CA1057584A

CA1057584A - Process for burning carbonaceous material

Info

Publication number: CA1057584A
Application number: CA260,489A
Authority: CA
Inventors: Lothar Reh; Martin Hirsch; Per H. Collin; Sune N. Flink
Original assignee: Metallgesellschaft AG
Current assignee: GEA Group AG
Priority date: 1975-09-05
Filing date: 1976-09-03
Publication date: 1979-07-03
Also published as: FR2323101A1; IN143376B; ZA763293B; RO86704B; AU1572476A; SE7609676L; SU898960A3; GB1510946A; DE2539546B2; AU500206B2; CS212255B2; RO86704A; DD126526A5; FR2323101B1; JPS5233132A; DE2539546A1; BE845872A; DE2539546C3; SE424225B; SE424225C

Abstract

ABSTRACT OF THE DISCLOSURE:

Carbonaceous material, preferably coal or the like finely divided solids with a mean particle diameter of 30 to 250 microns, is burned to produce steam in a fluid bed furnace having a lower free space without internal fixtures and provided above this free space with internal cooling surfaces. A secondary gas inlet introduces the secondary gas so that the volume ratio of fluidizing gas to secondary gas ranges from 1:20 to 2:1 at a location above the fluidizing gas and fuel inlets but below the internal cooling surfaces, the gas velocity of the several gases being adjusted so that the mean suspension density of the solids above the secondary gas inlet is 15 to 100 kg/m3. Approximately stoichiometric conditions are maintained with respect to the oxygen in the gases introduced and the carbonaceous material and solids are recycled to the bed after being separated from the gases emanating therefrom.

Description

1057589t This inventlon relates to the process of burning carbonaceous materials under approximately stoichiometric conditions in a fluid bed, wherein the discharged solids are recycled to the fluid bed and heat of combustion is dissipated through cooling surfaces.
Numerous systems have already been used to burn carbonaceous materials. It is known, inter alia, to use for this purpose fluidized-bed reactors operated as described herein-before (see British Patent Specification 784,595 and J.R. GRACE, "Fluidization and its Application to Coal Treatment and Allied Processes", AICHE Symposium Series 141, Vol. 70 (197~), pp. 21-26, and DL.KEAIRNS et al. "DeSign of a Fluidized Bed Combustion Boiler for Industrial Steam Generation", AICH~ Symposium Series 126, Vol, 68 (1972), pp. 259-266.
The known processes have the disadvantages that the height of the bed must be comparatively low so that the pressure loss is kept within reasonable limits, that the presence of cooling surfaces in the lower part of the reactor space involves a disturbance of the transverse mixing of the solids in the fluidized bed so that the inhomogeneities of temperature (over-heating, formation of crusts) occur, and that the op0ration of the reactor cannot be satisfactorily adapted to varying power requirements. An adaptation can be effected virtually by a fall in temperature in connection with modification by combustion and fluidization conditions, or by a shut-down of individual reactor units.
It is an object of the invention to provide a process in which the known disadvantages, particularly those mentioned hereinbefore, are avoided.
3o An object of the invention is to provide a process which can be carried out with minimum structural expenditure with greater economy and without the disadvantages of the earlier ~ 057584 systems mentione~ above.
Another object of the invention is to provide an improved fluid bed combustion system especially for particulate carbonaceous material.s with greater combustion load per reactor volume unit, low nitrogen oxide level in flue gases and improved ability to respond to varying power demands.
St.ill another obJect of the invention is to provide a combustion system for the purposes described which minimizes the level of noxious or toxic components in the flue gases.
It is also an object of the invention to provide an improved system for burning carbonaceous materials which have been burned only problematically heretofore witll respect to temperature homogenei.ty.
These objects are attained according to the invention in that:
(a) combustion is carried out in the presence of oxygen-containing gases, which are supplied in two partial streams at different height levels of an upright fluid bed, and at least one of the partial streams is used as a secondary gas and fed into the combustion chamber on one plane or a plurality of su~eriml~osed planes;
(b) the volume ratio of fluidizing gas to secondar~
gas is adjusted to a value in the range of substantially 1:20 to 2:1;
(c) the gas veloci.ty and the ratio of fluidizing gas to sccondary gas are adjusted to provide above the secondary gas inlet means a f]uldized bed condition having a mean suspension density of 15-100 kg/m3;
(d) at least a substantial part of the heat of combus-tion is dissipated through cooling surfaces disposed in thefree furnace space above the secondary gas inlet means;

