CA1104423A - Treatment of waste - Google Patents

Abstract

TREATMENT OF WASTE

Abstract of the Disclosure A method for treating waste which comprises feeding the waste into a fluidized bed incinerator and calciner; pass-ing a gas effluent from the incinerator and calciner to a dry cyclone for removing solid particles from the gas effluent;
passing the solid particles to a storage container for subse-quent treatment and/or packaging; removing a gas effluent from the cyclone and passing it to a quench tank; removing liquid particles from the quench tank and passing them to a scrub solution tank; removing a gas effluent from the quench tank and passing it to a venturi scrubber and then to a wet cyclone;
removing liquid particles from the wet cyclone and passing them to a scrub solution tank; removing a gas effluent from the wet cyclone and passing it to a condenser and then to a demister, removing liquid particles from the demister and passing them to a scrub solution tank; removing a gas effluent from the demister;
heating the gas effluent and passing the effluent through a filter for removal of remaining solid particles; and then pass-ing the gas effluent through a sorber for removal of halogen gases therefrom.

Description

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!.4 4~ Z3 Field of the Invention The present invention is concerned with a method for treating and disposal of waste materials. The present invention is especially advantageous in the treatment of radio-active wastes such as those which include radioactive halogens such as iodine 131 isotope. The present invention is partic-ularly directed to a method which substantially reduces the volume of both li~uid and solid radioactive waste materials including concentrated chemical wastes, filter sludges, spent ion exchange resin beads, rags, and other similar materials.
The process of the present invention reduces all liquid and combustible solid waste to anhydrous granular solids.

Backqround of the Invention . 1,' .
During the last few years, there has been a signifi-cant increase in the use of energy including nuclear energy for power plants. This increased demand has been accompanied by increased treatment and disposal problems of the waste ~aterials.
one nignificant problem is that due to the increase in the num-ber of operating facilities, there is a great demand on available space at licensed disposal sites. Moreover, it is believed that selection o~ new commercial disposal sites in the future will involve close government supervision and strict regulation, In particular, it is believed that government regula-tory agencies will now review and monitor low level radwaste disposal installations. Requirements to obtain a license will probably become more stringent.

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' ` t A major concern in disposal is the safety of trans-porting the treated waste to its final disposal site. In deal-ing with this concern, it is desirable to reduce the volume of the waste as much as possible along with increasing the stability of the materials.
Therefore, an object of the present invention is to provide a treatment process which makes it pos'sible to signifi-cantly reduce the volume of the waste materialv A major problem in the treatment of wastes generated in nuclear plants is that the types of waste can differ signif-icantly in chemical and physical characteristics and many treatments of waste must be tailored for only a single facility.
The present invention provides a process which is as independent as possible from the chemical composition of the waste material and therefore useful for treatment of a myriad of waste materials.
Fluidized beds have been employed for li~uid calcina-tion or combustible waste incineration in industrial plants for several years. For instance, see Richard C. Corey, Principals and Practices of Incineration, Wiley-Interscience, ~ew York, .. . ... _ ..
1969, page 239. Moreover, fluidized bed calcination of radio-active wastes was developed during the period of 1952 to 1959 at the Idaho ~ational Engineering Laboratory. Use of calcina-tion for liquid radwaste reduction was employed in an engineer-ing scale facility, the Waste Calcining Facility ~WCF), at the Idaho Chemical Processing Plant in 1963.
A batch operated fluidized bed calciner was d~signed and built as part of the Midwest Fuel Recovery Plant (MFRP) at :: ' ~ -3-4~Z3 Morris, Illinois for General Electric Company. A batch calci nation process was employed on a fully radioactive basis in the WSEP program from about 1966 to about 1970. This process was developed at Oak Ridge ~ational Laboratory for the specific purpose of solidification of high level radioactive liquid waste but did not employ a fluidized bed process. `
Incineration of combustible radioac~ive wastes has been in use as a disposal technique since 1948 when a pilot plant incinexator and off-gas clean~up system was built at Mound Laboratory. The earlier systems were adaptations of standard refuse incinerators and demonstrated that considerable volume reduction in waste handling was possible. Data taken in the early 1960's at the General Electric Atomic Power Equipment Department in San Jose, California showed that about 99% of the radioactivity of the incinerated wastes remained in the ash.
Similar data was reported from an incinerator at Pratt and Witney Aircraft where approximately 99.1 to 99.98% of the radioactivity remained in the ash.
For~a discussion of various incinerators for rad-waste treatment, attention is directed to B. L. Perkins, "Incineration Facilities for Treatment of Radioactive Wastes:
A Review", LA-6252, Los Alamos Scientific Laboratory, Los Alamos, New Mexico, 1976O
Fluidized beds which have been previously employed in converting liquid waste streams including radioactive streams to solid particles are composed of the resulting solid products from previous drying or calcining a liquid waste stream simiiar ~` ~
llG44Z3 to the one being treated.
The difficulty encountered with the above approach is that the fluidized particles are simultaneously subject to growth, from deposition of new liquid waste on the surface whe~e the water flashes off and leaves a layer of resultin~
solids, and size reduction caused by the "seif-grinding" action of the particles colliding with each or with any solid surface to which they are exposed.
The simultaneous growth and size reduction processes are very critical to proper operation because lf the fluidized bed particles become too large, they cannot be properly fluid-ized thereby limiting the successful operation of the process.
on the other hand, if the bed particles become too small, they will be blown out at the top of the fluidized bed as the ter-minal velocity of the particles will approach the fluidizing air superficial velocity in the vessel. Entrainment of solid particles in the effluent gas is commonly referred ~o as elu-triation. Accordingly, in such system, due to the delicate balance between growth and size reduction, it is necessary to continually monitor the particle size distribution of the fluidized-bed media and make adjustments in operating conditions to control the particle size and particle growth phenomena to assure proper particle size.
l'his particle growth and size reduction phenomena is greatly influenced by the chemical characteristics and com-pQS ition of the liquid waste stream being converted to the solid. Por instance, if the total solids content (dissolved . - .

