolytic detoxification reactor apparatus comprising a detoxification reactor having heating the core region to a temperature sufficient for decomposition of the toxic compound therein; Circulating a stream of gaseous toxic compounds to the core region and then to the annulus for reaction and a stoichiometric excess of water in the flow of gaseous toxic compounds before entering the core region. is introduced and reacts with the toxic compound in the core region, and the gas immediately before entering the core region is heat exchange between the stream of gaseous toxic compounds and the stream of effluent gas leaving the steam annulus. How to characterize it. 12. Water may be introduced into the device between the core region and the location where the heat exchange process described above takes place. The method according to claim 11, characterized in that: 13. Water may be introduced into the gaseous toxic waste prior to the point where the above heat exchange step takes place. The method according to claim 11, characterized in that: 14. directing at least some of the effluent gas from the reactor to the reactor; according to claim 11, characterized in that it is returned to the source of the gaseous toxic compound for circulation. Method. 15. The pressure within the reactor is maintained at substantially atmospheric pressure or lower. 12. The method according to claim 11.