(e) a major part of the carbonaceous material is fed into the space which is disposed below the secondary gas inlet means and virtually free of internal fixtures; and (f) solids are withdrawn from the circulation system which comprises the fluid-bed reactor, separator, and recycle conduit.
In one aspect of the invention, there is therefore provided a process for burning a carbonaceous material to produce steam, which comprises the steps of:
introducing carbonaceous material into a fluid bed in an upright reactor;
fluidizing the carbonaceous material in the fluid bed with a primary fluidizing gas introduced at the bottom of the bed and a secondary gas introduced in the fluid bed at a level above that at which the primary gas is introduced and above the bottom of the fluid bed, at least the secondary gases containing oxygen;
burning the carbonaceous material with the oxygen;
maintaining the supply of carbonaceous material and oxygen to the fluid bed at distinct proportions;
maintaining the volume ratio of fl.uidizing gas to secondary gas at substantially 1:20 to 2:1;
removing thermal energy from the fluid bed by disposing therein at a level about the location at which the secondary gas is introduced, cooling surfaces in contact with the fluid bed and extending into the interior thereof;
cooling the surfaces with water to produce steam;
controll.ing the removal of thermal energy by adjusting the mean solids suspension density above the location at which the secondary gas is introduced within the range of 15 to lO0 kg/m3 as a result of the adjusted velocity and the volumé ratio of the gases;

~ 3 ~

~5'~584 controlling the fluidization of the material in the bed to preclude the formation of a discrete upper level of the bed and to ensure a solids density gradient decreasing over substantially the entire height of the reactor;
maintaining below the level at which the secondary gas is introduced, a space substantially free of internal obstruction at which the carbonaceous material is introduced;
separating solids from the gas effluent from the bed at the top thereof to collect solid particles;
recycling the solid particles to the fluid bed at a lower portion thereof whereby the fluid bed and the means for separating and recycling the particles constitute a closed solids circuit; and removing excess solids from the circuit, after the separation thereof from the gas effluent from the bed.
The invention also provides, in a second aspect thereof, an apparatus for the combustion of a carbonaceous material comprising:
an upright vertically elongated fluid bed chamber;
means for introducing the carbonaceous material into a lower portion of the chamber;
means for introdueing a fluidizing gas into the chamber at the bottom thereof;
means for introdueing a secondary gas into the chamber at least one meter above the fluidizing gas inlet means and at a location up to substantially 30% of the total height of the chamber, at least one of said gases containing oxygen sustaining combustion within the chamber;
means for removing a flue gas entraining solid particles from the top of the chamber;
cooling surfaces provided with ducts from a cooling fluid disposed in the chamber and extending into the bed over a region thereof above the secondary gas inlet means, the lOS'7584 chamber having a substantially free space below the secondary gas inlet means;
a separator for removing the particles from the flue gas;
conduit means for recycling the particles separated from the flue gas to the chamber;
a fluidized bed cooler;
means for removing recirculated particles from the cycle formedby the chamber, the separator and the conduit means and introducing same into the cooler;
means for fluidizing the particles in the cooler with one of the gases prior to introducing same into the chamber; and means for passing the other of said gases in indirect heat-exchanging relation with the fluidized particles in the cooler prior to introducing the other gas into the chamber.
The solids are carried with the flue gases from the bed by entrainment and are separated from the flue gases in a single or multistage separation system, being recycled, at least in part to a lower portion of the bed.
This lower portion of the bed is, according to a critical feature of the inventionr free from internal fixtures as note.d above, including any cooling surface which might obstruct an undisturbed movement of the solids and gases of the bed at least from the point of introduction of the primary fluidizing gas (bottom of the bed) to a point at a safe distance from the secondary gas inlet. Such lack of disturbance of lateral solids mixing and of the initial mixing gases and solids has been found to be essential to a satisfactory practice of the invention.
However, it is also important and indeed critical to the present invention that internal cooling surfaces within the column or shaft of the bed are provided above the free space t ~ .

` l~)S7584 and preferably over a major fraction of the heightof the bed, these surfaces being generally in the form of upright fluid-cooled walls.
It has also been found to be critical to control the gas velocities and volumes! especially the ratio of fluidizing gas to secondary gas so as to maintain above the secondary gas inlet a fluidized bed with a mean solids suspension density of 15-100 kg/m3. We have found that deviations from the range result in sharp reductions of heat transfer rates at lower values and increases in energy consumption for higher values leading to a loss of efficiency at either end.
From an orthodox fluidized bed, which comprises a dense phase that is separated from the overlying gas space by a distinct step in density, the fluidized bed used in accordance with the invention differs in that it involves states of distribution which lack a defined boundary layer. There is no drastic change in density between a dense phase and an overlying dust-containing space but the concentration of solids in the reactor decreases continuously in an upward direction to the place at which the solids are entraii~led out of the reactor in a gas stream.
When the operating conditions are de~ined by means of the Froude and Archimedes number, the following ranges are obtained:

0.1 ~ 3/4 . u . Pg ~ 10 g d Pk g and 0.01 ~ Ar ~100 where dk g (Pk~Pg) Pg Y

In the above relations:

~S7584 u = relative gas velocity in m/sec;
Ar = Archimedes number;
Pg = density of the gas in kg/m ;
Pk density of the solid particle in kg/m3;
dk = diameter of the spherical particle in m"
y = kinematic viscosity in m2/sec;
g = constant of gravitation in m/sec.2.
Because all oxygen-containing gases re~uired for the combustion are divided into at least two partial streams which are supplied on different levels, the combustion is effected in two stages. Because of the substoichiometric combustion in a first lower zone and an afterburning in a second higher zone there results a "soft" combustion, which eliminates local overheating so that formation of crusts or clogging is avoided and the formation of nitrogen oxide is limited to values below 100 ppm.
Because internal blockage in the lower reactor space, below the secondary gas inlet means, are avoided as far as possible, a good distribution of the fed carbonaceous material is instantaneously effected. The rapid mixing with the hot bed material ensures good degasification and ignition of the fuel.
If the carbonaceous material is fed in A fineyrained state, e.g., with a mean particle diameter oE 30 - 250 ,u, it has a large surface area so that short reaction times are enabled.
It should be noted that the mean particle diameter of 30 - 250 microns applies principally to fine-grain solid carbonaceous materials which have been found to be particularly suitable for use with the present invention.
The combustion may be carried out in a fluid-bed reactor which is rectangular, square, or circular in cross-section~ The lower part of the fluid-bed reactor may be down-wardly tapered, e.g., conical; this is particularly desirable Y, j`,~! ~
.,,~

1t)5'~584 with reactors which are large in cross-section or where an inert fluidizing gas is used.
Under atmospheric pressure, the gas velocities in the fluid-bed reactor above the secondary gas inlet means are usually above 5 m/sec. and may be as high as 15 m/sec.
The ratio of the diameter to the height of the fluidized-bed reactor should be such that gas residence times of 0.5-8.0 sec., preferably 1-4 sec., are obtained.

- 7a -, .

lUS75~34 The latter parameters are not critical in the sense that if deviation from these ranges occur, the system will become inoperative or pose an environmental hazard. However, it has been found that a residence time of 0.5-8.0 seconds for the gas traversing the fluid-bed reactor should be maintained for optimum results. If the residence time is greater or less than this range,the system remains operative although various economic disadvantages arise.
The fluidizing gas may consist of virtually any desired ]0 gas which will not adversely affect the quality of the exhaust gas. Suitable gases are, e.g., inert gases such as recycled flue gas (exhaust gas), nitrogen, and water vapor. To increase the combustion rate, it will be desirable, to supply the reactor with a fluidizing gas consisting of a partial stream of the oxygen-containing gases required.
In view of the above, the process can be carried out in the following ways:
1. An inert gas is used as a fluidizing gas. In this case the oxygen-containing combustion gas used as secondary gas must be charged in at least two superimposed planes.

2. Oxygen-containing gas is used as fluid~zinK gas.
In this case it i5 su:Eficient ~o feed secondary gas in one plane, although the secondary gas also can be fed in a plurality of planes in this embodiment.
A plurality of secondary gas inlet openings are preferably provided in each feeding plane.
According to a preferred feature of the invention, the secondary gas is fed on a level which is up to 30% of the total height of the fluid-bed reactor, and at least 1 m, over the fluidizing gas inlet. If in this case the secondary gas is fed in a plurality of planes, the above level refers to the level of the uppermost secondary gas inlet. The feeding on this ,~-~05758~

