Patent Application
20110000406
The present invention relates to oxycombustion fluidized bed reactors and their operation. The invention particularly relates to an oxycombustion circulating fluidized bed reactor comprising a reactor chamber and a gas distribution arrangement in a bottom section of the reactor chamber for introducing gas into the reactor chamber. The gas distributor arrangement comprises a first gas feeding system for introducing recycled gas originating from the reactor chamber and a second gas feeding system for introducing oxygen-rich gas.
The invention also relates to a method of operating an oxycombustion circulating fluidized bed reactor comprising a reactor chamber and a gas distribution arrangement arranged in the bottom section of the reactor chamber, in which method, gas is introduced into the reactor chamber through the gas distribution arrangement, the gas distributor arrangement comprising a first gas feeding system through which recycled gas originating from the reactor chamber is introduced into the reactor chamber and a second gas feeding system through which oxygen-rich gas is introduced into the reactor chamber.
The development of new regulations and other demands limiting gas emissions, e.g., relating to the so-called greenhouse effect have contributed to the implementation of new technologies to decrease, e.g., carbon dioxide in power stations using fossil carbonaceous fuels.
For example, U.S. Pat. No. 6,505,567 discloses a circulating fluidizing bed steam generator, in which the combustion is supported by recycled carbon dioxide, which is a product gas of the combustion. The combustion is maintained by means of pure oxygen, which is introduced into the circulating fluidized bed steam generator. Introducing pure oxygen may create areas with a very high local temperature, which is not desired, due to, e.g., the stresses on the structural elements close to those areas.
The introduction of oxygen into a circulating fluidized bed reactor is a particularly delicate process. An uneven distribution of oxygen may create local over heated spots, which are also prone to cause problems, such as agglomeration of bed material. This is particularly the case when pure oxygen is in question.
PCT Publication No. WO 2005/119126 discloses a fluidized bed device having a combustion chamber in which the bottom section is provided with first-type and second-type primary gas supply nozzles. First, the first-type nozzles are provided for injecting a first gas mixture at a first level close to the base of the chamber by means of a conventional wind box and nozzles. Second, the second-type nozzles are provided for injecting a second gas mixture enriched in oxygen at a second level above the first level. According to this publication, the second-type nozzles comprise an arrangement for mixing oxygen with a second gaseous component within the nozzle, connected at the lower end thereof to an oxygen supply and to a supply of the second gaseous component. The second gaseous component is mentioned to be either the gas from the wind box or from a separate gas collector.
In this kind of an arrangement, in which the oxygen is mixed in the nozzle with the gas introduced from the wind box, the control of the oxygen ratio in the mixture is always dependent on the pressure prevailing in the wind box, so that independent control is difficult, if not impossible.
In circulating fluidized bed reactors, the fluidization gas velocities vary considerably, since the variation of load also requires respective changes in the gas amounts fed through a grid of the reactor. The operation range of the grid is determined, e.g., by the pressure drop, which should not be excessive during high loads and yet, during low load operation, the pressure drop should be adequate to provide an even distribution of gas flow over the cross-sectional area of the grid. In practice, there is a certain minimum air flow that also must be fed through the grid during the low load operation, which, in some cases, may be the limiting factor of the lowest obtainable load from the reactor.
Particularly, in oxycombustion circulating fluidized bed reactors, there is, in addition to a variation of gas velocities due to load variations, also a question of a proper introduction of oxygen-rich gas into the process maintained in the oxycombustion circulating fluidized bed reactor.
U.S. Pat. No. 4,628,831 discloses a grid for conveying gaseous fluidization fluid to a treatment chamber using a fluidized bed. The grid comprises two separately supplied circuits of channels, a first circuit of channels with orifices widened towards the top, for providing a dense fluidized bed in the chamber, and a second circuit of tubular channels, opening out above the widened orifices, for providing a forced fluidized bed of particles in the chamber, respectively. This kind of a grid of two separate sets of nozzles and pipe networks is very complicated to manufacture.