4~23 and undissolved) of the waste is less than a certain value dependent upon the chemical identity of the liquid waste, it is not possible to grow fluidized-bed particles. This is due to the size reduction (attrition) rate being greater than the size increase (growth) rate because of the small amount of solid-building material present in the liquid waste stream.
This dependency of such fluidized-be'd calcination or evaporation processes upon the chemical identity of the li~uid waste is a major disadvantage which requires extremely close process supervision to assure proper operation. Accord-ing to the present invention, a process is provided whereby the calcination and incineration is not so critically dependent upon the liquid waste chemistry.
! Moreover, the above type of calcination processes cannot handle very dilute liquid waste streams in view of this particle size control problem. The proceas of the present in-vention is capable of successfully treating very dilute liquid waste ~treams as well as entirely solid waste material. The present invention makes it possible to employ the same fluidized bed but operating at different conditions (e.g., different tem-peratures) for both calcination and incineration.
In a booklet by the assignees of the present applica-tion entitled'~WR-l Radioactive Waste Reductio~'which was avail-able in about October 1975,at a trade conference in Switzerland, a system was suggested wherein an afterburner was required after the incinerator-calciner. According to the present invention, n vlew of the particular controls on certain process parameters, ,

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i~ is no longer necessary to employ a separate afterburner.
Any afterburning needed occurs directly in the incinerator/
calciner rather than after leaving the incinerator/calciner and after a subsequent cyclone treatment. The above booXlet did not disclose the necessary details concerning the fluidized bed which are essential to the present invention.

Summary of the Inventlon The present invention is concerned with a method for the treatment of and volume reduction of waste material which includes employing a fluidized-bed incinerator and calciner wherein the bed material is resistant to oxidation, agglomera-tion, and attack by chemicals at temperatures up to at least about 1000C. Combustion conditions are maintained in the fluidized bed by supplying fuel and an oxygen-containing gas thereto. The bed particles are maintained in the form of fluidized particles by introducing a gas into the fluidized bed region of the incinerator and calciner at a velocity suf-ficient to maintain the particles in fluidized condition.
The waste to be treated is fed into the fluidized bed region of the fluidized-bed incinerator and calciner.
The waste is incinerated or calcined in the incinerator and calciner and a gaseous effluent is removed therefrom and directed to a dry cyclone. Solid particles are separated from the effluent in the dry cyclone. The solid particles are removed from the dry cyclone and directed to a storage container for possible subsequent treatment and/or packaging, if desirea.

