Abstract:
The present disclosure relates to a method of operating a boiler system that includes an oxy-fuel boiler in which an oxygen stream and a fuel stream are combusted to generate a flue gas stream. An air separation unit produces the oxygen stream for the oxy-fuel boiler. A gas processing unit cleans and compresses at least a portion of the flue gas stream generated in the oxy-fuel boiler producing a pressurized carbon dioxide stream. The method includes operating the boiler system, at least for a period of time, in a recirculation mode, during which a carbon dioxide stream from a CO 2  compression unit within the gas processing unit is evaporated in the air separation unit and forwarded as a stream to the gas processing unit. The present disclosure further relates to a boiler system for an oxy-fuel process as well as to a power plant comprising such a system. The present disclosure also relates to the use of a carbon dioxide containing stream as a refrigerant.

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
       [0001]    This application claims priority to European application 12190795.0 filed Oct. 31, 2012, the contents of which are hereby incorporated in its entirety. 
       TECHNICAL FIELD 
       [0002]    This disclosure is related to an oxy-fuel boiler system and a way of operating such a system. 
       BACKGROUND 
       [0003]    In the combustion of a fuel, such as coal, oil, peat, waste, etc., in a combustion plant, such as a power plant, a hot process gas is generated, such process gas containing, among other components, carbon dioxide CO 2 . With increasing environmental demands various processes for removing carbon dioxide from the process gas have been developed. One such process is the so called oxy-fuel process. In an oxy-fuel process a fuel, such as one of the fuels mentioned above, is combusted in the presence of a nitrogen-lean gas. Oxygen gas, which is provided by an air separation unit, is supplied to a boiler in which the oxygen gas oxidizes the fuel. In the oxy-fuel combustion process a carbon dioxide rich flue gas is produced, which can be treated using various CO 2  capture technologies in order to reduce the emission of carbon dioxide into the atmosphere. Oxygen may be provided by an oxygen production unit known as an air separation unit (ASU), which extracts oxygen out of the surrounding air. There are various technologies that are used for this separation process, but the most common is via cryogenic distillation. To achieve the low distillation temperatures (the cooling of the gases) in an ASU a large amount of energy is required to make this refrigeration cycle work and may delivered by an air compressor. 
         [0004]    Further, CO 2  capture often comprises cooling, or compression and cooling, of the flue gas to separate CO 2  in liquid or solid form from non-condensable flue gas components, such as N 2  and O 2 . 
         [0005]    After purification and separation of carbon dioxide, a carbon dioxide rich stream is obtained and need to be handled, such as by storing and transportation in tanks (stationary or on a truck or ship), transporting via pipelines and/or pumping into the ground for prolonged (definitive) storage and mineralisation. 
         [0006]    Different components used in an oxy-fuel process may not always be used to their full capacity. Components downstream of the boiler are designed in view of the output from the boiler. Some of the apparatuses used in an oxy-fuel process are thus oversized, or occasionally oversized, since the oxy-fuel process not always is operated at full capacity all the time. One such apparatus may be the compressors in the gas processing unit (GPU) acting on the concentrated carbon dioxide stream. 
         [0007]    There is always a need to improve the flexibility of an oxy-fuel process. It would be desirable to find new ways to lower overall energy consumption, scale down the size/capacity of the components and better utilize the components present in an oxy-fuel process. 
       SUMMARY 
       [0008]    By using heat energy from parts of a process and forward it to other parts where it is needed the overall energy consumption may be lowered. By, during periods of low load, recirculating a carbon dioxide rich stream from the discharge of a CO 2  compression unit to the inlet of the CO 2  compression unit the CO 2  compression unit is continuously running steady. The recirculated carbon dioxide rich stream is passed through an air separation unit where it is acting as a refrigerant by transferring heat energy from streams within the air separation unit to the carbon dioxide rich stream which then is evaporated. Thus, this presents an opportunity to decrease the supply of external heat energy from outside the oxyfuel process, i.e. by using heat energy available in the process the required energy input may be decreased. 
         [0009]    The load dependent heat transfer system results in a decreased overall energy consumption, and decreased operational costs for the process. 
