System for combined flue gas heat recovery and dust precipitation improvement as retrofit solution for existing coal-fired power stations

Abstract

A power plant is suggested with an additional heat transfer between the flue gas that flows through a flue gas line (5) and the feed-water in a feed-water line (19). The claimed arrangement of the first heat exchanger (13) upstream and adjacent to a precipitator (7) leads to a reduced space demand and optimizes dust precipitation as well as the pressure drop of the flue gas.

Claims

1. A power plant having a boiler for combusting carbonaceous fuel and generating flue gas having dust disposed therein, said power plant comprising: a flue gas line to convey flue gas; a diffuser to receive and diffuse flue gas from the flue gas line; a first heat exchanger in fluid communication with the diffuser to receive and cool flue gas from the diffuser; a dust precipitator abuttingly connected to the first heat exchanger to receive flue gas from the first heat exchanger and remove dust from the flue gas received from the heat exchanger; an induced draft fan downstream of the dust precipitator for raising the pressure of flue gas exiting the dust precipitator and transporting the flue gas exiting the dust precipitator towards an outlet stack; and a second heat exchanger in parallel to a first feedwater heater, wherein heat extracted from flue gas passing through the first heat exchanger is transferred to a thermal energy carrier that flows through conduits to the second heat exchanger, and wherein the second heat exchanger is configured to heat feedwater bypassing the first feedwater heater with heat from the thermal energy carrier, wherein the diffuser and the first heat exchanger are disposed upstream of the dust precipitator system, the diffuser is configured to reduce a velocity of flue gas flowing to both the first heat exchanger and the dust precipitator, and wherein the first heat exchanger and the dust precipitator define respective cross-sections where the first heat exchanger and the dust precipitator directly abuttingly connect, and the respective cross sections are the same.

2. The power plant according to claim 1, wherein the dust precipitator is an electrostatic precipitator.

3. The power plant according to claim 1, wherein flue gas enters in a horizontal direction into the first heat exchanger and the dust precipitator.

4. The power plant according to claim 1, further comprising: an air heater to receive flue gas therethrough, the air heater located downstream of the boiler and upstream of the first heat exchanger.

5. The power plant according to claim 1, wherein a velocity of flue gas exiting the first heat exchanger is approximately the same as a velocity of flue gas entering the dust precipitator.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 an embodiment of the claimed power plant,

(2) FIG. 2 an inventive flue gas cooler and precipitator with horizontal gas flow,

(3) FIG. 3 a flue gas cooler and a separate precipitator, and

(4) FIG. 4 an embodiment showing a flue gas cooler with vertical flue gas flow.

DETAILED DESCRIPTION

(5) FIG. 1 shows an embodiment of the claimed invention consisting of a combined system to recover heat from flue gas downstream an air heater and to improve the dust precipitation of the flue gas in a fired steam power plant.

(6) The claimed power plant comprises a boiler 1 that may be fired by coal. The combustion air flows through an air heater 3 which is heated by the flue gas that flows through a flue gas line 5. In the boiler feed-water is converted into steam thereby raising the pressure by raising the temperature of the feed-water that enters the boiler.

(7) Since the boiler 1 of a conventional fossil fuel fired power plant works is well known to a man skilled in the art, the boiler 1 and the feed-water and steam circulation inside the power plant are not described in detail. In FIG. 1 only the components that are of relevance with regard to the claimed invention are schematically shown and will be described in more detail.

(8) The flue gas that exits from the boiler 1 with a temperature of about 350 Celsius transfers heat in the air heater 3 to the combustion air. After having passed the air heater 3, the flue gas in the flue gas line 5 has a temperature of approximately 130 to 160 Celsius. The temperature of the combustion air is raised when the combustion air flows through the air heater accordingly.

(9) Since the flue gas that has passed the air preheater still contains particles and pollutant components the flue gas will be cleaned for example in a dust precipitator 7, which can be a so called electrostatic precipitator (ESP), a so called baghouse or any other type of precipitator. After having passed the precipitator 7 an induced draft IDfan 9 raises the pressure of the flue gas in the flue gas line 5 and transports it through a stack 11 into the ambient air.

(10) The claimed invention further comprises a first heat exchanger 13 upstream of the precipitator 7 and directly connected to the precipitator 7. This first heat exchanger serves to cool the flue gas that flows through the flue gas line 5. The heat that has been extracted from the flue gas in the first heat exchanger 13 is transferred to a thermal energy carrier that flows through conduits 15 to a second heat exchanger 17. The second heat exchanger 17 may be a shell and tube heat exchanger. The shell of the second heat exchanger 17 is connected to the conduits 15 and consequently the heat transfer medium that flows to the conduits 15 also flows through the shell of the second heat exchanger 17.