11~4~Z3 The gas effluent is removed from the cyclone and directed to a quench tank wherein liquid is introduced for cooling of the gas effluent and wetting of particles still contained in the effluent. ~iquid and wetted particles not remaining entrained in the gas effluent are then removed from the quench tank and are directed to a scrub solution tankv A gas effluent is removed from the ~uench tank and additional liquid is added to the venturi scrubber to wet particles remaining in the gas effluent and to cause conden-sation of water vapor. A gas effluent containing wet particles i~ removed from the venturi scrubber and directed to a wet cyclone. Liquid particles are removed from the wet cyclone and are directed to a scrub solution tank. A gas effluent is removed from ~he wet cyclone and is directed to a condenser.
A gas effluent and condensed liquid particles are removed from the condenser and are directed to a demister wherein liquid particles are removed. The liquid particles are then conveyed to a scrub solution tank_ The gas effluent is removed from the demister and i9 heated. The heated gas effluent is then pas~ed through a filter for removal of re-maining solid particles and then through a sorber for removing of halogen gases therefrom.
The scrub solution tank or tanks are employed pri-marily as a collection means for maintaining a reserve of scruh solution. The scrub solution is withdrawn, when needed, from the scrub solution tank or tanks for supplying liquid to the quench tank and venturi scrubber, and/or recycling to the 4~;~

plant liquid waste system. Thus, radioactive halogens which may be introduced into the scrub solution tank are retained within the treatment system for a sufficient amount of time to allow decay to a nonradioactive daughter. In the preferred embodiments, a halogen treating or getting agent is introduced into the scrub tank.

Brief Description of the Drawinq The figure illustrates a sequence of processing steps within the scope of the present invention.

Description of Preferred Embodiments The present invention can be more fully understood by I reading th0 following description in conjunction with the figure which schematically illustrates a preferred process according to the present invention. Also, for convenience, the process will be described in terms of treating low level radioactive waste materials with the understanding that other waste materials can be treated according to the present invention.
Reference to the figure shows a feed system which includes vessels 1, 3, 4, and 6; an incineration and calcina-tion system which includes vessel 9, and an of~-gas clean-up system which includes vessels lO, 12, 13, 14, 15, 16, 170 18, 19, and 21.
When desired, the waste can be pretre~tea prior to introduction into the feed system. For instance, relatively large noncombustible solids such as tools~ piping, and the like ~g _ .