         [0010]    An object of the present invention is to provide a method of operating a boiler system comprising an oxy-fuel boiler in which an oxygen stream and a fuel stream are combusted to generate a flue gas stream, an air separation unit producing the oxygen stream for the oxy-fuel boiler, and a gas processing unit for cleaning and compressing at least a portion of the flue gas stream generated in the oxy-fuel boiler producing a pressurized carbon dioxide stream, the method comprising:
   operating the boiler system, at least for a period of time, in a recirculation mode, during which a carbon dioxide stream from a CO 2  compression unit within the gas processing unit is evaporated in the air separation unit and forwarded as a stream to the gas processing unit.   
 
         [0012]    According to one embodiment the method, in the recirculation mode, the carbon dioxide stream from the CO 2  compression unit is made to expand before entry into the air separation unit. Such an expansion may be made close to the site where it is to be used, i.e. here close to the air separation unit, or at any other suitable place. 
         [0013]    According to one embodiment, the method further comprises:
   establishing whether the boiler system operates at a first load or at a second load, wherein the second load is a lower load than the first load,   controlling the boiler system to operate in the recirculation mode when the boiler system operates at the second load, and controlling the boiler system to stop operation in the recirculation mode when the boiler system operates at the first load.   
 
         [0016]    According to one embodiment, the recirculation mode of the boiler system is controlled using a controlling device and a regulating device. 
         [0017]    According to one embodiment, the regulating device is also responsible for expanding the carbon dioxide stream from the CO 2  compression unit before entry into the air separation unit as the stream. 
         [0018]    According to one embodiment, the carbon dioxide stream from the CO 2  compression unit is a part of the pressurized carbon dioxide stream exiting the gas processing unit or is taken from the CO 2  compression unit before the pressurized carbon dioxide stream is exiting the gas processing unit. 
         [0019]    According to one embodiment, the recirculated carbon dioxide stream from the air separation unit is forwarded to the inlet of the CO 2  compression unit or to a stream containing carbon dioxide entering the CO 2  compression unit. 
         [0020]    An object of the present invention is to provide a boiler system comprising an oxyfuel boiler in which a stream of oxygen and a fuel are combusted to generate a flue gas stream,
   an air separation unit producing the stream of oxygen for the boiler,   a gas processing unit for further cleaning and compression of the flue gas for producing a stream of pressurized fluid comprising carbon dioxide,   a recirculation system, operable at least for a period of time in an recirculation mode, in which a carbon dioxide stream from a CO 2  compression unit within the gas processing unit is evaporated in the air separation unit and forwarded as a stream to the gas processing unit. The boiler system may further include an air quality control system for cleaning at least a portion of flue gas generated in the boiler, and a flue gas condenser for condensing the cleaned flue gas,   
 
         [0024]    According to one embodiment, the boiler system further comprises a controlling device and a regulating device which controls the recirculation system to be operable in the recirculation mode based on a measured load on the boiler system. 
         [0025]    According to one embodiment, the regulating device is also responsible for expanding the carbon dioxide stream to be recirculated from the CO 2  compression unit before entry into the air separation unit. 
         [0026]    According to one embodiment, the carbon dioxide stream from the CO 2  compression unit is a part of the pressurized carbon dioxide stream exiting the gas processing unit or is taken from the CO 2  compression unit before the pressurized carbon dioxide stream is exiting the gas processing unit. 
         [0027]    According to one embodiment, the carbon dioxide stream from the air separation unit is forwarded to the inlet of the CO 2  compression unit or to a stream containing carbon dioxide entering the CO 2  compression unit. 
         [0028]    According to one embodiment, the gas processing unit apart from the CO 2  compression unit further comprises a flue gas compression unit and a carbon dioxide separation unit. 
         [0029]    An object of the present invention is to provide an oxy-fuel combustion power plant comprising the above mentioned system. 
         [0030]    An object of the present invention is to provide a use of a carbon dioxide stream from a CO 2  compression unit within a gas processing unit of a boiler system, said carbon dioxide stream, as a refrigerant in an air separation unit of said boiler system, wherein the carbon dioxide is withdrawing heat energy from the air separation unit, said carbon dioxide being evaporated and a resulting evaporated carbon dioxide stream is forwarded back to the gas processing unit. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0031]    Referring now to the figures, which are exemplary embodiments, and wherein the like elements are numbered alike: 
           [0032]      FIG. 1  is a schematic view of a boiler system  27  in an oxy-fuel process, disclosing one embodiment a recirculation system  26 . 
           [0033]      FIG. 2  is a schematic view of a boiler system  27  in an oxy-fuel process, disclosing one embodiment a recirculation system  26 . 