level ensures that there is a sufficiently large space for the first combustion stage, so that the reaction of the carbonaceous material and the oxygen-containing gas is almost complete in this stage - whether the oxygen-containing gas is supplied as fluidized gas or as secondary gas in a lower plane- and enables the accommodation of sufficiently large cooling surfaces in the upper reaction space disposed over the secondary gas inlet means.
The cooling surface area can be further increased if, in accordance with another preferred feature of the invention, additional cooling surfaces are installed on the wall of the fluid~bed reactor. These cooling surfaces may cover also the wall of the lower part of the reactor because this will not adversely affect the mixing of solids. The wall itself may constitute a cooling surface.
The cooling surfaces consist generally of rectangular tube plates, which are cooled by a force-fed fluid and are spaced at least 150 mm. preferably 250-500 mm, apart. Such Gooling surfaces are used also in cooling walls. The axes of the tubes should be parallel to the direction of flow of the gas-solids suspension because this results in a minimum of erosion, Whereas this results in a slightly lower heat transfer per unit of cooling surface area than an arrangement of tubes having a horizontal axis, which is at right angles to the direction of flow, the smaller heat transfer is not significant because the process according to the invention permits of an accommodation of large cooling surfaces in the fluid-bed reactor and, if desired, in the succeeding separating and recyclinG unit.
If the carbonaceous materials have only a low content incombustibles, it is not economical to utilize their sensible heat after their withdrawal from the circulation system compris-ing the fluid-bed reactor, the separator, and the recycle conduit. On the other hand, if the content of incombustibles _~_ ~)57584 is high, the heat content will desirably be utilized. To this end, the solids may be cooled in a fluidized-bed cooler. An improved heat balance can be obtained if, in accordance with a preferred feature of the invention, the solids are cooled in a fluidized-bed cooler which preferably comprises a plurality of chambers flown through in succession, and in which gas serving as fludizing gas and/or secondary gas in the fluid-bed reactor is heated, so that the heat content of the solids is returned to the combustion process.
It will also be desirable to extract heat from the exhaust gas from the fluid-bed reactor used for the combustion.
To this end conventional steam boiler technology waste-heat recovery may be adopted or, in a particularly desirable manner, the exhaust gas may be fed as fluidizing gas to a fluidized-bed cooler. The fluidized-bed cooler may be of the Venturi type and may be rectangular or square or circular in cross-section and may consist of tube plates. Heat may alternatively be ex-changed with a coolant flowing in tube bundles. Water is most desirably used as a coolant because the water is thus heated and is then fed to the cooling surfaces of the fluid-bed reactor used for the combustion and is evaporated and/or superheated there.
To minimize the sulfur content of the exhaust gas, the combustion process is preferably carried out in the presence of fine-grained desulfurizing agents such as lime, dolomite and the like. The desulfurizing agents should have approximately the same particle size as the solid carbonaceous material and are simply fed jointly with the latter or are introduced scpa-rately in the fluid-bed reactor.
For a reactor having given dimensions, the capacity can be increased in accordance with a further preferred feature of the invention in that the combustion process is carried out - with oxygen-enriched air rather than with air and/or under i ~ ~ _ 10575~4 superatmospheric pressure, preferably up to 20 kg/cm gauge.
In this case the cooling surface area must be larger than for an operation with air and/or under atmospheric pressure.
This may be accomplished, e.g., by the installation of additional cooling registers in the furnace space above the secondary gas inlet means.
If oxygen-enriched air is used, the density of the suspension in the reactor space above the secondary gas inlet means should lie in the upper part of the range from 15 to lO0 kg/m3 because the heat flow densities are higher and a higher solids concentrations yield higher coefficients of heat transfer.
The main advantage of the process according to the invention resides in that it can be adapted in a very simple manner to the power requirement, which varies substantially in practice. According to a preferred feature of the invention this is accomplished in that the combustion rate is controlled by a control of the density of the suspension in that part of the furnace space of the fluid-bed reactor which is disposed above the secondary gas inlet means.
Given operating conditions, including given flui-dizing gas and secondary gas volume rates and a gtven resulting mean average density of the suspension, are accompanied by a distinct coefficient of heat transfer at the cooling surfaces.
The heat transfer will be increased if the density of the suspen-sion is increased by an increase of the fluidizing gas rate and, if desired the secondary gas rate, At a virtually constant combustion temperature in the whole cyc]e, the increased heat transfer enables the dissipation of the heat at the rate which corresponds to the higher combustion rate. The higher o~ygen requirement which is due to the higher combustion rate is virtu-ally automatically met by the fact that the fluidizing gas and, if desired, secondary gas are fed at higher rates to increase 1) s l~St~584 the density of the suspension.
~ or an adaption to a lower power reauirement, the combustion rate can be controlled by a decrease of the density of the suspension in that part of the furnace space of the fluid-bed reactor which is disposed above the secondary gas inlet.
The decrease of the density of the suspension results in a decrease of the heat transfer so that less heat is dissipated from the fluid-bed reactor and the combustion rate can be decreased sub-stantially without a decrèase in temperature, The carbonaceous material is fed in the conventional manner, most desirably through a single lance or a plurality of lances and preferably by pneumatic blowing. Owing to the good lateral solids mixing, a relatively small number of lances are sufficient and in fluid-bed reactors having small dimensions even a single lance will suffice.
The solid combustion residues entrained by the exhaust gases from the fluid-bed reactor are recycled by means of cyclone separators or baffles or impingement separators in which the gas stream is deflected, The walls of the recycling means are provided, if desired, with coolin~ surface~ which are ~re~erably approached by ~arallel flows.
The final purification of the gases may be accomplished in a conventional way, e,g,, by means of an electrostatic precip-itator. The solids which are thus collected may by recycled into the fluid-bed reactor to minimize the carbon content.
The process according to the invention is particularly suitable for the combustion of coal of any kind, of coal-washing refuse, retort residue, oil shale, fuel oil and mixtures thereof.
Where fuel oil.is used as the carbonaceous material, a bed material is required which consists, e.g. of fine-grained lime or dolomite or other mineral substances having approximately particle sizes in the range of 30 - 250 microns.