can be separated by sorting means. Explosi~e materials can be removed by conventional methods, if needed.
The feed system to the incinerator and calciner vessel 9 shown in the figure is arranged for feeding three separate types of waste. These three types of waste include a low-level radioactively contaminated combustible waste, spent resins and sludges, and liquid waste. Of course, this feed system is only exemplary of the myriad systems which may be employed depending upon the exact waste being treated and/
or the existence of a feed system already at a facility.
In handling combustible waste, when needed, it is desirable to reduce the size of the individual particles of waste such as by shredding so that they can be efficiently transported into the incinerator. The maximum size of the particles must be smaller than the inside diameter (ID) of the transport piping leading to the process vessel and is limited, when a pneumatic feed is employed, by the flow rate of the feed gas. Moreover, the particle size must be small enough to substantially preclude migration to the bottom of the vessel 9 before incineration can be completed.
For a potential commercial system now being pursued, the limiting condition on particle size is the ID of the trans-port piping. In particular, the preferred maximum dimension of particle for the above-mentioned commercial system is less than about 2". Reduction of particle size when desired can be done by way of a shredder located within the storage hopper 6.
By including the shredder within the storage hopper 6, the ~ ~ :~
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handling about 200 to about 300 pounds/hour of combustible solid wastes.
Resin and sludge are introduced into tank 3 ~ia con-duit 33 and collected therein. Typical resin and sludge feeds include cation and anion exchange resin beads, powdered resin -filter precoat materials (e.g.~ "Powdexi'), nonresinous filter precoat materials (e.g., "Solkafloc"* diatamaceous earth and the like), along with varying amounts of water. The resin and sludge are conveyed via conduit 34 to a mixing and dewatering tank 4. From tank 4, the material is then conveyed to a meter-ing device and pump 5 whereafter it is injected into the vessel 9 via conduit 35.
Suitable sizing of vessel 9 for many applications is designed to be capable of hanaling about 100 to about 175 pounds of resin and sludge feed wastes. In the dewatering and mixing tank 4, the waste is mechanically agitated which helps prevent bridging, compaction, or adhesion to the tank walls. After de-watering, the slurry desirably includes only as much water as is necessary to maintain a pumpable slurry. Typically, feed slurries contain at least about 70% by weight of solids and up to about 80% by weight of solidO
Water which is obtained ~rom the dewatering can be re:turned to the slurry pumping system as make-up water or can be pumped to the liquid waste storage tank 1 via conduit 36 by ` pump 5. The pump 5 can be a positive displacement mechanical feed device which meters the waste as it is injected into the incinerator. When desired, the system can be continuously * Trademark il~ 3 shredding and hopper loading operations can occur at the same time with a minimum amount of effort and radiological exposure.
It is desirable that the storage hopper be large enough so as to maintain at least about a month's supply of shredaed waste.
Preferably, the storage hopper is sealed to the atmosphere to guard against possible radiological contaminàtion of the sur-rounding area. Some typical low level radioa~tive combustible waste materials include protective fabric clothing, gloves, rags, p~astics, paper respiratory filters, wood, and the like.
The combustible waste can be conveyed to incinerator and calciner 9 via, for instance, a screw conveyer 31 and con-duit 32. Other means of conveyance can, o~ course, be employed.
In order to ensure against the possibility of outleakage of radioactive contamination from the radioactive material in the 1: .
system, the vessel 9 is maintained at a pressure lower than ambient pressure and the feed is to a portion of the vessel whexein the pressure is lower than ambient pressure. A conven-ient pressure at which process vessel 9 can be maintained is about 10-35 mm Hg and preferably about 28 mm Hg vacuum. In addition, if desired, the screw feeder can include an isolation valve (not shown) which is used to provide a positive air-tight seal when the combustible feed system is not in use~ The shredder and hopper 6, as well as accompanying feed conduits, are preferably constructed of carbon steel.
The flow rates of the waste feeds are primarily de-pendent upon the size or capacity of vessel 9. Suitable sizing of vessel 9 for many applications is designed to be capable of - t operated since dewatering, metaring, ana injection are simul-taneous operations. Also, when desired, the rate of feed can be automatically regulated.
The resin and slud~e are introduced into vessel 9 at a position wherein the pressure is below atmospheric and generally about l to 2 psi below ambient. The equipment for the mixing and dewatering of the resin and sl~dge is preferably constructed of stainless steel.
Liquid waste is introduced into liquid waste tank l via conduit 37. Suitable sizing of vessel 9 f~r many applica-tions is designed to be capable of handling about 30 to about 50 gallons/hour of the liquid waste. Liquid waste is pumped from tank l by pump 2 via conduit 38 to vessel 9. It is pre-ferred that the liquid waste be introduced into the vessel 9 through atomizing nozzles, The liquid waste is desirably at a temperature sufficient to maintain the solids in solution.
The liquid waste should be at a temperature above the satura-tion temperature of the solid wastes at the concentration in the s~lution. The temperature is generally from a~out 50F
to about 200F depending upon the amount and type of solids.
This tends to at least retard precipitation of dissolved solids from the waste stream onto the nozzles and conveying equipment and in turn inhibits subsequent plugging of process piping, valves, noæzles, and the like.
Typical liquid waste can c~ntai~ about 50 to about~
9~/O water along with such soluble materials as sodium sulfate, ammonium sulfate, sodium chloride, boric acid~ and the like.

l~ Z3 Some specific liquid waste compositions include Boiling Water Reactor (BWR) waste from a forced recirculation evap-orator which contains about 75% water, about 22.9% sodium sulfate, about 2% sodium chloride, and 0.1% miscellaneous ingredients; Pressurized Water Reactor (PWR) waste from a forced recirculation evaporator which includes about 73.4%
water, about 14.9% sodium sulfate, about 9.6%.ammonium sulfate, about 2% sodium chloride, and about 0.1% miscellaneous ingred-ients; and boric acid waste from a forced recirculation evap-orator which contains about 87.9% water, about 12% boric acid, and the remainder miscellaneous ingredients. The above per-cents are all by weight.
It is understood, of course, that since the different types of feed require different temperatures of treatment de-pending on whether calcination or incineration is needed, only one stream is introduced into the vessel 9 at any one time and is treated therein. Accordingly, when one of the streams is being introduced into the vessel 9, the other two streams are closed off from the vessel.
It is possible, according to the present invention, to employ the same vessel for both calcination and incinera-tion depending on the temperature conditions present in the vessel. This is accomplished by employing as the fluidized bed material a material which is xesistant to oxidation, agglomeration, and attack by chemicals such as acids and bases at temperatures up to at least about lOOO~C. The use of such an inert material eliminates problems existent in prior :

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fluidized-bed incinerators which required a close monitoring o~
the system to assure proper operation. This was due to the fact that the particle growth and size phenomena as discussed hereinabove had to be properly controlled. Bed materials which do not possess the above properties such as quartz have not been successful in the process of the present invention.
~he preferred inert bed materials po,ssess the follow-ing characteristics:
Hardness (Moh) 6.0 - 9.0 Specific Gravity 3.2 - 3.9 Dry Bulk Density (lbs/cu. ft.) 100 - 125 Coefficient of Thermal Expansion (in/in/F) 0.0083 Fusion Point 2300 - 3200F
(1538 - 1760C) High temperature reaction Basic High heat absorption Silicosis free Particle size About 0.5 - 1.5 mm.