An object of the invention is to provide an oxycombustion circulating fluidized bed reactor that provides an advanced solution for introducing both recycled gas and oxygen-rich gas into the oxycombustion circulating fluidized bed reactor.
According to a preferred embodiment of the invention, an oxycombustion circulating fluidized bed reactor comprises a reactor chamber and a gas distribution arrangement provided in a bottom section of the reactor chamber for introducing gas into the reactor chamber, which gas distributor arrangement comprises a first gas feeding system and a second gas feeding system for introducing oxygen-rich gas into the reactor chamber. The first gas feeding system comprises a first wind box and the second gas feeding system comprises a second wind box. The first wind box has a common wall with the reactor chamber and the second wind box, arranged under the first wind box, has a common wall with the first wind box.
The gas distribution arrangement is further in connection with a source of oxygen-rich gas. This arrangement allows an efficient and a reliable operation of an oxycombustion circulated fluidized bed reactor having the oxygen content of the gas introduced into the reactor chamber at an elevated level, higher than the oxygen content of air.
Advantageously, the second, lower wind box has its inner walls lined with material withstanding the conditions that result from the elevated oxygen content in the gas therein.
The second wind box is in connection with the reactor via a plurality of conduits extending from the second wind box through the first wind box into the reactor chamber. This provides the feature of the gas in the second wind box possibly being maintained at a lower temperature than that of the gas in the first wind box. Preferably, the conduits are removably arranged in the first wind box.
The reactor chamber is provided with a particle separator for separating fluidized particles that are entrained with the gases resulting from the reactions taking place in the reaction chamber, and the particle separator is provided with a gas outlet and an outlet for separated particles. The gas outlet is arranged in flow communication with the first wind box and the second wind box via a recycling conduit.
The recycling conduit is advantageously in connection with a first mixing element in the first gas feeding system through a conduit provided with a first flow control device and with a second mixing element in the second gas feeding system through a conduit provided with a second flow control device. In this manner, the flow rate of recycled gas into both of the first and second gas feeding systems may be independently controlled.
The source of oxygen-rich gas is in connection with the first mixing element through a conduit provided with a third control device and with a second mixing element through a conduit provided with a fourth control device. In this manner, the flow rate of oxygen-rich gas into both of the first and second gas feeding systems may be independently controlled, and the method according to the invention may be practiced.
According to the invention, in a method of operating an oxycombustion circulating fluidized bed reactor, which comprises a reactor chamber and a gas distribution arrangement provided in a bottom section of the reactor chamber, gas is introduced into the reactor chamber through the gas distribution arrangement, the gas distributor arrangement comprising a first gas feeding system and a second gas feeding system through which gas is introduced into the reactor chamber. Gas in is introduced into the reactor chamber through a first wind box of the first gas feeding system, and through a second wind box of the second gas feeding system in a manner such that the oxygen-rich gas introduced through the second wind box is introduced through a plurality of conduits extending through the first wind box into the reactor chamber.
According to a preferred embodiment of the invention, the gas introduced into the reactor chamber contains recycled gas, which recycled gas is divided into streams comprising a stream that is controllably introduced into the first gas feeding system and a stream that is controllably introduced into the second gas feeding system. Oxygen-rich gas is introduced into the stream of recycled gas in the first gas feeding system, so that the oxygen content of the gas in the first gas feeding system is less than or equal to a first oxygen content, and that oxygen-rich gas is introduced into the stream of recycled gas in the second gas feeding system so that the oxygen content of the gas in the second gas feeding system is equal to or more than the first oxygen content.
Preferably, the first oxygen content is adjusted such that a risk of self ignition, that is, ignition without external ignition, of any combustible material present in the gas distributor arrangement, is minimized.
The oxygen content is controlled according to an embodiment of the invention by maintaining the O2 concentration of the CO2—H2O—O2 gas mixture so low (typically, less than twenty-eight percent by volume), so that the adiabatic combustion temperature of the combustible material is equal to or less than that of combustion air.
