7 7 IN FLUID BED SYSTEMS Df INDUSTRIAL AND HAZARDOUS WASTE COMBUSTION L720 By John F. Mullen and Robert J. Sneyd Keel er/Uorr-Ol i ver, Stamford, CT 06904 INTRODUCTION .--.I___ Although there i s a general perception that fluid bed combustion i s a new technology, primarily because of its relatively recent application to coal fired steam production, fluid beds have been utilized in industry for over 60 days. technology was applied to catalytic cracking of heavy oils and to metallurgical roasting applications i n the late thirties, and i n subsequent years applied to calcining, drying, sizing, cooling and combustion processes. Dorr-Oliver, the world leader i n fluid bed development, has installed 775 reactors worldwide, ranging i n size from 3 to 45 foot reactor working diameter. Beginning i n Germany i n the twenties for coal gasification, the The increasingly difficult disposal problem for industrial and municipal wastes, including hazardous wastes, has generated interest i n further application of fluid bed technology. variety of liquids, sludges and solids in an energy efficient and environmentally acceptable manner make it suitable for many applications. Its unique ability to combust a wide OPERATI ON DESCRIPTION -.----- Figure 1 i s a schematic representation of a fluid bed reactor. Combustion/fluidizing air i s supplied by a blower to the windbox and distributed through a constriction plate to the bed itself. (generally of silica sand) i s levitated by the upcoming air and the solids-gas mixture takes on the characteristics of a liquid. The inert bed This suspended sol ids-gas mixture has a vigorous boi 1 i ng action resul ti ng i n rapid and thorough mixing of the feed combustibles, oxygen and hot bed medium, and providing an ideal environment for combustion. The flue gas proceeds through the freeboard where combustion (particularly of volatiles) i s completed if required and the larger solid particles entrained in the flue gas are disengaged and fall back into the bed. ADVANTAGES OF FBC'S Many of the advantages of fluid bed combustion can be derived from the previous description of i t s mode of operation, such as: 1- -- -- -- - 1. The intimate mixing in the bed provides virtually complete combustion at low excess air levels, maximizing utilization feed calorific value. Uni forin temperature and atmosphere i n a single reaction chamber provides for single accurate measurement of process conditions, resulting i n ease of process control and simplified automation of the process. 2. 7
Transcript
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I N FLUID BED SYSTEMS Df INDUSTRIAL AND HAZARDOUS WASTE COMBUSTION L720
By John F. Mul len and Robert J . Sneyd Keel er/Uorr-Ol i ver, Stamford, CT 06904
INTRODUCTION .--.I___
Although there i s a general percept ion t h a t f l u i d bed combustion i s a new technology, p r i m a r i l y because o f i t s r e l a t i v e l y recen t a p p l i c a t i o n t o coal f i r e d steam product ion, f l u i d beds have been u t i l i z e d i n i ndus t r y f o r over 60 days. technology was app l i ed t o c a t a l y t i c c rack ing o f heavy o i l s and t o m e t a l l u r g i c a l r o a s t i n g app l i ca t i ons i n the l a t e t h i r t i e s , and i n subsequent years app l i ed t o ca l c in ing , dry ing, s i z ing , c o o l i n g and combustion processes. Dor r -O l iver , the wor ld leader i n f l u i d bed development, has i n s t a l l e d 775 reac to rs worldwide, ranging i n s i z e from 3 t o 45 f o o t reac to r working diameter.
Beginning i n Germany i n the twent ies f o r coal g a s i f i c a t i o n , the
The inc reas ing l y d i f f i c u l t d isposal problem f o r i n d u s t r i a l and munic ipa l wastes, i n c l u d i n g hazardous wastes, has generated i n t e r e s t i n f u r t h e r a p p l i c a t i o n o f f l u i d bed technology. v a r i e t y o f l i q u i d s , sludges and s o l i d s i n an energy e f f i c i e n t and env i ronmenta l ly acceptable manner make i t s u i t a b l e f o r many app l i ca t i ons .