       
    
    
     DETAILED DESCRIPTION 
       [0034]    The present method establishes the load at which the boiler system operates. By providing limit values on the load for when the recirculation mode is to be active the method is switching between an inactive and active mode based on a load value measured in the process during operation. The load value is the set point of the power plant capacity. By directly or indirectly measuring e.g. the amount of ingoing fuel into the boiler, power consumption of the fuel pump, oxygen demand (e.g. weight or volume flow of oxygen forwarded to the boiler), load on the CO 2  compression unit, electrical power output, demand from the grid, flue gas flow rate, flue gas volumetric flow rate, steam production and/or temperatures of the process, the capacity of the boiler system is established. The recirculation mode is to be active during a low load on the boiler system. The load on the boiler system is considered low when the load is at most or below 75% of maximum capacity of the boiler and/or CO 2  compression unit, preferably 30-75%. 
         [0035]    The load on the boiler system could be measured and controlled using the oxygen demand or flow rate to the boiler. The load on the CO 2  compression unit could be measured and controlled using the operating point of the CO 2  compression unit. The load of big centrifugal compressors is measured typically by flow control. Below a 75% load such machines are operated using recirculation to prevent damages to the equipment from surge conditions. A predetermined set point of a compressor, depending e.g. on the compressor&#39;s manufacturer and model, is generally in the range of 75% to 80% of the compressor&#39;s capacity. For certain compressor types, e.g. screw compressors or reciprocating ones, the range could be extended to 30 to 75%. 
         [0036]    The limit values of the boiler system to operate in the recirculation mode are set as a first and a second load. The limit value for a first load may be set to at least 75% of maximum capacity of the boiler or CO 2  compression unit, at which the boiler system deactivates the recirculation mode. The limit value for a second load may be set to below 75% of maximum capacity of the boiler or CO 2  compression unit, at which the boiler system activates and operates in the recirculation mode. 
         [0037]    The mode of operation of the boiler system is controlled by a controlling device, such as a computer, microprocessor or controller, which compares the value of a measured current load with the set limit values and then regulate the process accordingly. 
         [0038]    The carbon dioxide rich streams of the gas processing unit (GPU) are controlled, e.g. in terms of temperature and/or flow. The liquid, gaseous and supercritical carbon dioxide streams in the boiler system are forwarded by controlling the flow of carbon dioxide in a per se known manner. 
         [0039]    By the term “carbon dioxide rich” used throughout the application text is meant that the gas stream referred to contains at least 40% by volume of carbon dioxide (CO 2 ). 
         [0040]    The CO 2  compression unit comprises at least one compressor having at least one, and typically two to ten compression stages for compressing the carbon dioxide gas from a preceding CO 2  separation unit. Each compression stage could be arranged as a separate unit. As an alternative, several compression stages could be operated by a common drive shaft. The CO 2  compression unit may be run under subcritical conditions or supercritical conditions. Further, the CO 2  compression unit may also comprise intercoolers and aftercoolers. Also, separators may be included to separate liquid phase from gaseous phase. The carbon dioxide rich stream to be recirculated may be taken from the CO 2  compression unit upon exit from the CO 2  compression unit or streams within the CO 2  compression unit. If the carbon dioxide rich stream to be recirculated is taken from within the CO 2  compression unit it may be taken after the compressors included in the CO 2  compression unit and after an at least one cooling unit before forwarding the carbon dioxide stream out of the CO 2  compression unit, or after the compressors included in the CO 2  compression unit and before an at least one carbon dioxide pump, forwarding the carbon dioxide stream out of the CO 2  compression unit. 
         [0041]    Carbon dioxide at or above the critical point (31.1° C. and 7.39 MPa) for carbon dioxide, may adopt properties midway between a gas and a liquid, a supercritical fluid, expanding like a gas but with a density of a liquid. The stream exiting the CO 2  compression unit is a CO 2  product, liquid or supercritical fluid form to be stored, temporarily or permanently, and/or used in other processes. 
         [0042]    The recirculation and heat transfer process and the system involved will now be disclosed more in detail with reference to  FIGS. 1-2 . It is to be noted that not all streams or controlling means needed to operate an oxy-fuel process are disclosed in the figures. The  FIGS. 1-2  are focusing on the main flow of the CO 2  stream, which is purified, cooled, separated and then compressed but mainly on the CO 2  rich stream around the CO 2  compression unit, which flow is dependent of fluctuations in process load, in order to make the oxy-fuel process more flexible in terms of energy resource allocation and capacity. 