Some examples of bed materials which can possess all of the above properties include chrysolite, olivine, Xyanite, corundum, and alumina.
The most preferred inert bed materials are the magnesium-iron silicates known as olivine or chrysolite. A
typical olivine material suitable as the fluidized-bed material, according to the present invention, has the following chemical and physical characteristics~

4~3 Olivine Hardness (Moh) 6.5 - 7~0 Dry bulk density (lbs./cu. ft.) 100 - 125 Specific gravity 3.2 - 3~6 Thermal expansion (in./in.) 0.00~3 Apparent heat transfer Low Fusion point 2300F - 3200F

High temperature reaction Basic Wettability to molten metal ~ot generally Chemical reaction Basic Particle size About 0.5 - 1.5 mm.

Chemical Analysis Ran~e MgO ..................................... 45 - 49%
SiO2 ... ~................................ 39 - ~3%
FeO ........ ............................. 6 - 8%
Cr203 ...... ............................. .6 - .8%
Ni ..... ,................................ .2 - .3%
A1203 ................ ................... .2 - .8%
Trace elements .... .5%

Mineraloqical Analysis Olivine .............. 92 - 93%
Enstatite .... ,....... 5%
Serpentines .......... 1 - 2%
Chromite ............. 1%
Total....... ~....... 100%

other ProPerties Constant coefficient of expansion.
High heat absorption.
High heat conductivity at low temperatures.
Tough, durable grain.
Silicosis free.
Insulator at high temperatures.
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. ~ -11~49~3 The maximum temperature employed in the calcination process is primarily limited by the melting point of the feed solids. The maximum temperature for incineration is primarily determined by economic and practical considerations concerning the strength of the material of construction of vessel 9. The bed material is generally maintained at a te~perature of between about 350~C and 550C and preferably about 400jC for calcination, between about 800 and about 1000C and preferably about 800C
for the incineration treatment of resin and sludge; and between about 900 and about 1200C and preferably about lOOO~C for the treatment of compactible solids.
A gas such as air is blown into the bottom of vessel 9 via blower 7 and conduit 39 to maintain the bed in it~
fluidized condition and at proper height. This gas when air i8 employed also supplies the oxygen necessary for combustion.
Moreover, if desired, additional air can be injected a~ove the bed to enhance complete combustion via conduit 32. In view of the interrelationship between the height of the vessel 9 and the flow rate of the treated material, the material remQins above the bed for a sufficient amount of time that any necessary afterburning for combustion occurs before the entrained partic-ulate matter is exhausted into the dry cyclone. This eliminates the need for an afterburner. An overall height of vessel 9 of about 15 feet is suitable for processing the amounts of materials discussed hereinabove. The static bed height for processing the amounts of materials discussed hereinabove can be from about 18 to about 35 inches. Of course, the bed height and~or vessel ~.

height can be scaled up or down depending upon the actual amount of material to be processed.
The heat for the calcination or incineration and for preheating the bed is provided by combustion within the bed of a liquid hydrocarbon fuel in a burner (not shown).
Combustion within the bed provides the needea heat transfer.
The fuel is pumped via pump 8 and conduit 40 to the burner.
The incinerator and calciner are preferably constructed of Inconel or alternatively titanium, hastelloy or steel with a refractory or ceramic lining. A gas effluent leaves vessel 9 via conduit 41 and is directed to a dry cyclone lO.
The table below sets forth some approximate typical operating conditions for the various operating mo~es for dry cyclone lO of the dimensions given.
Capacity of Unit - 1750 CFM
Inlet velocity - 50 ft/sec Inlet duct - .5 ft x l.0 ft (long dimension is vertical) Cyclone I.D. - 2 ft.
C~alcin ti n of liquid wastes 2 - 166 lb/hr ~2 ~ 858 lb/hr CO~ - 235 lb/hr ~2 - 86 lb/hr Solids - 50 lb/hr Total - 1395 lb/hr Temperature - 375C
Pressure - 14 psia CFM - 90o Incineration of resins/filter sludqes 2 ~ 33 lb/hr N2 - 725 lb/hr C2 - 157 lb/hr H20 - 141 lb/hr Solids - 2 lb/hr Total - 1058 lb/hr Temperature - 800C
Pressure - 14 psia Incineration of compactible waste 2 - 44 lb/hr ~2 - 874 lb/hr C2 - 294 lb/hr H20 - 120 lb/hr Solids ~ 8 lb/hr TotaI - 1340 lb/hr Temperature - 1000C
Pressure - 14 psia ~ .