~57S~9~

The essential advantage afforded by the process according to the invention resides in that the temperature throughout the circulation system comprising the fluid-bed reactor, separator, and recycling means is more constant than in any previous processes of burning carbonaceous material. The intense motion of solids precludes temperature gradients so that an overheating of individual solid particles is avoided.
In the preferred embodiment of the process, comprising the addition of desulfurizing agents, the fact that temperatures are constant has a beneficial effect also on the desulfurization ef~iciency of the exhaust gases. As a result of the constant temperatures, the desulfurizing agents retain their activity and their capacity to take up sulfur and low ~toichi~metric ratios of Ca:S (less than 2) are needed.
This aclvantage is supplemented by the small particle size of the desulfurizing agent because the sulfur-combining velocity depends mainly on the diffusion velocity and is particu-larly promoted by the existing relation of surface area to volume.
The process according to the invention also enables a complete combustion of the carbonaceous material. In the preferred embodiment of the invention with oxygen rates only slightly above the stoichiometric requirement e.g., not above an excess of 30 % preferably not above 10 % such results are obtained.
The invention will now be explained more ~ully and by way of example with reference to the accompanying drawing and the Examples, In the drawing:
Fig. 1 is a diagrammatic sectional view showing a fluid-bed reactor having a square reactor space;
Fig. 2 is a diagrammatic sectional view showing a fluid-bed reactor having a cylindrical reactor space which has a conical lower part;

1a~5-7~

Fig, 3 is a diagrammatical sectional view showing the fluid-bed reactor of Fig. 1 and the equipment connected thereto.
A fluid~bed reactor l is provided with cooling surfaces

3 disposed above a secondary gas inlet 2. ~dditional cooling surfaces 4 and 5 are disposed on the wall of the fluid-bed reactor 1 and of a separator 6, which is structurally combined with the fluid-bed reactor 1. To show the arrangement of the cooling surfaces more clearly, the several tubes have a horizontal orientation, which differs from the preferred embodiment in which the tubes run vertically.
In operation, the fluid-bed reactor l is fed with carbonaceous material through a lance 7, with fluidizing gas through inlet 8, and with secondary gas through inlet 2. A rela-tively dense fluidized bed is disposed between the secondary gas inlet 2 and the fluidizing gas inlet ~ and has a density of sus-pension which may attain a value as high as the bulk density of the bed material. The mean density of the suspension above the secondary gas inlet 2 is 15 - lO0 kg/m3.
The solids entrained by the exhaust gas from the fluid-bed reactor l are collected from the exhaust ~as in the separator 6 and are recycled throu~h conduit 9 into the ~luid-bed reactor 1. The surplus solids produced are withdrawn through conduit 10.
The fluid-bed reactor shown in Fig. 2 has a conical lower portion. In this case, secondary gas is fed through in-lets 2a, 2b, and 2c, 2d disposed on different levels. The other reference characters are the same as in Fig. 1.
In the embodiment shown in Fig. 3, the arrangement shown in Fig. l is succeeded in the exhaust gas path by a waste-heat boiler 11 and an electrostatic precipitator 12. A fluidized-bed cooler 14 provided with cooling registers 13 serves to cool the solids discharged through conduit lO.
/~