I t s unique a b i l i t y t o combust a wide
OPERATI ON DESCRIPTION -.-----
F igure 1 i s a schematic representa t ion o f a f l u i d bed reac tor . Combust ion / f lu id iz ing a i r i s suppl ied by a blower t o the windbox and d i s t r i b u t e d through a c o n s t r i c t i o n p l a t e t o the bed i t s e l f . ( genera l l y of s i l i c a sand) i s l e v i t a t e d by the upcoming a i r and the sol ids-gas m ix tu re takes on the c h a r a c t e r i s t i c s o f a l i q u i d .
The i n e r t bed
Th is suspended so l ids-gas m ix tu re has a v igorous b o i 1 i ng a c t i o n resu l ti ng i n r a p i d and thorough m ix ing o f the feed combustibles, oxygen and h o t bed medium, and p rov id ing an i dea l environment f o r combustion. The f l u e gas proceeds through the freeboard where combustion ( p a r t i c u l a r l y o f v o l a t i l e s ) i s completed i f requ i red and the l a r g e r s o l i d p a r t i c l e s en t ra ined i n the f l u e gas a re disengaged and f a l l back i n t o the bed.
ADVANTAGES OF FBC'S
Many o f the advantages o f f l u i d bed combustion can be der ived f r o m the prev ious d e s c r i p t i o n o f i t s mode o f operat ion, such as:
1- -- -- -- -
1. The i n t i m a t e m ix ing i n the bed prov ides v i r t u a l l y complete combustion a t low excess a i r l e v e l s , maximizing u t i l i z a t i o n feed c a l o r i f i c value.
Uni forin temperature and atmosphere i n a s i n g l e reac t i on chamber prov ides f o r s i n g l e accurate measurement o f process cond i t ions , r e s u l t i n g i n ease o f process c o n t r o l and s i m p l i f i e d automation o f the process.
2.
7
3.
4.
5.
6.
7.
The simple control feature of the FluoSolids Reactor allows the e f f i c i en t use of subautogenous or superautogenous feed or of feed which sh i f t s between the two. When b u r n i n g superautogenous feeds, heat exchanger surfaces, (usually steam generating tubes) can be intal led direct ly i n the bed. This takes advantage of the higher heat transfer coefficients available on the bed side (about five times greater than those i n a conventional bo i le r ) , since the bed material has the character is t ics of a l i q u i d . can be preheated ( u p to 1200°F) by the sensible heat of the f lue gas, t h u s reducing or eliminating the need for auxiliary fuel. T h i s l a t t e r system i s shown schematically i n Figure 2 , which we call the h o t windbox system. When feed var iab i l i ty i s such that i t alternately varies above and below autogenous, auxiliary fuel or cooling water can be injected direct ly into the bed, as required, by an automatic system activated by bed temperature.
I n combusting subautogenous feeds, the incoming combustion a i r
Combustible materials entering the bed are subject t o the ful l combustion temperature for residence times on the order o f 5 to 8 seconds or more. This insures e f f i c i en t destruction of organic materials and produces a n i ne r t ash which i s normally suitable for l a n d disposal.
Reactions of combustion and water evaporation are vir tual ly instantaneous and therefore there is a very low inventory of fuel or feed anywhere in the system. T h i s permits start-ups and shut-downs i n a matter of minutes when reactor i s near operating temperature. This character is t ic , coupled w i t h the slow ra te of bed cooling i n a shut-down reactor (5°C per hour), permits intermittent operation i f desirable, w i t h l i t t l e or no auxiliary fuel use.
The large inventory of bed material acts as a thermal flywheel, minimizing thermal shock t o the refractory. of moving parts i n the hot zone, resul ts i n low maintenance cost.