         [0043]      FIG. 1  is a schematic representation of a boiler system  27 , as seen from the side thereof. The boiler system  27  comprises, as main components, a boiler  7 , being in this embodiment an oxy-fuel boiler, and an air quality control system (AQCS)  9 . The air quality control system  9  comprises a particulate removal device, which may, for example, be a fabric filter or an electrostatic precipitator, and a sulphur dioxide removal system, which may be a wet scrubber. 
         [0044]    A fuel, such as coal, oil, or peat, is contained in a fuel storage  1 , and can be supplied to the boiler  7  via a supply stream  2 . An air separation unit (ASU)  4  is operative for providing oxygen gas in a manner which is known per se. A stream  3  of air is separated within the air separation unit  4  into an oxygen containing gas stream  6  and a stream  5  comprising nitrogen. The oxygen containing gas stream  6  from the air separation unit  4  is continuously, during operation of the boiler  7 , fed into the boiler. The produced oxygen gas to be feed to the boiler  7 , comprises typically 90-99.9 vol.% oxygen, O 2 . A re-circulation of flue gas (not shown), which contains carbon dioxide, to the boiler  7  is provided in the boiler system  27 . The re-circulation of flue gas may be taken from a flue gas stream  8  from the boiler  7 , a flue gas stream  10  from the AQCS  9  or a flue gas stream  12  from the flue gas condenser  11 . The re-circulation of flue gas and the oxygen gas may become mixed with each other to form a gas mixture containing typically about 20-30% by volume of oxygen gas, the balance being mainly carbon dioxide and water vapour, upstream of the boiler  7 . The boiler  7  is operative for combusting the fuel, which is supplied via the supply stream  2 , in the presence of the oxygen gas. The flow of oxygen stream  6  may be controlled by a controlling system which may e.g. comprise computer, micro processor, controller, valves, actuators and/or pumps, which system is not shown in the figures for the purpose of maintaining clarity of the illustration. Controlling the flow of oxygen is done in a per se known manner. 
         [0045]    A stream  8  is operative for forwarding carbon dioxide rich flue gas generated in the boiler  7  to the air quality control system  9 . By “carbon dioxide rich flue gas” is meant that the flue gas leaving the boiler  7  via the stream  8  will contain at least 40% by volume of carbon dioxide, CO 2 . Often more than 50% by volume of the flue gas leaving the boiler  7  will be carbon dioxide. Typically, the flue gas leaving boiler  7  will contain 50-80% by volume of carbon dioxide. The balance of the “carbon dioxide rich flue gas” will be about 15-40% by volume of water vapour (H 2 O), 2-7% by volume of oxygen (O 2 ), since a slight oxygen excess is often preferred in the boiler  7 , and totally about 0-10% by volume of other gases, including mainly nitrogen (N 2 ) and argon (Ar), since some leakage of air can seldom be completely avoided. 
         [0046]    The carbon dioxide rich flue gas generated in the boiler  7  may typically comprise contaminants in the form of, for example, dust particles, hydrochloric acid, HCl, sulphur oxides, SO X , and heavy metals, including mercury, Hg, that should be removed, at least partly, from the carbon dioxide rich flue gas prior to disposing of the carbon dioxide. 
         [0047]    The air quality control system  9  removes in different steps most of the dust particles from the carbon dioxide rich flue gas and also sulphur dioxide, SO 2 , and other acid gases from the carbon dioxide rich flue gas. 
         [0048]    An at least partly cleaned carbon dioxide rich flue gas is forwarded from air quality control system  9  via a stream  10  to a flue gas condenser  11 . From the flue gas condenser  11  via a stream  12  the flue gas is forwarded to a gas processing unit (GPU)  25  in the form of a gas compression and purification unit of the boiler system  27 . In the GPU  25  the cleaned carbon dioxide rich flue gas is further cleaned and is compressed for disposal or further use. 
         [0049]    The cleaned carbon dioxide rich flue gas enters the GPU  25  via the stream  12  and is introduced into the flue gas compression unit  13 , optionally comprising intercooling and separation steps. 
         [0050]    A stream  12  forwards the compressed gas from the flue gas compression unit  13  to a CO 2  separation unit  15  in which a carbon dioxide rich stream  14  is formed, e.g. nitrogen and oxygen are separated from carbon dioxide. 
