|Publication number||US3519254 A|
|Publication date||Jul 7, 1970|
|Filing date||Nov 5, 1968|
|Priority date||Nov 5, 1968|
|Also published as||DE1955186A1|
|Publication number||US 3519254 A, US 3519254A, US-A-3519254, US3519254 A, US3519254A|
|Inventors||Putman Richard E|
|Original Assignee||Westinghouse Electric Corp|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (4), Referenced by (18), Classifications (11)|
|External Links: USPTO, USPTO Assignment, Espacenet|
July 7, 1970 R. E. PUTMAN 3,519,254
METHOD AND APPARATUS FOR THE CONTROL OF BURNER HEAT DISTRIBUTION Filed NOV. 5. 1968 2 Sheets-Sheet 2 FIG.2.
CONTROL COMPUTER RNER ANALOG TO DIGITAL CONVERTER SIGNAL MULTIPLEX UNIT MOTOR TEMPERATURE SENSOR United States Patent 3,519,254 METHOD AND APPARATUS FOR THE CONTROL OF BURNER HEAT DISTRIBUTION Richard E. Putman, Penn Hills, Pa., assignor to Westinghouse Electric Corporation, Pittsburgh, Pa., a corporation of Pennsylvania Filed Nov. 5, 1968, Ser. No. 773,488 Int. Cl. F27b 1/26 US. Cl. 263- 9 Claims ABSTRACT OF THE DISCLOSURE There is disclosed a method and apparatus for the control of the length of the flame from a fuel burner device, for better distribution of the heat from the flame within a furnace or kiln, by including inert gas such as furnace flue gas along with the air supplied to the burner and controlling the proportion of the inert gas, to vary the total oxygen in the resulting gas flow to the burner relative to the desired supply of fuel to the burner and the desired operation of the furnace or kiln.
BACKGROUND OF THE INVENTION In the control of reverberatory furnaces and cement kilns, the point of application of the heat input is of significance. In the case of reverberatory furnaces it assures that the concentrate in the different zones is properly smelted, while in the case of cement kilns it assures that the correct position of the burning zone along the length of the kiln is maintained while at the same time giving the calcining and heating zones the necessary amounts of heat.
In boilers and cement kilns there is a problem as to how the heat from the flame is being distributed within the furnace and the kiln. For the operation of a straight burner with fuel and primary and secondary air, which, in accordance with the teachings of the prior art, has come direct from the atmosphere via a heat exchanger, there is little opportunity for control except by regulating the primary and secondary air distribution but this provides a limited amount of control.
SUMMARY OF THE INVENTION The present invention relates to the regulation of burner flame length by the dilution of air supplied to the burner with inert gas. In particular reference to a pulverized coal burner, the coal entering the pulverizing mill is separated from the gas purging the mill in a cyclone which is also used as a storage hopper for the pulverized coal. The gas used to purge the mill is substantially inert gas drawn from the exhaust of the furnace or kiln, and the gas separated from the cyclone is taken back and added to the primary gas fan inlet. In this way the amount of substantially inert gas circulating through the primary gas fan, mill and cyclone system is a function of the requirements of the mill, with the mill output being regulated from the level of the fuel stored in the cyclone. The pulverized coal is fed to the burner by means of a speed controlled rotary valve which deposits the pulverized coal in the primary air duct gas stream leading to the burner.
Warm secondary air is conveyed by a fan to the burner registers with a branch leading to the primary air duct of the burner. Inert gas passes from the discharge of the primary gas fan to the burner primary air duct.
It is an object of the present invention to provide a better control of the flame length and heating pattern for better heat distribution in relation to a fuel burner operating with a kiln or boiler or the like and particuice larly more beneficial when applied to a pulverized coal burner device.
It is another object to provide an improved flame length control for a burner device, which recognizes that the amount of oxygen in the primary air supply is a significant parameter and determines flame length for a given primary air/fuel flow ratio.
BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 illustrates the burner flame length control of the present invention; and
FIG. 2 illustrates one way to sense and provide the desired temperature profile in a cement kiln or the like.
DESCRIPTION OF A PREFERRED EMBODIMENT In the present method and apparatus for the control of the flame length and heat distribution from a burner device, the resulting temperature in the kiln, or pressure in the boiler, associated with that burner is sensed and used as an operating condition for the regulating of the supply of fuel to the burner. This same control signal is used to determine the gas mixture flow of both air and inert gas to the burner in the primary air duct leading to the burner. There is a desired fixed ratio between the primary air duct gas velocity and the supply of fuel, since the velocity must be high enough to insure that the fuel remains in suspension and is properly transported to the burner. There is also an optimum ratio of total air flow to total fuel supplied for the most eflicient combustion of the fuel. A damper in the branch from the discharge of the secondary air fan to the primary air duct is regulated in accordance with desired flame length. Since the total air flow is controlled by a damper in the secondary air duct to the burner registers, this damper in the branch pipe determines the distribution of air between the primary and secondary ducts while the total air is the proper amount required for eflicient combustion of the fuel. By regulating the gas flow into the primary duct so as to maintain the total primary duct flow at the desired value for transport purposes, the total amount of gas required to convey the fuel to the burner can be considered as consisting of the air coming through the branch pipe plus the amount of primary gas required to make up the difference.
The principle of the present invention is applicable for the regulation of flame length with fuel burners. In addition to being able to regulate flame length, a further advantage of the present invention is the better utilization and distribution of heat within the furnace. The use of the bin and feeder system also allows closer control of the air fuel ratio to be carried out.
The amount of air provided in the primary duct lead ing to the burner is an important parameter for the desired control of flame length. The oxygen content of the primary duct air and gas mixture can be determined 'by the controlled dilution of this mixture by readily available low oxygen and substantially inert waste gasv This provides the additional safety benefit that the pulverized coal mill is operated with this same waste gas.
The amount of fuel supplied to the burner requires a predeterminable velocity of primary duct transport gas mixture, and the use of a mixture including relatively inert waste gas with air permits a desired control of the oxygen content while still providing the desired velocity of this primary duct gas.
In FIG. 1 there is shown a kiln 10 including a burner 12 which is supplied pulverized coal from a storage cyclone 14 through a rotary valve 16, the position of which is controlled by a valve control 18 to determine the amount of fuel supplied through the valve 16 to the burner 12 in accordance wtih the fuel demand control signal from a control computer 20 to maintain a desired burning zone temperature as sensed by a temperature sensor 64 operative with the computer 20. The burner 12 is suppled a controlled gas mixture through the primary duct 86 from a primary gas fan 22 and a secondary air fan 24. The secondary air fan 24 receives heated input air through a heat exchanger 26. The primary gas fan 22 receives substantially inert gas back from the cyclone separator 14 through a conduit 28 and exhaust flue gas from the kiln through a conduit 32 after passing through the heat exchanger 26. The output gas from the primary gas fan 22 passes through a damper 42 operative with a mill transport gas flow control 22 as determined by a signal from the control computer 20 in relation to the controlled operation of the pulverized coal mill 46, which gas passes to the pulverized coal mill 46 where the input coal is pulverized and carried through a conduit 48 to the cyclone separator 14. The cyclone separator 14 functions as a separator device to separate the mill transport gas from the pulverized coal, which mill transport gas is supplied back through the conduit 28 to the input of the primary gas fan 22. The cyclone separator 14 further functions as a storage device for the pulverized coal fuel, the level of which is sensed by a level control 50 and compared with 9. reference signal from the computer 20 for determining the operation of the pulverized coal mill 46. The level control 50 receives the set point or reference signal from the control computer 20 to set and control the desired reference level of the pulverized coal within the cyclone separator 14.