T h i s feature, combined w i t h the absence
The low temperature combustion of f luid beds inherently produces lower concentrations of NO,. Should additional control be required, staged combustion can be readily achieved i n a single reactor, by r u n n i n g the bed low on stoichiometric a i r and introducing overbed a i r f o r secondary combustion i n the freeboard.
Because of i t s f l ex ib i l i t y , f lu id bed technology has the potential for comustion of a wide variety of waste feeds. which have been successfully combusted i n the t e s t reactor a t Dorr-Oliver's Springdale Laboratories or which by nature of the i r physical and chemical properties are readily amenable t o f l u id bed combustion. Further discussion and experimental tes t ing on industrial wastes from the paint, p last ics , rubber and t ex t i l e industries is reported i n reference 1. feed f l ex ib i l i t y of f lu id beds, D-0 commercial reactors have burned sol ids , sludges, 1 i q u i d s and gases, wi t h fuel vaql ues of 400 t o 18500 Btu/l b , and wi t h water contents ranging from dry t o greater than 90% water.
7 Table 1 i s a l i s t i ng of feeds 1
E: As an i l lus t ra t ion of the
- 1 F l u i d beds are
8
p a r t i c u l a r l y app l i cab le t o v o l a t i l e solvents, sludges and t a r r y wastes, which are d i f f i c u l t t o handle i n a convent ional b o i l e r , w h i l e m a t e r i a l s wi th s i g n i f i c a n t amounts o f coarse non-combustible so l ids , such as glass, metal o r rocks, a re genera l l y n o t su i tab le . S i m i l a r l y , f l u i d bed reac to rs are capable o f hand l ing the poorer mater ia l s, t y p i c a l l y those w i th h igher mois ture conten t o r low c a l o r i f i c value, w h i l e f l u i d bed o r convent ional b o i l e r s a re genera l l y more app l i cab le f o r feeds w i t h h igher c a l o r i f i c values. l i m i t e d i n s i z e and shape o f feed, i n t h a t the r e s u l t a n t ash res idue must be capable o f be ing f l u i d i z e d .
F l u i d beds are
SYSTEM CONFIGURATION - Three v a r i a t i o n s i n reac to r type have a l ready been discussed: windbox f o r autogenous fue l s , the h o t windbox f o r subautogenous f u e l s and t h e c o l d windbox w i t h bed c o i l s f o r superautogenous fue ls . t he process f l o w diagrams f o r the th ree systems. energy recovery systems. i nc ine ra to rs , we l l over 90% o f recent i n q u i r i e s t o Dor r -O l iver f o r these systems have s p e c i f i e d energy recovery, usua l l y as steam, b u t a l so as process heat i n the form o f h o t gas, a i r o r water. Note t h a t even w i t h the windbox system, downstream energy recovery may prove economi a1 , since w i t h heat exchanger f l u e gas exhaust temperatures ranging from 1000 t o 1200°F, over 30% of the i n p u t lower heat ing value o f the f u e l i s recoverable heat downstream. The a i r p o l l u t i o n c o n t r o l device u t i l i z e d i s a f u n c t i o n o f the system requirements. The l e a s t c a p i t a l in tense i s t he wet v e n t u r i scrubber; however, t h i s produces a wet ash which normal ly e n t a i l s a d d i t i o n a l d isposal opera t ing expense, unless a lagoon i s ava i lab le . baghouses, e l e c t r o s t a t i c p r e c i p i t a t o r s and spray devices. devices can a l so be used t o c o n t r o l gaseous emissions; e.g., ch lo r ine .