The oxygen-rich gas in the second gas feeding system is fed to the second wind box and is subjected to heat flow from the reactor chamber, which heat flow is decreased by warming up the gas in the first wind box. This way, the oxygen-rich gas in the second wind box may be maintained easily at a lower temperature than that of the gas in the first wind box. Preferably, the oxygen-rich gas in the second wind box is introduced via a plurality of pipes extending through the first wind box into the reactor chamber, being simultaneously heated by the gas in the first wind box.
In the following, the invention will be described with reference to the accompanying schematic drawing, in which
Exhaust gas, which in normal operation of combustion contains mostly CO2 and H2O, is led further to an exhaust gas conduit 45 via the gas outlet 35. The exhaust gas conduit 45 is shown here with a dotted line illustrating the fact that the exhaust gas is subjected to certain treatment processes, such as a heat recovery process, provided in connection with the exhaust gas conduit 45, but not shown here for clarity reasons.
The bottom section of the reactor chamber 15 is provided with a gas distribution arrangement 50, which comprises a grid 55, through which fluidization gas and oxygen containing gas are introduced into the reactor chamber 15. Regardless of the contents of the gas, all the gas introduced through the grid 55 participates in the fluidization of the bed material. The reactor chamber 15 is bordered by the grid 55 at its lower end. The grid 55 is provided with two sets of openings 60, 65, which are in connection with a first gas feeding system 70 and a second gas feeding system 75, respectively, for introducing as into the reactor chamber 15 in a manner to be described in the following. The openings are provided in practice with special nozzles, which are not shown here for clarity reasons. The nozzles are distributed substantially evenly over the area of the grid 55.
The first gas feeding system 70 comprises a first wind box 71. The first wind box 71 is formed by its bottom wall 76, top wall 77 and side wall(s) 78. The number of sidewalls 78 is determined by the cross-sectional shape of the first wind box 71; e.g., if circular, there is only one side wall encircling the wind box 71. The first feeding system 70 additionally comprises a first mixing element 101 through which the gas is arranged to flow into the first wind box 71.
The second gas feeding system 75 comprises a second wind box 80, which is respectively formed by its bottom wall 81, top wall 82 and side wall(s) 83. The second wind box 80 is arranged directly under the first wind box 71. The first wind box 71 and the second wind box 80 have a common wall with each other. The bottom wall 76 of the first wind box 71 and the top wall 82 of the second wind box 80 are integrally attached to each other or they may even be formed of a single common wall. In other words, the first wind box 71 is directly below the reactor 15 and the second wind box 80 is directly below the first wind box 71. The second feeding system 75 comprises a second mixing element 102, through which gas is arranged to flow into the second wind box 80.
Both of the first wind box 71 and the second wind box 80 are provided with gas inlets 85, 90, which open into the inner space of the respective wind box. The first mixing element 101 and the second second mixing element 102 are arranged in connection with the respective inlets, upstream thereof. The exhaust gas conduit 45 is provided with a recycling conduit 95 provided with a blower device 96. The recycling conduit 95 is arranged for introducing product gas resulting from the reactions taking place in the reactor chamber 15 as recycled gas. In practice, during the normal operation of combustion, the recycled product gas contains mostly CO2 and H2O.
The recycling conduit 95 is in connection with the first mixing element 101 through a conduit 107 and with the second mixing element 102 through a conduit 111. The conduits 107 and 111 are provided with first and second flow control devices 108 and 112, respectively.
The first mixing element 101 and the second mixing element 102 are connected to the gas inlets 85, 90, respectively. In the mixing elements 101 and 102, the oxygen-rich gas is introduced into the stream of recycled gas with simultaneous mixing. The amount of recycled gas introduced into each wind box 71 and 80 is controlled by the first flow control device 108 and the second flow control device 112. The flow control devices 108 and 112 may comprise, for example, a first control valve and a second control valve. According to an embodiment of the invention, the flow control devices 108 and 112 comprise dedicated inverter controlled blowers (not shown in the figure) provided in each of the conduits 107 and 111, in addition to or instead of a control valve. This provides an efficient way of controlling the amount of recycled gas introduced into the wind boxes 71 and 80. Having a blower instead of a valve minimizes unnecessary pressure losses, because the blower 96 in the recycling conduit 95 need not produce as high a pressure as in the case of using valves.