The secondary air fan 24 receives inlet air through the heat exchanger 26 and passes it through a first flow control damper 60 leading to the primary air duct, with the damper 60 operation determined by a flow control 62 in accordance with a temperature profile or heat distribution control signal from the computer 20. The temperature profile or heat distribution is sensed by a temperature sensor 150 operative to sense the temperature profile or heat distribution within the kiln 10. The secondary air also passes through a second damper 68 operative with a flow control 70 in accordance With the sensed flow of total secondary air as determined by the flow sensor 74. In addition a ratio relay 76 is operative with the flow control 70 in accordance with the total fuel supply to the burner 12.
The primary gas flow to the burner is controlled by a damper 80 operative with a flow control 82 in accordance with a signal from a flow sensor 84 operative with the primary duct 86. A ratio relay 88 also provides a control signal to the flow control 82 for determining the flow of primary gas flowing through the conduit 86 in relation to the actual amount of fuel and as desired for transport purposes to carry the fuel to the burner 12.
In FIG. 2 there is shown an illustrative rotary kiln 100. A kiln of this type is typically used for the manufacture of cement. In the kiln there are four discrete zones consisting of drying, calcining, burning and cooling. The actual values of the temperatures and distribution of the temperatures throughout the process have an important effect on the nature and degree of the reactions taking place in the corresponding zones. In the operation of the kiln the processed material flows through the kiln toward the burner or front end, while the air and gases pass through the kiln from the burner towards the feed or back end of the kiln. Even if the material feed flow and gas flow rates are held substantially constant, the temperature distribution and heat exchange between the gases and raw materials can vary to distrube the eflectiveness of the cement making process. The two primary kiln operation control parameters are the temperature of the clinker in the burning zone and the speed of the kiln which controls material retention time and the material profile within the kiln. Burning zone temperature is controlled by varying the fuel combustion rate as related to the amount of fuel supplied to the burner 12. Since the maximum combustion efiiciency coincides with a predeterminable maximum oxygen in the flow gases, the ratio of total air to the fuel fired by the burner is to this extent fixed. Thus air mixture volumes and temperature vary with firing rate and can change the heat transfer characteristics along the whole length of the kiln. In FIG. 2, the rotary kiln includes a motor 102 operative to provide a computer controlled rotation of the kiln 100 through a drive gear 104 and a ring gear 106 fastened to the kiln. A plurality of electrical temperature signal collector rings 108, 110, 112, 114, 116, 118, and 122 are provided with suitable transducers for indicating heat flow or temperature condition measurements from the interior of the kiln through the kiln wall to the outside atmosphere at the respective locations of the provided collector rings for the purpose of indicating the temperature at the respective zones of the interior of the kiln. These temperature signals received from the latter collector rings are applied sequentially through a signal multiplex unit 124 and an analog-to-digital converter 126 to the control computer 20. The signal multiplex unit 124 is sequence controlled in its operation by suitable control signals from the control computer 20, as is the operation of the motor 102 controlled in relation to desired material flow and treatment by the control computer 20. A temperature sensor 123 is operative to sense the temperature of the exhaust gases leaving the kiln 100. The respective collector rings can be opeartive with thermocouples or suitable temperature sensing devices extending through the walls of the kiln to sense the respective zone interior temperatures at the location of the collector rings if desired. In this way a profile of the selected temperatures relative to the desired operation of the kiln is obtained.