HEAT BALANCE AND SYSTEM PRELIMINARY DESIGN
The bas ic method i n s i z i n g a f l u i d bed r e a c t o r system i s f i r s t conduct ing a heat balance o f t he r e a c t o r as i s shown schemat ica l ly i n F igure 6. s i z i n g o f t he r e a c t o r and downstream components i s b a s i c a l l y a f u n c t i o n o f t he exhaust volume, reduc t i on o f t h i s volume w i l l u s u a l l y r e s u l t i n lower c a p i t a l cos ts . dewatering (a l though t h i s w i l l r a i s e the dewatering system cos t ) , use o f minimum excess a i r , and ma in ta in ing minimum reac to r temperature t o sus ta in combustion. minimum c a p i t a l c o s t i s achieved by us ing d i r e c t bed water a d d i t i o n t o ma in ta in reac to r temperature. i s desired, water a d d i t i o n i s t he l e a s t e f f i c i e n t method (because of t h e unrecoverable heat o f vapor i za t i on ) . and t h e use of in-bed heat recovery c o i l s prov ides the h ighes t e f f i c i e n c y . Thus t h e ac tua l t o t a l system i s o f t e n a ser ies of t radeo f f s , among components o f c a p i t a l c o s t and l i f e cyc le cost . i n c l u d e cons ide ra t i on o f such f a c t o r s as feed s i z e and s i z e d i s t r i b u t i o n , feed moisture, c a l o r i f i c value, feed chemical cons t i t uen ts , as f u s i o n temperature, and a u x i l i a r y f u e l c h a r a c t e r i s t i c s .
-I
the c o l d
F igures 3, 4 and 5 a r2 A l l th ree f i g u r e s i nc lude
While f l u i d beds can be operated pure ly as
Dry ash producing systems inc lude Most o f these
Since
The q u a n t i t y o f exhaust gas can be m i n i m i zed by maximum feed
For superautogenous fue ls , where i n c i n e r a t i o n on ly i s desired,
On the o ther hand, if energy recovery as steam
Excess a i r a d d i t i o n i s more e f f i c i e n t
Fur ther , a complete system design w i l l
9
However simplifying assumptions may be made t o permit a determination of whether a hot or cold windbox i s required and to determine preliminary component sizing and potential heat recovery. If we consider a waste material w i t h a s ignif icant moisture content, the heat loss associated M i t h the ash is re1 a t i vely small and can be neglected. temperatures and S X C ~ S S a i r requirements may vary over a substantial range depending on the waste feed character is t ic and the optimization parameter (minimum capital cost , maximum thermal efficiency, e t c . ) , 1500°F and 40% excess a i r will generally be a good f i r s t assumption for f l u i d bed combustion.
Simi 1 arly whi 1 e combusti on
A signif icant parameter i n the design o f a f l u i d bed reactor system i s the relationship between the fuel heating value and i t s water content which is called the Specific Feed Characteristic (SFC). ( h i g h ) heating value of the feed per u n i t mass of moisture.
Using the assumptions above, beat balance data f o r the al ternate systems shown i n the flow diagrams may be determined and are shown i n Table 2. following conclusions w i t h regard t o SFC may be drawn:
T h i s i s defined as the gross
The
1. Feed materials w i t h an SFC of 4000 Btu/pound water are exactly autogenous i n a cold windbox reactor.
2. Feed materials w i t h an SFC o f 2600 Btu/pound water are exactly auto enous i n a hot windbox reactor w i t h a combustion a i r preheat of 1000°F. ?If preheat i s raised t o 1200"F, the autogenous SFC drops to 2400 Btu/pound water. 1
3 . Feed materials w i t h an SFC greater than 4000 Btu/pound water are superautogenous and excess combustion heat may be recovered direct ly by steam generating co i l s immersed i n the f l u i d bed. Alternatively excess heat may be absorbed via excess a i r or in-bed water injection.
Feed materials w i t h an SFC l e s s t h a n 2600 (2400 w i t h 1200°F a i r preheat) a re non-autogenous even w i t h internal heat recuperation and will requi re auxiliary fuel f o r combustion.
4.
5. Feed materials w i t h an SFC between 2600 and 4000 are in t r ins ica l ly non-autogenous, b u t may be made autogenous by internal heat recuperation. A1 ternatively, auxiliary fuel may be used to sustain combustion. Auxiliary fuel combustion will resu l t i n lower capital cost b u t higher operating cost.