         [0051]    The CO 2  separation unit  15  may further include a trace substance removal unit (not shown), which removes any trace components still present in the stream, e.g. by adsorption or absorption to remove mercury and other substances. 
         [0052]    The CO 2  separation unit  15  may include a drier unit (not shown), e.g. at least one adsorption drier, operative for removing at least a portion of the content of water vapour of the flue gas. An adsorption drier contains an adsorbent or desiccant capable of adsorbing water molecules from a gas stream. The desiccant may, for example, be silica gel, calcium sulfate, calcium chloride, montmorillonite clay, molecular sieves, or another material that is, as such, known for its use as a desiccant. The molecular sieves have a pore size suitable for adsorption of water, e.g. molecular sieves having a pore size in the range of 3 to 5Å. 
         [0053]    The CO 2  separation unit  15  of the GPU  25  may optionally comprise a flue gas economizer (not shown) arranged between a trace substance removal unit and a drier unit and configured to recover heat from the flue gas stream leaving the trace substance removal unit using, e.g. boiler feed water. The CO 2  separation unit  15  may include a CO 2  condenser unit (not shown), in which the gas is cooled in a heat-exchanger, often called a cold-box, to cause liquefaction of the carbon dioxide such that the carbon dioxide can be separated from gases, such as nitrogen, that are not liquefied at the same temperature as carbon dioxide. 
         [0054]    Furthermore, the GPU  25  comprises a high pressure CO 2  compression unit  17  arranged downstream of the CO 2  separation unit  15 , and comprising one or more compression stages for compressing the carbon dioxide to a suitable pressure for a following sequestration. After compression of the gas in the CO 2  compression unit  17 , the compressed carbon dioxide, which may be in a supercritical or subcritical fluid state, may be forwarded, via stream  18  for further use. The CO 2  compression unit  17  comprises at least one compressor having at least one, and typically two to ten compression stages for compressing carbon dioxide to liquid or supercritical fluid. Each compression stage could be arranged as a separate unit. As an alternative, several compression stages could be operated by a common drive shaft. The CO 2  compression unit  17  may be run under subcritical conditions or supercritical conditions. 
         [0055]    Compressed carbon dioxide hence leaves the GPU  25  via a stream  18 . Compressed carbon dioxide leaving the GPU  25  may be transported away for disposal, which is sometimes referred to as “CO 2  sequestration”. 
         [0056]    A recirculation system  26  operates at a specific mode. The recirculation system  26  is active during low load on the boiler system  27 . During high load on the boiler system  27  the recirculation system  26  is inactive. The recirculation system  26  is used to prevent damages to the equipment of the CO 2  compression unit  17  from surge conditions and transfer heat energy from the ASU  4  to aid the cooling process performed in the ASU  4 . The stream  18 , comprising pressurized carbon dioxide, leaving the GPU  25  may be divided to partly be used in the recirculation system  26 . The stream  18  may be divided into a carbon dioxide stream  19  for further use or disposal and a carbon dioxide stream  20  to be used within the recirculation system  26 . The split of stream  18  is dependent upon how much carbon dioxide is needed for recirculation to keep the CO 2  compression unit running smoothly. A regulating device  21 , e.g. a valve, is used to control the flow of the recirculation system  26  using a controlling device  22 . The controlling device  22  may be a computer, microprocessor or controller, which compares the value of a measured current load with the set limit values and then regulate the process accordingly. The stream  20  comprises carbon dioxide in liquid or supercritical fluid form. Optionally the regulating device  21  may also be used to expand the carbon dioxide in liquid or supercritical fluid form. Following the regulating device  21  a stream  23  comprising carbon dioxide in liquid form or two part form, i.e. both liquid and gaseous form, is forwarded to the ASU  4 . Within the ASU  4  the stream  23  is evaporated by heat transfer. Streams related to the separation of air within the ASU  4  are heat exchanged with ingoing carbon dioxide containing stream  23 . Stream  23  is acting as a refrigerant within the ASU  4 . An evaporated carbon dioxide containing stream  24  is exiting the ASU  4 , and may be forwarded back to the GPU  25 , e.g. inlet of the CO 2  compression unit  17  or ingoing stream  16  to the CO 2  compression unit  17 . The evaporated carbon dioxide containing stream  24  exiting the ASU  4  may also be forwarded back to the inlet of the flue gas condenser  11  or inlet of the flue gas compression unit  13 , either directly or via a stream entering one of said units. Because the flue gas compression unit  13  and the flue gas condenser  11  also have turn down ratios the recirculation may have a positive impact on the system. If the CO 2  is recycled before the flue gas compressor it has the advantage this increases the molecular weight which makes the compression a little bit more energy efficient. The heat energy transferred in air separation unit  4  results in a decreased temperature therein, i.e. a decreased temperature of streams included within the ASU  4 . The evaporated carbon dioxide rich stream  24  may be forwarded using a pumping device (not shown) in a manner known per se. 