1~5~7584 In the waste-heat boiler 11, which consists of a fluidized-bed cooler, additional sensible heat is extracted from the exhaust gas from the separator 6 of the fluid-bed reactor.
A fine purification of the exhaust gas is effected in the electro-static precipitator 12. Solids which are thus collected are conducted in conduit 15 and combined with the solids discharged through conduit 10. The combined solids are then fed to the fluidized-bed cooler 14, The fluidized-bed cooler 14 comprises four chambers, which are flown through in succession, and is supplied with oxygen-containing fluidizing gas through conduit 16. The gas is collected in the hood and is fed through inlet 2 as secondary gas to the fluid-bed reactor 1. By the cooling registers 13, the solids are indirectly cooled with a gas, which is supplied through conduit 17 and which may contain oxygen, if desired.
Except for a partial stream, the gas leaving the cooling registers 13 is supplied through conduit 8 as fluidizing gas to the fluid-bed reactor 1. The branched-off partial stream is used for pneumatically feeding the carbonaceous material through lance 7.
In Figs. 1-3 the feed line 7 for the carbonaceous material is shown to be provided with a blower 7a through which a carrier air or gas can be introduced and which entrains particles of a desulfurizing agent from a dispenser 7b and particles of a carbonaceous material from a dispenser 7c. A valve 7d permits a portion of the primary fluidizing gas to be used as part of the carrier gas or allows part of the carbonaceous material or the carrier gas to be introduced at the bottom of the fluid-bed.
Example 1 (with reference to E`i~. 1) Coal was burned with air. The fluid-bed reactor 1 used for this purpose had a base area of 1 x 1 m2 and a height of 12 m, The reactor was provided throughout its inside wall with a cooling surface 4 having an area of 60 m2. Besides, the reactor 1~)57584 space contained plane vertical cooling surfaces 3 having an additional cooling surface area of 27 m2 and disposed above the secondary gas inlet 2. The fuel lance 7 was disposed 0.2 m over the grate and the secondary gas inlet 2 was disposed 2.5 m over the grate.
Coal having a calorific value Hu = 7170 kcal/kg (= 30.0 MJ/kg) and a mean average particle diameter of 0.1 mm was pneumatically fed at a rate of 1 metric ton/h by means of air at a rate of 150 standard m3/h. The fluid-bed reactor 1 was fed through the grate with 4000 standard m3/h air at 300 C and through inlet 2 with 4300 standard m3/h air at 300C.
The mean density of the suspension in the reactor space was 300 kg/m3 below the secondary gas inlet 2 and 50 kg/m3 above the inlet. The temperature throughout the circulation system was about 850C.
The combustion residues were collected from the exhaust gas in the separator 6 and were recycled into the fluid-bed reactor 1. A partial stream was discharged at 10 and so controlled that the amount of residues recycled per hour was five times the amount of solids contained in the fluid-bed reactor.
Under the above-mentioned process conditions, coefficients of heat transfer amounting to 120 watts/m2C were obtained. Of the total heat supplied at a rate of 9.2 x 106 watts, heat at a rate of 5.8 x 106 watts was dissipated through the cooling surfaces and used to generate saturated steam at 60 bars. The utilization of the fuel was 99~. The CO content in the exhaust gas was less than 0.1~.
Example 2 (with reference to Fig. 1) Coal was burned with oxygen-enriched air. The fluid-bed reactor 1 described in Example 1 was used for this purpose.
In that reactor the area of the cooling surfaces disposed in the upper reactor space had been increased to 37 m2. Besides, ti ? /b 1057~4 additional cooling surfaces having an area of 15 m2 had been installed in the separator 6 on the walls thereof.
During operation under full load, coal having a calorific value H = 7170 kcal/kg and a mean particle diameter of 0.1 mm was pneumatically fed at a rate of 2.7 metric tons/h by means of 300 standard m3/h oxygen-containing gas, which contained 60% by volume oxygen and was at 300 C. The density of the suspension was about 300 kg/m3 in the reactor space below the secondary gas inlet 2 and about 90 kg/m3 in the reactor space above the secondary gas inlet 2. The temperature throughout the circulation system was about 850 C. The solids collected from the exhaust gas in the separator 6 were recycled to the fluid-bed reactor 1 at such a rate that the amo~lnt of solids recycled per hour was eight times the solids content of the reactor. The remainder was discharged through conduit 10.
The coefficients of heat transfer obtained under these conditions amounted to 290 watts/m2 C. Of the total heat supplied (23.4 x 106), heat corresponding to 18.7 x 106 watts was dissipated through cooling surfaces and used to generate saturated steam at 60 bars.
Owing to a reduc~d power requirement, it was desired to operate the plant at one-third of the steam generation rate.
Whereas the fluid-bed reactor 1 and the installed cooling surfaces