6. When internal heat recuperation is used to minimize or eliminate the use o f auxiliary fuel, i t a1 so has the effect of reducing the heat available for recovery by downstream heat recovery devices.
, I i
T h u s the SFC can be used for a preliminary determination of whether a hot or cold windbox system i s required. W i t h th i s determination made, the capacity data of Table 3 may be used to determine an approximate reactor size. the graphical summation Figure 7, and a known value o f SFC, a required
From
7
1 0
auxiliary fuel ra te for sub-autogenous fuels and the potential for heat release can be determined. While the final design of a f l u i d bed system is dependent on many variables tha t are not discussed above, the methodology outlined serves as a useful f i r s t apprximation for system design and s iz ing .
I N DUSTRI AL APPL ICATI ON S
In the past twenty years, Dorr-Oliver has instal led over 160 combustion systems handling industrial and municipal waste. Instal led system capacit ies range from 2 t o 140 million B t u per hour.
-
The f i r s t industrial instal la t ion was in 1962 to burn spent coffee grounds and tea leaves. T h i s was a 15' diameter reactor w i t h an i n p u t feed capacity of 25 million Btu/hour. down because of process changes a t the plant.
The largest single industrial combustor i s a 28' inner diameter, capable of burn ing refinery oily wastes a t a rate of 70 million Btu/hour.
I t was operated successfully through 1977 when i t was s h u t
A representative l i s t of wastes burned i n FluoSolids ins ta l la t ions i s given i n Table 4. i n a f lu id bed. Table 4 i s res t r ic ted to only those wastes actually combusted on a commercial basis i n a fu l l s ize Dorr-Oliver c l i en t owned reactor.
Whereas Table 2 provides a l is t ing of wastes amenable to combustion
HAZARDOUS WASTES
The basic performance cr i ter ion for hazardous waste incinerator design is achieving 99.99% destruction and removal efficiency ( D R E ) of the Primary Organic Hazardous Constituents (POHC) i n the waste. The two other RCRA defined performance c r i t e r i a -- particulate release and HC1 emission -- are essenti a1 ly control led by downstream components rather t h a n the incinerator i t s e l f . The efficiency of the destruction reaction s both time and temperature dependent. i s tha t they have inherently longer gas residence time a t temperature (normally on the order of f ive to ten seconds) than most competing technologies. ( I n e f fec t , the freeboard of the f luid bed ac ts as an afterburner.) As a resul t , equivalent values of DRE can often be obtained a t lower operating temperatures. This i s of particular advantage when the waste i s sub-autogenousy since less auxiliary fuel i s required to achieve combustion, or when the waste i s a sludge b e i n g dewatered to achieve autogenicity, since a lower level of dewatering i s required.
An important point i n considering f l u i d bed reaactors
AS early as 1975, t e s t s for hazardous waste destruction were conducted i n a Dorr-Oliver reactor instal led a t Franklin, Ohio. T h i s work (Reference 2 ) was done by TRW Defense and Space Systems Group for the EPA Office of S o l i d Waste Management. instal led in 1970 t o burn municipal refuse and a primary and secondary sludge. (1 ) an aqueous solution of methyl methacrylate monomer and ( 2 ) an aqueous/cresol sludge. Composition of the waste streams i s given in tables 5 and 7 while operating conditions and t e s t resu l t s are shown in table 6 and 8. constituents was greater than 99.999%.
The reactor is a 25' freeboard diameter, cold windbox type
Two separate t e s t s were conducted:
I n both cases, the DRE for the waste
More recently, (within the past two years) , testing was conducted a t a different Dorr-Oliver FluoSolids commercial reactor as a part of i t s Part B Hazardous Waste i nci nerati on Permit process under RCRA. permit has not ye t been issued, the c l i en t operator does not w i s h t o be identified a t t h i s time, and detai ls of the i n s t a l l a t i o n which might permit such ident i f icat ion cannot be released. Similarly, because the final approval by €PA is s t i l l pending , test resu l t s must be viewed as preliminary. Reactor feeds, hazardous consitutents, operating conditions and tes t results are shown on Table 9. detectable. carbon tetrachloride, c lass i f ied by EPA as one of the more d i f f i cu l t t o b u r n wastes (Reference 3 ) .