In reference to the illustration of FIG. 1, and in the particular illustrated example of a pulverized coal fired burner 12 operative with a kiln 10, the pulverized coal requires a certain air and gas mixture Volume because the gas mixture operates as a transport medium as well as a combustion control medium for the operation of the burner 12. Therefore, a certain amount of gas mixture flow is required in relation to a certain amount of fuel, but the gas mixture supplied to the burner 12 does not have to be all air. It is feasible that by combining in the primary gas fan 22 a regulated amount of inert gas from the flue exhaust of the kiln 10 and the overflow of the cyclone separator 14, the output of the primary gas fan 22 would be a substantially inert gas having a high nitrogen and carbon dioxide content, and the gas volume can be maintained as required to act as a transport medium for the pulverized coal, with the oxygen content of the gas mixture as supplied to the burner 12 being subjected to regulation by controlling this mixture for the purpose of controlling the length of the flame from the burner 12. Thusly, two functions are provided by the gas mixture flow through the primary duct 86, one being the trans port of the pulverized coal fuel and the other controlling the oxygen content for operation of the burner 12, with the latter being subjected to regulation by the addition of substantially inert gas or flue gas through the damper 80 and having a low oxygen content. Thusly, the primary duct gas mixture and the secondary duct air drawn from heat exchanger are passed through to the burner 12, with the primary duct gas mixture being the pulverized fuel transport gas as correlated with the operation of the rotary valve 16 and passing through the primary duct or conduit 86 leading to the burner 12. The primary duct gas mixture is made up of inert gas from the flue of the boiler 10, which is supplied by the primary gas fan 22.
This inert gas also passes through the damper 42 and to the pulverized coal mill 46 for the purpose of moving the pulverized coal into the cyclone hopper '14. It should be noted that inert gas has an advantage here since there is less danger in the operation of the pulverized coal mill 46 with inert gas passing through it of the coal spontaneously igniting. The mill 46 is essentially a ball mill, and coal is fed into the mill and ground up and carried out by the inert gas flow. The coal from the mill 46 is deposited in the cyclone separator 14 and is metered through operation of the rotary valve 16 into the prlmary gas duct or conduit 86, as required for the proper operat on of the burner 12 and the kiln 10. The inert gas passing through the damper 80 and into the primary duct 86 permits a desired control of the flame envelope shape to determine for a certain amount of fuel how the resulting heat is to be distributed within the kiln 10. More specifically, if less oxygen is supplied in the gas mixture passing through the primary duct 86 to the burner 12, a longer flame results such that if the amount of inert gas increases, as determined by operation of the damper 80 in the output of the primary gas fan 22, this results in a lengthening of the flame of the burner 12. On the other hand if the amount of inert gas supplied by the primary duct 86 through operation of the damper 80 is decreased, the flame of the burner 12 shortens such that the whole intensity of the combustion provided by the burner 12 and the distribution of heat therefrom is determined by the primary duct oxygen to fuel ratio which can be determined in this manner. In a normal burner configuration, increasing the secondary air flow does not reduce the primary air oxygen and therefore has less influence on the flame characteristic other than varying excess air and turbulence.
By the teachings of the present invention which uses the exhaust flue gas from the kiln as an inert gas to mix in a controlled manner with the primary duct air, the oxygen in the primary duct gas mixture is diluted and thereby controls the length of the flame from the burner 12 since the dilution of the primary duct air is more important for this purpose than is the secondary duct air regarding the length of the flame from the burner 12.
In relation to a cement kiln, the flame length is critical because there are a plurality of heat zones such as the calcining, heating, drying and burning zones, and these each have certain heat requirements in order to achieve their intended functions which they are designed to perform. If the exhaust flue gases leaving the exit or back end of the kiln are not hot enough as sensed by temperature sensing device 123 shown in FIG. 2, but the burning zone temperature is right, this indicates that more heat must be put in and passed back into the kiln to allow the calcining and drying to proceed as desired but the burning zone temperature should not be disturbed. Thusly, a longer flame with a new amount of heat going back into the calcining and drying zones is required while leaving the same amount of heat going into the burning zone. The teachings of the present invention can be utilized for this purpose. It should be noted that if the flame is longer, the heat has more tendency to go past the burning zone and into the calcining zone. It should be understood that a typical flame of the type under consideration here may be in the order of thirty feet in length, leaving a twelve inch jet pipe which comprises the burner 12.
In regard to a boiler, the steam temperature particularly of the superheat portion of the boiler can be controlled by the length of the flame of the burner operative with the boiler. In the case of a boiler, a temperature sensor such as temperature sensor 150 shown in FIG. 1 would provide an indicative signal to the control computer 20 for controlling the length of the flame, which temperature sensor 150 could be operative with a particular location such as the superheat region of the boiler.