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The controlling dimensions of the dry cyclone are the inlet duct dimensions which establish the inlet flow rate and the inlet diameter which determines flow rates, and thus centrifugal force, developed within the dry cyclone. ~he dry cyclone is for removing any solid material in the gas effluent and preferably removes at least about 82% of the solids con-tained therein. The gas effluent enters the c'yclone at a side approximate the top of the cyclone to achieve a circular swirl-ing motion. The solids which are separated from the gas efflu-ent settle towards the bottom of the dry cyclone and are exited therefrom via conduit 42 and are directed to disposable con-tainer 11. The solid particles are then solidified by conven-tional means for subsequent disposal such as by burial. Approx-imately at least 82% o$ radioactivity from the solid particulate ~atter is removed from the dry cyclone along with at least about 17% of radioactive halogens.
In the dry cyclone, the swirling motion of the air causes a centrifugal force to act upon the solid particles so that they migrate to the wall. The air velocity is lower close to the wall due to the boundary effect, so that the particles slide downward along the wall to the particulate exit 42. The gas effluent exits upward from the top center of the cyclone 10 via conduit 43 and is directed to quench tank 12~ The dry cyclone can be constructed of the same types of materials as the incinerator and calciner.
In quench tank 12, the gas effluent is cooled to a temperature of about 70C by a liquid spray which is introduced :

4~23 into the quench tank via conduit 44 and spray nozzles (not shown). In quench tanX 12, turbulent gas motion is created which causes intimate contact between the gas and liquid streams. This causes both cooling of the gas effluent and wetting of most of the remaining solid particles in the gas effluent. The larger liquid droplets fall to the bottom of quench tank 12 and are returned to scrub solu~ion tank 21 via ~
conduit 4~ taking the wetted solid particles along with them. ~ `
Smaller liquid droplets are swept out of the quench tank 12 with the gas effluent via conduit 47. The quench tank and scrub solution tank are preferably of 300 series stainless steel or of Inconel, hastelloy or steel linea with glass or Teflon.
~ The liquid particles are aamixed with water in scrub solution tank 21 and preferably with a halogen "getter"
~i.e., material for capturing halogens~. Some examples of getters for iodine include resorcinol, sodium thiosulfate, , .
sodium sulfate, cyclohexyl amine, potassium ferxocyanide, potassium carbonate and potassium hydroxide. The halogen getter and any pH adjusting materials can be added to the ;~ scrub solution tan~ usually as an aqueous composition via conduit 46. The amount of halogen getter employed is gener- !
ally from about 10 to about 100 ppm in the scrubbing solution The gas effluent exits the quench tanX via conauit 47 and is directcd to venturi scrubber 13~ Scrub solution is sprayed into the gas ef~luent via conduit 48 at the thr~at of the venturi scrubber. In venturi scrubber 13, it is desirable *Trademark : , .
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to achieve saturation and entrainment of water to facilitate wetting of those particles which were not wetted in quench tank 12. The yas effluent leaving vessel 9 contains a great deal of water vapor such as in the order of about 9 to about 17%. Moreover, as the gas effluent passes through quench tank 12, water vapor, in addition to entrained water, was acquired, At the venturi scrubber 13, the gas effluent iis substantially saturated with water vapor. Saturation is ensured by spraying additional scrub solution via conduit 48 into the gas e~luent as it passes through the t-hroat of the venturi scrubber 13.
As the gas effluent passes through the venturi throat, the pressure drops which in turn causes an increase in the amount o~ moisture which the gas can maintain in vapor form. Accord-ingly, evaporation occurs. As the gas effluent enters the divergent section of the venturi scrubber, the velocity de-creases and the pressure increases thereby resulting in con-densation of water vapor. This condensation in turn causes the existing droplets to become larger along with causing new droplets to form on the unwetted particles which serve as con-densation nuclei.
As can be seen, the primary purpose of the quench tank and venturi scrubber is to cool the off-gas so as to wet as many of the solid particles as possible to facilîtate re-moval. It is easier to remove a liquid droplet than it i9 to remove a much smaller solid particle. The liquid particles are removed subsequently whether the particles are composed of sol-uble material which have gone into solution in the droplet or `~ {
11~4~;z3 the particles are composed of insoluble material which is re tained as a wetted solid within the droplet. In either situa-tion, the solid particle moves with the liquid droplet~ The venturi scrubber can be cons~ructed from the same types of materials as the quench tank. The following table sets forth some typical process parameters for quench tank and venturi scrubber of the sample dimensions given below..