Because the f i nal
DREs ranged from 99.996% t o greater than 6 nines w i t h P I C s not Of particular significance i s the destruction, a t 1600"F, of
Fluid bed technology has been proven in commercial plants a s a cost effect ive and environmentally acceptable s o l u t i o n t o combustion o f a wide range o f l iquid and solid wastes, including hazardous waste.
Preheating of incoming combustion a i r in a hot windbox can significantly reduce or el iminate the need for auxi 1 i ary fuel. Conversely, energy recovery can be optimized for over-autogenous fuels by the use of in-bed heat recovery tubes.
Al though f inal design of a FluoSolids system will require an optimization of design parameters, a preliminary evaluation and system s i t i ng may be accomplished relat ively simply th rough the use of the Specific Feed Characteristic.
REFERENCES - 1.
2.
3.
"F1 u i d i zed Bed I nc i ne r a t i on of Sel ec ted Carbonageou s I n d u s t ri a1 Wastes" Prepared by Batelle Laboratories, Columbus, Ohio for the Sta te of O h i o Department of Natural Resources under Grant 12120FYF. March, 1972.
Ackerman, D.G. , e t a1 . (TRW Defense 81 Systems Group) "Destroying Chemical Wastes i n Commercial Space Incinerators. Faci l i ty Report No. 3-Systems Technology" Prepared for U.S. EPA, Office of Solid Waste Hanagement, Washington, D.C., April, 1977, NTIS No. PB-265-540.
Bonner, T.A., e t a1 , "Engineering Handbook for Hazardous Waste Incineration. 'I EPA SW-889. Prepared by Monsanto Research Corp., Dayton, Ohio for U.S. EPA, Industrial Environmental Research Lab, Cincinnati , Ohio under Contract EPA 68-03-3025. September, 1981.
1 2
7 Figure I . Cold Windbox Reactor System
7
3
Sight glass\
4
Feed Nozzle
‘I
inlet - Air I
Scrubber exhaust -
Windbox
Fuel 4 Nozzle
13
- -
- 4 -
Scrubber cooling
Sigh glas!
Heat exchanger
:uel rozzle 1
Scrubber exhaust
Air blower
i i
Scrubber cooling il
L
Figure 2. Hot Windbox Reactor System with Air Preheating
-1
FIGURE 3 COLD WINDBOX WITH WASTE HEAT BOILER.
PROCESS FLOW DIAGRAM
RECOVERED HEAT
STEAM + I
FEED WATER
> EXHAUST GASES
ASH HOT GAS
BOILER SYSTEM WASTE HEAT CLEANUP
FLUOSOLIDS REACTOR
WASTE FEED
-----.I
b
BLOWER
15
FIG. 4
HOT WlNDBOX WITH WASTE HEAT BOILER. PROCESS FLOW DrIAGRAM
- RECQWRSD MEAT I N m-
STBEM _ _ PEE@ WATER
I SX)fAUST GASES
LIsn .-..- WTGAS CLEARUP
FLUOSOLIDS
WA
AUXILIARY FUEL - - - (IF NEEDED)
WASTE BOILER
COMBUSTIOW AIR
16
'3 ..