In the case of the cement kiln, a combination of burning zone temperatures and other temperatures along the kiln, such as generally shown in FIG. 2, would be sensed by the control computer 20 and utilized to provide a measurement profile of the temperature along the kiln, which profile would be compared with a stored profile entered into the program memory of the control computer 20. Adjustments of the actual profile, relative to the reference or desired profile, could then be made by adjusting the length of the flame to increase or concentrate the heat energy input into the kiln at the desired zone area. Knowing the desired end condition of the cement product to get the proper chemical combination of the oxides, it may be advantageous to know the oxygen content as well as the temperature of the flue gas leaving the kiln which is desired to prevent condensation in the precipitators or to make sure that adequate drying and calcining are taking place. The flame length can be adjusted as desired to provide the desired heat distribution and related operating conditions for the kiln. An oxygen analyzer 30 can be included as shown in FIG. 1 for sensing the oxygen content of the flue gas if desired.
The control computer such as shown in FIG. 1 would be operative in response to burning zone temperature to control the amount of pulverized coal fuel supplied to the burner 12 by suitable speed control of the rotary valve 16. The heat distribution within the kiln is controlled in relation to the control of the damper 60 relative to the primary duct air mixture flow to the burner and the control of the damper relative to the primary gas flow introduced into the primary duct 86 leading to the burner. The control of the damper 68 relative to the secondary duct air flow to the burner is determined in relation to the total fuel supplied to the burner, and considering the proper gas and air mixture flow to the burner 12 in the primary duct 86 in relation to the desired percentage of inert gas in that duct 86. The damper 80 is operative to control the supply of inert gas from the primary gas fan to the burner, which is determinative of the length of the flame of the burner. It should be noted that the control computer 20 is operative to determine the total air flow, from the secondary air fan 24, which would be desirable for the proper combustion of the provided amount of fuel. The damper 80 is controlled to make up any primary duct gas mixture required to provide an adequate trasport air and gas mixture flow through the primary duct 86 for proper physical transport of the pulverized coal fuel supplied by the rotary valve 16, and to control the amount of oxygen supplied through the primary duct 86 to the burner 12 in relation to the total air supplied through both the primary duct and the secondary duct for the proper combustion of the fuel and for the determination of the proper length of flame from the burner 12. The desired ratio of fuel to the total air for the desired operation of a fuel burner is a weld-known relationship to persons familiar with the combustion characteristics of pulverized coal fuel and the operation of fuel burners. The secondary air fan 24 provides the total air going to the burner, with the primary duct air and inert gas mixture flow being controlled in relation to the fuel determined by the operating speed of the rotary valve 16. The transport air and gas mixture needed to physically move the provided fuel is made up of the air passing through damper 60 and the inert gas passing through damper 80. The heat distribution of the flame from the burner 12 is measured by one of more temperature sensors for controlling the primary duct air containing oxygen relationship supplied to the burner. If the computer shuts the primary duct air damper 60, this causes the make-up of inert gas to increase to make the flame longer; if more inert gas is included, the flame goes longer, while less inert gas causes the flame to shorten.
Thusly, it will be seen that the control computer 20 is operative to control the total amount of heat going into the kiln by setting the amoun of fuel going in through control of the rotary valve 16, and the computer determines the required fuel to air ratio to satisfy desired combustion through its operation to set the amount of air being supplied from the secondary air fan 24 to the burner.