         [0057]    The load on the boiler system  27  is not always constant. Thus, during periods of low load, e.g. during night time, the boiler system  27  is not performing at its full potential. The CO 2  compression unit  17  may be designed to be able to handle a full load on the boiler system  27 . The operating range of a compressor is limited on the high flow side by the choke region and on the low flow side by the surge region. To avoid surge a flow from the discharge side is recirculated to the suction side of the compressor. 
         [0058]    During periods of low load on the CO 2  compression unit, e.g. below 75%, the CO 2  compression unit work partly on recirculation. The recirculated CO 2  from the CO 2  compression unit  17  is used as refrigerant to cool the process in the ASU  4  by transferring heat energy from air separation streams (not shown) within the ASU  4  to the recirculated CO 2 . Another way of looking at this is by the recirculation of CO 2  flow a surplus of cold energy is extracted out of the stream  23  by evaporation of the carbon dioxide. The surplus of cold energy may then be used in the ASU  4  to cool the air separation process therein. 
         [0059]    The difference in load on the boiler system  27  triggers the use of the recirculation system  26 . As an example a measuring unit (not shown) could be connected to the boiler  7  or the CO 2  compression unit  17 , measuring the load on the boiler  7  or the CO 2  compression unit  17 , respectively. When the load on the boiler  7  or CO 2  compression unit  17  reaches a specified value the recirculation system  26  changes modes from active to passive, or the other way around. When the load is high, e.g. at least a load of above 75% on the boiler  7  or CO 2  compression unit  17 , the recirculation system  26  is passive. When the load is lower, e.g. below a load of 75% on the boiler  7  or CO 2  compression unit  26 , the recirculation system  26  is activated to facilitate heat exchange with air separation unit  4 . 
         [0060]      FIG. 2  is a schematic representation of a boiler system  27 , as seen from the side thereof. The boiler system  27  comprises the same features as in previously mentioned  FIG. 1  apart from the construction at the beginning of the recirculation system  26 . 
         [0061]    The CO 2  compression unit  17  comprises at least one compressor having at least one, and typically two to ten compression stages for compressing the carbon dioxide gas from a preceding CO 2  separation unit  15 . Further, the CO 2  compression unit  17  may also comprise intercoolers and aftercoolers (not shown). Also, separators (not shown) may be included to separate liquid phase from gaseous phase. The carbon dioxide rich stream  20  to be recirculated may be taken from streams within the CO 2  compression unit  17 . The carbon dioxide stream  20  to be used for recirculation may be forwarded from the CO 2  compression unit  17  after the compressor(s) i.e. all compression stages, included in the CO 2  compression unit  17  and after an at least one cooling unit (not shown) before forwarding the carbon dioxide out of the CO 2  compression unit  17 , or after the compressor(s) included in the CO 2  compression unit  17  and before an at least one carbon dioxide pump (not shown). 
         [0062]    The herein disclosed incorporation of a recirculation system  26  on the recirculation of the CO 2  compression unit  17  results in a decreased overall energy consumption. The use of the surplus of cold energy for the separation of air in the air separation unit  4  may also influence the design of the air separation unit  4 , since it may be modified. Thus, by using heat energy from another part of the oxy-fuel process the overall energy consumption is decreased. Also by adapting the boiler system process to different load cycles the process may be optimized in view of energy consumption. 
         [0063]    It will be appreciated that numerous variants of the embodiments described above are possible within the scope of the appended claims. 
         [0064]    While the invention has been described with reference to a number of preferred embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted for elements thereof without departing from the scope of the invention. In addition, many modifications may be made to adapt a particular situation or material to the teachings of the invention without departing from the essential scope thereof. Therefore, it is intended that the invention not be limited to the particular embodiments disclosed as the best mode contemplated for carrying out this invention, but that the invention will include all embodiments falling within the scope of the appended claims. Moreover, the use of the terms first, second, etc. do not denote any order or importance, but rather the terms first, second, etc. are used to distinguish one element from another.