Quench Venturi Tank Scrubber Gas flow rate (CFM) 900-1800 500-900 Inlet temperature (C) 400-1000 60-75 Outlet temperature (C) 60-75 45-65 Inlet pressure (psia) 13.7 13.7 ~p (p~i) negligible 2 Scrub solution flow rate tgpm) 5 11 Sizing 4' dia x 8 ' 6 " dia 32" length 2.7" throat A gas effluent containing liquid particles is removed from the venturi scrubber ~ia conduit 49 and introduced into wet cyclone 14 near the top. In wet cyclone 14, liquid runs down the side of the cyclone to a drain in the bottom thereof. The liquid is then removed from the cyclone ~ia conduit 15 and directed to scrub solution tank 21.
Typical operating parameters for the cyclone 14 in-clude a temperature range of about 45~C to about 65~C, an inlet pressure of about 12 psia, a ~p of about 0.5 psia, and a gas ~flow rate of about 400 to about 750 CFM.

, ~ -23-A gas effluent is removed from the top of wet cyclone 14 via conduit 51 and is conducted to a condenser 15 for cooling the gas effluent. The condenser can be a shell and tube type heat exchanger if desired. In the condenser, the liquid parti~
cles grow in size to a point wherein a significant amount of the water in the gas effluent is removed by gravitational or momentu~
effects, In a gravitational removal mechanis~, the drops are so large that they fall to the bottom of the vessel. On the other hand, in a momentum removal mechanism, the droplets are not large enough to fall out of the off-gas stream but they are large enough so that when the gas changes direction suddenly, the droplets impinge upon the wall or other solid material which has caused the direction change, Typical operating parameters for the condenser 15 include a gas flow rate of about 400-800 CFM, about 5-20 gallons~
minute of cooling liquid, inlet temperature of about 45 to 65C, a aT of about 10-30C, inlet pressure of about 11.5 psia, and a ~p of about 2 psi.
The gas effluent and liquid droplets exit the con-denser via conduit 52 and are directed to the demister 16. The demister operates to remove the liquid particles by the momentum removal effect. Gas is passed through a filter of woven fiber~
whiCh causes the gas to undergo rapid and fre~uent changes in direction. However, since the liquid droplets are too laxge to turn as sharply as the gas particles, they collide with the fi}ter fibers. The liquid droplets then run down the fiber to the wall of demist-er 16 and from there to the drain and conduit 4~3 53 which returns the liquid droplets to scrub tank 210 The gas effluent leaves the demister 16 near the top via conduit 54 and is directed to a heater 55 which heats the gas effluent to a temperature between about 40C and about 55C. The heater i8 employed to control the relative h~midity of the gas effluent in order to protect the HEPA filter 17 from clogging or plugging due to moisture overloading. The gas effluent is conducted from the heater to the HEPA filter via conduit 56 wherein solid particles which have not been wetted or which have been formed when those droplets which were not removed in the demister were evaporated in the heater are trapped. The filter is composed of a medium with very small pores and the particles are removed by impingement.
The gas effluent exits the HEPA filter via conduit 57 and enters a halogen adsorber 18 which removes halogen by adsorption. The halogen atoms are held on the surface of the material by chemical bond with the adsorbing agent and decay t~ a stable atom. For instance, radioactive iodine decays to stable xenon, Examples of adsorbing agents include activated charcoal and silver impregnated solids such as silver silicates and silver zeolites.
The temperature and flow rate of the ga5 effluent through the HEPA filter and iodine adsorber is between about 40 and about 55C and about 350 CFM and about 550 CFM, respec-tively. Following the iodine adsorber, the gas effluent is directed via conduit 58 to a second HEPA filter 19. Co~bina-tions of the two HEPA fîlters 17 and 19 and iodine adsorber 18 .