I -I "-
[3
'1.1 1 1
FIG. 5
COLD WINDBOX WITH BED COILS AND WASTE HEAT BOILER. PROCESS FLOW DIAGRAM
RECOVERED HEAT
STEAM
EXHAUST GASES
FLUOSOLIDS
BLOWER
3
- ' 1 17
FIGURE 6 O V E N HEAT BALANCE
WASTE FEED L
COMBUSTION I
AIR
AUX FUEL, AIR OR H 0 - (IF NEEDED)
HEAT IN
(4) COMBUSTION
PRODUCTS c-
WATER
VAPOR -
EXCESS AIR - I 1
HEAT OF COMBUSTION (FEED COMBUSTIBLES + AUXILIARY FUEL)
FLUID BED 2: COLD WINDBOX 0 0 -- + o s 4 > 3 WITH BED COILS BOILER
-7 3
75
61.
MUNICIPAL WASTES I I 1 1 1 1 1 I I I I I I I ] 1-1 SECONDARY SLUDGES
'Yo COMBUSTION HEAT INPUT
- - -
AUXILIARY FUEL -
a
% COMBUSTION - HEAT RELEASE
- HEAT RECOVERY -
I I i I I I I I I I I I l l 1
100
00
30
io
10
!O
D too
IO
io
10
!O
I
1,000 2,600 4,000 10,000 BTU (HHV)/LB WATER 100,000
,J
~
2,300 23,000 MJ (HHV)/kg WATER 230,000
19
TABlE 1 POTENTIAL PROBUM WASTES COMBUSTIBLE IN FUJID BEDS
Animal oils & rendering wastes API separator sludges Carbon Tetrachloride Soluble oils Catalyst complexes Solvents Coal Water Wastes Coolants Thinners Cresol Vegetable oils Cutting oils & sludges Washer liquids DAF F b a t Detergent sludges Wastes from the manufacture of Dves Ammonia Food Processing Wastes Caprolactam Feedlot Wastes Coal Preparation Halogenated Organics Ethylene glycol Inks Methacrylates Oily wastes Methylamines Organic tars Nylon Intermediates Paint sludges & residues Peroxide Pesticides Pharmaceuticals Phenois Roofing Materials Polymers Textiles Resins Urea
Skimmer refuse Soap & detergent cleaners
Still & reactor bottoms
:J " I:
20
7 3
.I ."..
11
~ :I .-
._. '1 '-1 ...
I :1 nl
TABLE 2 HEAT BALANCE OF FLUID-BED COMBUSTION SYSTEMS.
System Fig. No. 3 4 5
Internal heat Recuperation Combustion Air, F'
Internal Heat Recovery (Bed Coils)
External Heat Recovery Exhaust Gases, F"
Combustion Heat input, Btu/Lb Water Evaporated
Net Heat Recovery % Combustion Heat Release'""
No Yes No 78 1000 78 No No Yes
Yes Yes Yes 500 500 500
4000 2600 6000
51 34 60
'Dorr-Oliver FluoSolids system feature combustion air preheating to 1 2OO0F, and a refractory arch constriction plate suitable for 1800°F windbox temperature.
"Firetube or water tube boiler, 500°F gas outlet, 350°F with economizer "'Combustion Darameters 1500°F. 40% excess air.
TABLE 3 SELECTED CAPACITY RATINGS OF FLUOSOLIDS REACTORS.
Reactor Cold Windbox H o t Windbox Size" Dia. Heat Release Evaporation Rate
'Standard reactor sizes available in diarneteis 4 to 35 ft diameter 1 ft increments SI Conversion m ft x 0 3048, W Btu/h x 2 093, kg Ib x 0 454
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TABLE 4 WASTE TYPES
PROCESSED IN DORR-OLIVER COMMERCIAL FLUID BED COMBUSTORS
1. MUNICIPAL SEWAGE SLUDGES
A. PRIMARY SLUDGE B. SECONDARY OR ACTIVATED SLUDGE C. DIGESTED SLUDGE D. BlOFlLTER SLUDGE E. PHOSPHATE EXTRACTION PROCESS SLUDGE