4 and 5 were not changed, the coal-feeding rate was reduced to 0.9 metric ton/h. Coal was fed through lance 7 by means of 100 standard m3/h air. The same fluidizing and secondary gases as described hereinbefore were fed at reduced rates of 400 and 2200 standard m3/h, respectively.
Under the above-mentioned conditions, the concentration of solids was increased to about 530 kg/m3 in the lower reactor space and was decreased to about 30 kg/m3 in the upper reactor - space. The coefficients of heat transfer were decreased to 100 watts / m2 C. I~
,~ - ~6 -10575~
It is apparant that an adaptation to the power require-ment was accomplished by the mere change of the rates at which coal, fluidizing gas and secondary gas were fed. The solids content throughout the fluid-bed reactor and the temperature of 850 (+10) C in the circulation system were not changed.
Only a very short time was required to run up the reactor to a higher power or to full load.
Example 3 (with reference to Fig. 1) Fuel was burned with air under superatmospheric pressure.
For this purpose, the fluid-bed reactor 1 was used which has been described in Example 1 and had been provided with cooling surfaces having a total area of 132 m2 60 m2 of said area were provided on the inside wall of the reactor space, 25 m2 on the walls of the separator 6, and 47 m in the free reactor space disposed over the secondary gas inlet 2. The fluid-bed reactor contained a sufficiently large amount of limestone as bed material.
Fuel oil having a calorific value of 96~0 kcal/kg (= 40.2 MJ/kg) and an S content of 3.2 % by weight was fed at a rate of 1.5 metric tons per hour through lance 7. Limestome which contained about 97% by weight CaC03 and had a mean particle diameter of about 0.1 ~ 0.2 mm was pneumatically fed as a bed material and as sulfur-combining agent at a metered rate of 278 kg/h, corresponding to a molar ratio of 1,8 moles CaO per mole of sulfur in the fuel oil, by means of 50 s-tandard m3/h air.
The fluid-bed reactor was fed through the grate with 10,500 standard m3/h air and through the secondary gas inlet 2 wit;h 7000 stnndard m3/h air. The air in both streams was under a pressure of 5 bars and at a temperature of 300 C. A tempera-ture of 850 C was obtained in the circulation system. The withdrawal of solids through conduit 10 and the recycling of solids through conduit 9 were controlled so that the amount of solids recycled per hour was about eight times the solids content - Jd~ .

lOS75~
of the fluid~bed reactor.
Under these conditions of operation, the mean density of the suspension in the reactor space was 300 kg/m3 below the secondary gas inlet 2 and 60 kg/m3 above the secondary gas inlet 2. The coefficient of heat transfer was about 150 watts/m2 C
Of the total heat supplied at a rate of 18.6 x 106 watts, heat at a rate of 11.4 x 106 watts was dissipated by the cooling sur-faces formed by tubes and was utilized to generate sa-turated steam at 60 bars.
The utilization of the fuel amounted to 99%. The C0 content in the exhaust gas was below 0.1% by volume and the N0 content below 100 ppm. A desulfurization of 90% was effected.
Example 4 ¦with reference to Fi~. 3.) Coal-washing refuse was burned with oxygen-enriched air. For this purpose, the f]uid-bed reactor 1 was used which has been described in Example 1 and which had been provided with cooling surfaces of 60 m2 area on its inside wall, of 58 m2 area in the upper reactor space and of 25 m2 area in the separator 6.
Coal-washing refuse containing 67% by weight ash, a combustible content of 30% by weight, a moisture content of 3 %
by weight, a mean particle size of 0.08 mm, and a calorific value of 2000 kcal/kg (-8.4 MJ/kg) was fed through lance 7 at a rate of 9.1 metric tons/h by means of 1000 standard m3/h conveying gas, which had an oxygen content of 60 % by volume and a temperature of 450 C. The reactor was fed through the grate with 4000 standard m3/h fluidizing gas and -through the secondary gas inlet 2 with 2700 standard m /h secondary gas.
Each of said gas streams had an oxygen content of 60 % by volume and a temperature of 450 C.
The mean density of the suspension amounted to about 250 kg/m3 below the secondary gas inlet 2 and to about 70 kg/m3 above the secondary gas inlet 2.

, ;, ~ --~057S84 Ash was recycled at such a rate that ten times the reactor content was recycled per hour. m e remainder was dis-charged through conduit 10. The temperature throughout the circulation system was at about 850 C.
The hot incombustible residue discharged through conduit 10 was fed to a fluidized-bed cooler 14, which comprised four chambers and interconnected cooling registers 13 immersing into the several chambers. The fluidizing gas at a rate of 2700 standard m3/h had an oxygen content of 60 % by volume and the indirect coolant at a rate of 500 standard m3/h consisted of a gas having the same composition. These gases were heated to 450 C and were supplied to the fluid-bed reactor 1 as secondary gas, as a fluidizing gas and as a feeding gas, respectively.
The incombustible residue was discharged from the fluidized-bed cooler 14 at a temperature of 150 C. Under these conditions, coefficients of heat transfer amounting to 200 watts/m C were obtained. Of the total heat supplied at the rate of 22.6 x 106 watts, heat at a rate of 16.6 x 10 watts was dissipated through the cooling surfaces and used to generate saturated steam at 60 bars.