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are commercially available and need not be disclosed in any greater detail herein.
The gas effluent leaving the HEPA filter via conduit 59 is sufficiently decontaminated-that any amounts of radio-active material which may be present in the gas are well below the levels permitted by the plant operating iicense and accord-ingly can then be discharged by means of a pump 20 and conduit 60 to the atmosphere.
As discussed hereinabove, a halogen getter can be introduced into the scrub solution tank 21 via conduit 46 so as to maintain the halogens in ionic form in solution for decay to a sta~le nonradioactive daughter. The scrub solution is removed from the scrub tank via conduit 61 and pump 23, In addition, if desired, a strainer 22 for removing solid particles can be included in line 41 between scrub tank 21 and pump 23.
Scrub liquor is then fed to a heat exchanger 24 wherein it is cooled sufficiently so that a portion of it can be recycled as the spray in quench tank 12 and venturi scrubber 13 via conduit 62. The remaining scrub tank liquor can then be returned to liquid waste tank l via conduit 63. The temperature downstream of the scrub cooler is typically about 30C. A typical flow rate of the scrub solution to the quench ta~X and venturi scrubber i9 about 15 gallons/minute and that of the scrub solu-tion recirculating to the scrub solution tank i9 about lO
gallons/minute.
~ he present invention makes it possible to reduce the volume of dry compacted solids by at least about 80 times, -- .

4~3 spent resins by at least about 18 times, concentrated liquids by at least about 8 times, and filter sludges by at least about 5 times.

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Claims (10)

WHAT IS CLAIMED IS:

1. A method for treating of waste which comprises:
(A) providing a fluidized bed incinerator and calciner wherein the bed material is resistant to oxidization, agglomera-tion, and attack by chemicals at tem-peratures up to at least about 1000°C;
(B) providing combustion conditions in the fluidized bed incinerator and calciner;
(C) feeding the waste into the fluidized bed region of the fluidized bed incin-erator and calciner;
(D) supplying fuel and oxygen-containing gas to the incinerator and calciner to main-tain combustion conditions therein;
(E) introducing gas into the fluidized bed region of the incinerator and calciner at a velocity sufficient to maintain the bed particles in the form of fluidized particles;
(F) incinerating or calcining said waste;
(G) passing a gas effluent from said incin-erator and calciner to a dry cyclone wherein particles are separated from the effluent;
(H) removing solid particles from said dry cyclone and passing them to a storage container;

(I) removing a gas effluent from the cyclone and passing it to a quench tank;
(J) introducing liquid into said quench tank for cooling and wetting particles con-tained in the gas effluent;
(K) removing liquid particles from said quench tank and passing them to a scrub solution tank;
(L) removing a gas effluent from the quench tank and passing it to a venturi scrubber;
(M) introducing liquid into the venturi scrubber to wet particles remaining in the gas efflu-ent and cause condensation of water vapor;
(N) removing a gas effluent and wetted particles from the venturi scrubber and passing them to a wet cyclone;
(O) removing liquid particles from the wet cyclone and passing it to a scrub solution tank;
(P) removing a gas effluent from the wet cyclone and passing it to a condenser for condensing liquid vapor;
(Q) removing a gas effluent and condensed liquid particles from the condenser and passing them to a demister;
(R) removing liquid particles from the demister and passing them to a scrub solution tank;

(S) removing a gas effluent from the demister and passing it to a heater for raising the temperature of the effluent for evaporation of remaining liquid droplets;
(T) passing the effluent through a filter for removal of remaining solid particles and through a sorber for removing halogen gases therefrom.

2. The method of claim 1 wherein said waste is radio-active waste.

3. The method of claim 1 wherein said bed material is olivine.

4. The method of claim 3 wherein said olivine has a particle size of about 0.5 - 1.5 mm.

5. The method of claim 1 wherein said calcining is carried out at about 400°C.

6. The method of claim 1 wherein said incinerating is carried out at about 1000°C.

7. The method of claim 1 wherein liquid introduced into said quench tank is from said scrub solution tank.

8. The method of claim 1 wherein liquid introduced into said venturi scrubber is from said scrub solution tank.

9. The method of claim 1 wherein said bed material has the following properties:
Hardness (Moh) 6.0 9.0 Specific Gravity 3.2 - 3.9 Dry Bulk Density 100 - 125 (lbs./cu. ft.) Coefficient of Thermal Expansion 0.0083 (in./in./°F) Fusion Point 2300 - 3200°F
(1538 - 1760°C) High temperature reaction Basic High heat absorption Silicosis free Particle size About 0.5 - 1.5 mm.

10. The method of claim 9 wherein said bed material is selected from the group consisting of chrysolite, olivine, kyanite, corundum, alumina, and mixtures thereof.