F. HEAT TREATED SLUDGE G. SCUM, GRITS, SCREENINGS H.
LIME, ALUM, FERRIC CHLORIDE
COMBINATIONS OF ALL OF THE ABOVE
II. INDUSTRIAL SLUDGES & WASTES
A. PAPER PULP WASTE SLUDGE B. PETROLEUM REFINERY WASTES C. OIL TANKER SLUDGE D. PHARMACEUTICAL SLUDGES E. AUTOMOBILE MFG SLUDGES F. LIVE STOCK (PIG) FARMS G. SODA ASH MFG H. NYLONMfG 1. CARBON BLACK FROM ACETELYNE J. WOOL WASHING WASTE K. BREWERY WASTES L. PLASTIC MFG WASTES
111. MISCEWNEOUS WASTES
A. B. SPENT TEA LEAVES C. COFFEE GROUNDS D. ANTHRACITE CULM E. PULP MILL SPENT COOKING LIQUOR
RDF (REFUSE DERIVED FUEL FROM GAREAGE)
3
22
EPA HAZARDOUS WASTE NO.
u002
u220 U239 U019 U188 U052 U052
TABLE 5 HAZARDOUS-TOXIC WASTE COMBUSTION AT DORR-OLIVER-BLACK CIAWON FLUID
BED COMBUSTOR AT FRANKLIN OHIO BY SYSTEM TECHNOLOGY CORPORATION (SYSTECH)
FLUID BED COMBUSTOR AT FRANKLIN, OHIO OPERATION CONDITIONS
DORR-OLIVER - BLACK CLAWSON - SYSTECH
t I IJIC) BLD TEMPERATURL F NEE BOARD TEMPERATURE % EXCESS AIR (APPROXIMATE) RESIDENCE TIME (SECONDS) WASTE FEED RATE (LITERS/MIN) WASTE/AUXILIARY FUEL (LITER/LITER) (NO. 2 FUEL OIL)
WEIGHT % SOLIDS
0.43 0.50 0.36 0.07 0.50 2.15 4.29 5.73
26.50 6.45
13.61
60.59
39.40
SYSTEM PERFORMANCE DESTRUCTION EFFICIENCY
TOTAL ORGANICS PERCENT WASTE CONSTl TU E NTS PERCE N1
BED COMBUSTOR AT FRANKLIN OHIO BY SYSTEM TECHNOLOGY CORPORATION (SYSTECH)
COMPOSITION OF METHYL METHACRYLATE WASTE
AT DORR-OLIVER-BUCK CUWSON FLUID
EPA )(A;zARDous WASTE NO.
u154 u002 U158
U162
u220 U239 u112 U188 U052
JC
WEIGHT % COMPOUND WEIGHT % SOUDS
METHANOL ACETONE METHYLENE CHLORIDE
METHYL PROPANOATE METHYL METHACRYLATE
TOLUENE XYLENE
PHENOL CRESOL
2-BUTANONE
2-ETHOXY ETHANOL
2-ETHOXY ETHYL ACETATE
SUB TOTAL
J COMBUSTIBLE SOLIDS
WATER
TOTAL
4.9 0.7 0.7 1.1 0.4
33.9 0.4 1.1 0.9 0.4 12.6 3.4
60.5
1.7
37.8
100.0
7.9 1 .I 1 .I 1.8 0.6
54.5 0.6 1.8 1.4 0.6
20.3 5.5
97.2
2.70
TABLE a METHYL METHACRYLATE WASTE COMBUSTION IN
DORR-OLIVER - BLACK CLAWSON - SYSTECH FWlD BED COMBUSTOR AT FRANKLIN, OHIO
OPERATING CONDITIONS
FLUID BED TEMPERATURE FREEBOARD TEMPERATURE % EXCESS AIR (APPROXIMATE) RESIDENCE TIME (SECONDS) WASTE FEED RATE (LITERS/MIN) WASTE/AUX I Ll ARY FUEL ( LITER/ LITER ) (NO. 2 FUEL OIL)