This enables the operation of the oxycombustion circulating fluidized bed reactor 10 in such a manner that the product gas of the reactions, which, in the case of combustion of carbonaceous fuel, taking place in the reactor 10 is mainly CO2 and H2O, may be partly recycled back to the reactor chamber 15, so that after a start-up phase, instead of air, the reactor 10 may be operated with a mixture of the product gas and oxygen. In this manner, the presence of nitrogen is avoided and recovery of CO2 from the exhaust gases may be more easily arranged.
The gas distribution arrangement 50 is also in connection with a source of oxygen-rich-gas 100, such as an Air Separation Unit (ASU). The source of oxygen-rich gas 100 is in connection with the first mixing element 101 through a conduit 103 provided with a third control valve 104 and with a second mixing element 102 through a conduit 105 provided with a fourth control valve 106.
The introduction of the gas into the reactor chamber 15 through the first wind box 71 is arranged to take place in the following manner. The third control valve 104 for oxygen-rich gas and the control device 108 for recycled gas are operated so that the gas introduced through the first gas feeding system 70 has a lower oxygen content than a first oxygen content, which, in practice, is about 28 vol.-%, preferably, about 23 to about 28 vol.-%. The first oxygen content preferably is adjusted such that a risk of self ignition of any combustible material present in the gas distribution arrangement 50 is minimized. In this manner, the operation of the reactor 10 is reliable and safe.
The introduction of the gas into the reactor chamber 15 through the second wind box 80 is arranged to take place in the following manner. The fourth control valve 106 for oxygen-rich gas and the control device 112 for recycled gas are operated so that the gas introduced through the second gas feeding system 75 has an elevated oxygen content being more than the first oxygen content. Thus, the oxygen content of the gas in the second wind box 80 is maintained substantially above the oxygen content of the air. Naturally, it is possible to adjust the oxygen content to be the same in both of the wind boxes, for example, when combustion with air is practiced, which is the case at least during the start-up phase.
The above-described arrangement makes it possible to introduce recycled gas with a certain predetermined oxygen content into both of the wind boxes 71 and 80. The mixing elements 101, 102 ensure that the gas entering into the wind boxes 71 and 80 has a substantially uniform composition. This minimizes the possibility of the existence of high local oxygen concentrations, which may cause premature ignition of carbonaceous material in a respective wind box and also local, overheated areas in the reactor chamber 15.
The total flow rate of the gas introduced through both the first and the second inlets 85, 90 and nozzles 60 and 65 is regulated based on the load of the oxy-combustion circulating fluidized bed reactor 10 and/or a predetermined requirement of the amount of fluidization gas flow rate. The amount of oxygen-rich gas introduced through the second gas inlet 90 and the nozzles 65 is regulated based on a predetermined target value of oxygen content of the gas introduced into the reactor chamber 15. In any case, it is preferable that the oxygen content of the gas introduced through the second wind box 80 is greater than the oxygen content of the first wind box 71, which is in connection with reactor chamber 15.
In a case in which any combustible material would enter the second wind box 80 having an elevated oxygen content, the risk of undesired ignition, despite the higher oxygen content, is minimized by maintaining a lower temperature in the second wind box 80 than that in the first wind box 71.
The combination of introducing the oxygen-enriched recycled gas having an elevated oxygen content through the second wind box 80 and arranging the second wind box 80 to be separated from the reactor chamber 15 by the first wind box 71 improves the safety of the circulating fluidized bed considerably. This is due to the fact that the temperature of the oxygen-rich gas in the second wind box 80, when in use, is maintained at a temperature lower than the temperature of the gas in the first wind box 71.