7 Further, when adjustments are made in the amount of fuel supplied, the computer coordinates the desired amount of transport gas mixture flowing through the primary duct 86 by controlling the amount of transport gas in relation to the amount of fuel supplied. The computer then controls the length of the flame to satisfy the heat distribution requirements by varying the the amount of air mixed with the inert gas in the primary duct 86 while holding the supply of total air. If desired, there can be included the measurement of the oxygen in the flue gas by operation of the oxygen analyzer 30 and adjusting the damper 60 to a hold a predetermined oxygen to fuel relationship compared to the pulverized coal of about 1 /2 to 2% for a cement kiln and this ratio is adjusted as necessary for corrections. The oxygen analyzer 30 will permit an adjustment of the ratio of total air to total fuel for improved control of the combustion operation. If the residual oyxgen in the flue 'gas is not enough, this indicates the efficiency of burning the fuel can be improved. If too much oxygen is present in the fiue gas, this indicates that heat is being wasted to heat up an excess of air. The damper 60 can be adjusted to optimize the operation of burner 12 in his regard.
While a preferred embodiment of the present invention has been described, it should be understood that various modifications and changes in the arrangement of parts may be made within the scope and spirit of the present invention.
I claim as my invention: 1. The method of controlling the distribution of heat from a fuel burner operative with an air supply and a substantially inert gas supply, including the steps of sensing a first burner operation condition for controlling the amount of fuel supplied to said burner,
controlling the amount of air supplied from said air supply to said burner in accordance with a predetermined air to fuel ratio desired for the operation of said burner,
and sensing a second burner operation condition for ctntrolling the amount of inert gas supplied from said inert gas supply to said burner in according with a predetermined heat distribution desired for the operation of said burner.
2. The method of claim 1, with said first burner operation condition being the burning zone temperature of a kiln operative with said burner and with said second burner operation condition being a predetermined temperature profile of said kiln.
3. The methof of claim 1, with said first burner operation condition being a predetermined pressure of a boiler operative with said burner and with said second burner operation condition being a predetermined temperature of said boiler.
4. The method of claim 1 operative with a burner having a primary gas duct, including maintaining an adequate flow of fuel transport gas in the primary gas duct leading to said burner in accordance with the amount of fuel supplied to said Iburner.
5. In fuel burner operation control apparatus operative with said burner having an air supply and a substantially inert gas supply, the combination of first sensing means responsive to a first operation parameter of said burner for providing a first control signal in accordance with the desired supply of fuel to said burner,
second sensing means responsive to a second operation parameter of said burner for providing a second control signal in accordance with the desired supply of air with said fuel to said burner, and control means operative 'with said supply of substantially inert gas and responsive to at least said first control signal for controlling the supply of substantially inert gas to said burner such that a desired operation of said burner is provided and operative with said supply of air and responsive to at least said second control signal for controlling the supply of air to said burner such that a desired operation of said burner is provided. 6. The control apparatus of claim 5 with said burner having a primary air duct and a secondary air duct,
said control means being responsive to at least said first control signal for controlling the fuel supplied through said primary air duct to said burner, said control means being responsive to at least said second control signal for controlling the air supplied through said primary air duct to said burner, and said control means being responsive to at least said first control signal for controlling the inert gas through said primary air duct to said burner such that a desired transport of said fuel to said burner is thereby effected. 7. The control apparatus of claim 5, with said fuel burner being operable with a kiln,
said first operation parameter being the burning zone temperature of said kiln, said second operation parameter being the temperature profile along at least the back end of the kiln away from the burner. 8. The control apparatus of claim 5, with said fuel burner being operable with a boiler,
said first operation parameter being a predetermined pressure of the boiler, said second operation parameter being a predetermined temperature of the boiler. 9. The method of claim 1, with said fuel burner having a primary air duct and a secondary air duct,
with said control of the amount of fuel supplied to said burner being in relation to the fuel supplied through said primary air duct to said burner, with said control of the amount of air supplied to said burner being such that the air supplied through the 1 primary air duct is controlled to provide a predetermined distribution of the heat from said burner and the air supplied through the secondary air duct makes up the additional air needed for providing a predetermined air to fuel ratio for the operation of the burner,
and with said control of the amount of inert gas being in relation to the inert gas supplied through said primary air duct to said burner being adequate to provide a predetermined transport of the amount of fuel supplied through said primary air duct to said burner.