1'-` -~ -

Claims

The embodiments of the invention in which an exclusive property or privilege is claimed are defined as follows:

1. A process for burning a carbonaceous material to produce steam, which comprises the steps of:
introducing carbonaceous material into a fluid bed in an upright reactor;
fluidizing the carbonaceous material in said fluid bed with a primary fluidizing gas introduced at the bottom of said bed and a secondary gas introduced into said fluid bed at a level above that at which the primary gas is introduced and above the bottom of the fluid bed, at least the secondary gases containing oxygen;
burning the carbonaceous material with the oxygen;
maintaining the supply of carbonaceous material and oxygen to said fluid bed at distinct proportions;
maintaining the volume ratio of fluidizing gas to secondary gas at substantially 1:20 to 2:1;
removing thermal energy from said fluid bed by disposing therein at a level about the location at which said secondary gas is introduced, cooling surfaces in contact with said fluid bed and extending into the interior thereof;
cooling said surfaces with water to produce steam;
controlling the removal of thermal energy by adjusting the mean solids suspension density above the location at which said secondary gas is introduced within the range of 15 to 100 kg/m3 as a result of the adjusted velocity and the volume ratio of said gases;
controlling the fluidization of said material in said bed to preclude the formation of a discrete upper level of said bed and to ensure a solids density gradient decreasing over substantially the entire height of the reactor;

maintaining below the level at which the secondary gas is introduced, a space substantially free of internal obstruction at which said carbonaceous material is introduced;
separating solids from the gas effluent from said bed at the top thereof to collect solid particles;
recycling said solid particles to said fluid bed at a lower portion thereof whereby said fluid bed and the means for separating and recycling said particles constitute a closed solids circuit; and removing excess solids from said circuit, after the separation thereof from the gas effluent from said bed.

2. The process defined in claim 1, wherein said primary fluidizing gas in a partial stream of an oxygen-containing gas, said secondary gas being an oxygen-containing gas.

3. The process defined in claim 1, wherein said carbonaceous material and said oxygen is supplied to said fluid bed at substantially stoichiometric proportions.

4. The process defined in claim 1, wherein said secondary gas is introduced into said fluid bed at a level up to 30% of the total height of the fluid bed reactor and at least one meter above the fluidizing gas inlet.

5. The process defined in claim 1, further comprising the step of dissipating part of the heat of the fluid bed by fluid cooling an interior wall thereof.

6. The process defined in claim 1, further comprising the step of passing a coolant along said surfaces parallel to the direction of flow of the gas-solids suspension through said bed.

7. The process defined in claim 1, further comprising the step of cooling solids withdrawn from said cycle in a fluidized bed cooler in heat-exchanging relationship with one of said gases.

8. The process defined in claim 7, wherein said solids removed from said cycle are cooled by indirect heat exchange with said fluidizing gas in said fluidized-bed cooler.

9. The process defined in claim 7, wherein said solids removed from said cycle are cooled in direct heat exchange with said secondary gas in a fluidized-bed cooler.

10. The process defined in claim 1, further comprising the step of introducing into said fluid-bed during combustion of said carbonaceous material therein, a fine-grain desulfurizing agent.

11. The process defined in claim 1, wherein at least one of said gases in oxygen-enriched air.

12. The process defined in claim 1, wherein said fluid-bed is maintained at a superatmospheric pressure during the combustion of said carbonaceous material therein.

13. The process defined in claim 12, wherein said superatmospheric pressure ranges up to 20 kg/cm2 gauge.

14. The process defined in claim 1, further comprising the step of controlling the combustion of said material in accordance with the power requirements of heated fluid withdrawn from said surfaces by regulating the density of said solids density in the fluid bed above the secondary gas inlet.

15. An apparatus for the combustion of a carbonaceous material comprising:

an upright vertically elongated fluid bed chamber;
means for introducing the carbonaceous material into a lower portion of said chamber;
means for introducing a fluidizing gas into said chamber at the bottom thereof;
means for introducing a secondary gas into said chamber at least one meter above the fluidizing gas inlet means and at a location up to substantially 30% of the total height of said chamber, at least one of said gases containing oxygen sustaining combustion within said chamber;
means for removing a flue gas entraining solid particles from the top of said chamber;
cooling surfaces provided with ducts from a cooling fluid disposed in said chamber and extending into said bed over a region thereof above the secondary gas inlet means, said chamber having a substantially free space below said secondary gas inlet means;
a separator for removing said particles from said flue gas;
conduit means for recycling the particles separated from said flue gas to said chamber;
a fluidized bed cooler;
means for removing recirculated particles from the cycle formed by said chamber, said separator and said conduit means and introducing same into said cooler;
means for fluidizing the particles in said cooler with one of said gases prior to introducing same into said chamber; and means for passing the other of said gases in indirect heat-exchanging relation with the fluidized particles in said cooler prior to introducing said other gas into said chamber.

16. The apparatus defined in claim 15, further comprising means for introducing a desulfurizing agent in finely divided form to said chamber.

17. The apparatus defined in claim 15, wherein said chamber is formed with cooling surfaces along the interior walls thereof, said cooling surfaces having vertically-extending coolant ducts.

18. The apparatus defined in claim 17, further comprising a waste heat boiler traversed by said flue gas downstream of said separator, and an electrostatic precipitator downstream of said waste heat boiler.