According to a preferred embodiment of the invention, the second wind box 80 is connected to the reactor chamber 15 through a plurality of conduits 140, which extend through the first wind box 71. In the embodiment of
According to an embodiment of the invention, the pipes 140 are removably installed between the bottom wall 76 and the top wall 77 of the first wind box 71, which facilitates the removal of the pipes for accessing the space in the first wind box 71 for maintenance and inspection purposes. In
In the method of operating an oxycombustion circulating fluidized bed reactor 10 comprising a reactor chamber 15 and a gas distribution arrangement 50 arranged in a bottom section of the reactor chamber 15, gas is introduced into the reactor chamber 15 through the gas distribution arrangement 50. The gas distributor arrangement 50 comprises a first gas feeding system 70 and a second gas feeding system 75, through which gas is introduced into the reactor chamber 15.
According to the invention, the gas introduced into the reactor chamber 15 contains recycled gas. The recycled gas is divided into streams comprising a stream that is controllably introduced into the first gas feeding system 70 and a stream that is controllably introduced into the second gas feeding system 75.
Oxygen-rich gas is introduced into the stream of recycled gas in the first gas feeding system 70, so that the oxygen content of the gas in the first gas feeding system 70 is less than or equal to a first oxygen content. Additionally, oxygen-rich gas is introduced into the stream of recycled gas in the second gas feeding system 75, so that the oxygen content of the gas in the second gas feeding system 75 is equal to or greater than the first oxygen content, that is, at an elevated oxygen content. The gas having an elevated oxygen content in the second wind box 80 of the second gas feeding system 75 is subjected to heat flow from the reactor chamber 15, which heat flow is decreased by warming the gas in the first wind box 71.
According to a preferred embodiment of the invention, the gas in the first wind box 71 is maintained at a temperature of less than about 300° C. and the gas in the second wind box 80 is maintained at a temperature of less than about 200° C. In this manner, despite the presence of oxygen-rich gas, a reliable operation of the circulating fluidized bed is ensured, and the risk of self ignition of combustible material is minimized.
The surfaces of the second wind box 80 are made of a fireproof material in the circumstances of elevated oxygen content gas, preferably, non-flammable, prevailing in the second wind box 80. The arrangement may be further improved by providing a base material, like carbon steel, of the first wind box 71 with an oxidizing prevention layer. This protects the base material from the effects of the oxygen-rich gas and the temperature in the second wind box 80. The oxidizing prevention layer is, according to an embodiment, a lining 135 on the inner walls of the second wind box 80, the lining being of a refractory material, for example, a ceramic material. The base material, like carbon steel, may also be lined with austenitic steel of a proper thickness. Protective liners and coatings of resistant alloys can also be used in conjunction with carbon steel or stainless steel.
The base material itself may be selected to withhold the circumstances caused by the presence of oxygen-rich gas. Thus, the prevention layer is, according to another embodiment of the invention, formed on the surface of the base material by the base material itself. For example, nickel- or copper-based super alloys may be successfully used. These alloys are oxidation and corrosion resistant materials and, when heated, a stable, passivating oxide layer is formed protecting the surface from further attack.
When operating the oxycombustion circulating fluidized bed reactor 10 according to the invention, in partial load circumstances, the present invention allows better controllability of the fluidization velocity due to the fact that the oxygen-rich gas is introduced independently of the introduction of the recycled gas. It is also clear that the described manner of introducing gas into the reactor chamber 15 may include further subsequent introduction of oxygen-rich gas for providing staged combustion, as depicted with reference number 150.
While the invention has been described herein by way of examples in connection with what are, at present, considered to the be the most preferred embodiments, it is to be understood that the invention is not limited to the disclosed embodiments, but is intended to cover various combinations or modifications of its features, and several other applications included within the scope of the invention, as defined in the appended claims. The details mentioned in connection with any embodiment above may be used in another embodiment when technically feasible.
| Number | Date | Country | Kind |
|---|---|---|---|
| 20085108 | Feb 2008 | FI | national |
This application is a U.S. national stage application of PCT International Application No. PCT/FI2009/050095, filed Feb. 5, 2009, published as PCT Publication No. WO 2009/098358 A2, on Aug. 13, 2009, and which claims priority from Finnish patent application number FI-20085108, filed Feb. 8, 2008.
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/FI09/50095 | 2/5/2009 | WO | 00 | 9/23/2010 |