References Cited UNITED STATES PATENTS 1,945,652. 2/ 1934 Martin.
2,092,657 9/1937 Smith 263-33 3,091,443 5/1963 Herz et al.
3,284,615 11/1966 Yetter.
JOHN J. CAMBY, Primary Examiner US. (:1. X.R. 236-15; 26352
|Cited Patent||Filing date||Publication date||Applicant||Title|
|US1945652 *||Mar 19, 1931||Feb 6, 1934||Martin Claude Worth||Means for controlling operation of cement kilns|
|US2092657 *||Dec 12, 1934||Sep 7, 1937||Gen Electric||Rotary kiln control arrangement|
|US3091443 *||Apr 17, 1961||May 28, 1963||California Portland Cement Co||Kiln automatic control method and apparatus|
|US3284615 *||Sep 24, 1956||Nov 8, 1966||Burroughs Corp||Digital control process and system|
|Citing Patent||Filing date||Publication date||Applicant||Title|
|US3884621 *||May 6, 1974||May 20, 1975||Round Rock Lime Company||Control of vertical heat treating vessels|
|US3969069 *||Apr 10, 1974||Jul 13, 1976||Koppers-Wistra-Ofenbau Gesellschaft Mit Beschrankter Haftung||Burner systems for ovens and methods of operating such systems|
|US4270470 *||Apr 27, 1979||Jun 2, 1981||Barnett William O||Combustion system and method for burning fuel with a variable heating value|
|US4315730 *||Feb 11, 1980||Feb 16, 1982||Telegan Limited||Burner control system|
|US4411204 *||Dec 7, 1981||Oct 25, 1983||Combustion Engineering, Inc.||Method of firing a pulverized fuel-fired steam generator|
|US4487577 *||Oct 27, 1982||Dec 11, 1984||Lecorp, Inc.||Adaptive control for thermal dryer|
|US4952147 *||Oct 1, 1986||Aug 28, 1990||Champion International Corporation||Lime sludge kiln|
|US8137099||Aug 2, 2006||Mar 20, 2012||L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude||Method for calcination of a material with low nochi emissions|
|US8490556 *||Mar 6, 2008||Jul 23, 2013||Ihi Corporation||Method and facility for feeding carbon dioxide to oxyfuel combustion boiler|
|US8550017 *||Mar 6, 2008||Oct 8, 2013||Ihi Corporation||Method and apparatus of controlling exhaust gas in oxyfuel combustion boiler|
|US20080291965 *||May 16, 2008||Nov 27, 2008||Environmental Energy Services, Inc.||Method for measuring ash/slag deposition in a utility boiler|
|US20090130615 *||Aug 2, 2006||May 21, 2009||Erwin Penfornis||Method for Calcination of a Material with Low NOchi Emissions|
|US20100050912 *||Dec 20, 2007||Mar 4, 2010||Khd Humboldt Wedag Gmbh||Method for controlling the operation of a rotary furnace burner|
|US20110048295 *||Mar 6, 2008||Mar 3, 2011||Ihi Corporation||Method and facility for feeding carbon dioxide to oxyfuel combustion boiler|
|US20110107944 *||Mar 6, 2008||May 12, 2011||Ihi Corporation||Method and apparatus of controlling exhaust gas in oxyfuel combustion boiler|
|EP0081114A2 *||Nov 18, 1982||Jun 15, 1983||Combustion Engineering, Inc.||Method of firing a pulverized fuel-fired steam generator|
|EP0081114A3 *||Nov 18, 1982||May 9, 1984||Lummus Crest S.A.R.L.||Method of firing a pulverized fuel-fired steam generator|
|WO2007015029A1 *||Aug 2, 2006||Feb 8, 2007||L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude||Method for calcination of a material with low nox emissions|
|U.S. Classification||432/21, 432/37, 432/48, 236/15.00R, 432/23, 432/26, 236/15.00E, 432/24|