(11) On the other side the second heat exchanger 17 is connected to a feed-water line 19. The feed-water line 19 starts at the condenser (not shown) of the power plant and finally enters the boiler 1 (not shown). On its way from the condenser to the boiler 1 the feed-water that flows through the feed-water line is raised in temperature by several feed-water heaters, starting for example with a first low pressure (LP) feed-water heater 21.

(12) As can be seen the second heat exchanger 17 is arranged parallel to the first feed-water heater 21 and its tubes are connected to the feed-water line 19 by a bypass line 25. Consequently a part of the feed-water that flows through the feed-water line 19 passes the second heat exchanger 17. For purposes of control of the flow through the second heat exchanger 17 a control valve 23 can be installed in the bypass line 25.

(13) This leads to a great flexibility of the feed-water flow through the second heat exchanger 17 and consequently to an improved behaviour of the power plant and its overall efficiency, since an optimized heat transfer from the flue gas to the feed-water can be achieved by controlling the flow through valve 23 through the bypass line 25. Further improved control of the heat transfer can be achieved if the flow rate through the conduits is controlled. This can be achieved by means of pump 27 and/or a valve 29. The pump 27 is preferably of the variable speed type.

(14) As mentioned above the heat transfer from the flue gas to the feed-water using the first heat exchanger 13, the conduits 15, and the second heat exchanger 17 improves the overall efficiency of the power plant and consequently improves the performance and/or reduces the fuel consumption of the power plant.

(15) A further very important aspect of the claimed invention is that due to the reduction of the temperature of the flue gas in the first heat exchanger 17 the volume flow of the flue gas is reduced and therefore the average velocity of the flue gas in the precipitator is also reduced. This leads to reduced pressure losses in the precipitator and an improved purification efficiency of the precipitator. Especially for low-sulfur coals the precipitation efficiency is strongly improved by means of temperature reduction and thereby decrease of dust resistivity. Since the flue gas volume flow rate is decreased the load of the fan 9 is at least not significantly raised by adding the pressure drop creating first heat exchanger 13 in the flue gas line 5.

(16) The gains in terms of unit efficiency rise are realized by transferring the recovered heat from flue gas into the feedwater of the water-steam cycle. This is done via the intermediate cycle 15, which is connected to the first heat exchanger 13 and the second heat exchanger 17. The second heat exchanger is installed in parallel to one or more of the existing feed-water heaters 21.

(17) The feed-water heaters 21 are partly bypassed and consequently extract less steam from the turbine. This reduced steam consumption of the feed-water heaters 21 directly contributes to additional power generation and/or raises unit efficiency.

(18) To be able to carry out heat recovery from flue gas with reasonable flue gas pressure drop it is necessary to reduce the flow velocity inside of the first heat exchanger 13. In FIG. 2 such an arrangement is shown for horizontal gas flow. As can be seen from FIG. 2 between the flue gas line 5 and the first heat exchanger 13 upstream of the first heat exchanger 13 is a diffuser 31 that leads to a reduction of velocity of the flue gas inside the first heat exchanger 13 and the precipitator 7, that is installed adjacent and downstream of the first heat exchanger 13. Downstream of the precipitator 7 there is the need of reducing the volume of the flue gas line 5 which leads to the installation of a concentrator 33. The concentrator 33 raises the velocity of the flue gas so that the cross-section of the flue gas line 5 upstream and downstream of the heat exchanger 13 and the precipitator 7 are similar.

(19) For reasons of comparison in FIG. 3 a less optimal configuration of a first heat exchanger 13 and a precipitator 7 is shown. In this configuration the first heat exchanger 13 and the precipitator 7 are not installed adjacent to each other. In this configuration between the first heat exchanger 13 and the precipitator 7 an additional concentrator 35 and an additional diffuser 37 are required. This would lead to an additional pressure drop in the flue gas and of course resulting in additional costs for building and installing the components 35 and 37.

(20) Further on the space that is required for installing the inventive first heat exchanger increases in the configuration shown in FIG. 3 compared to the preferred configuration of FIG. 2. Further on, if the configuration according to FIG. 3 were realized between the second diffuser 37 and the precipitator 7 an inlet screen plate 39 were required for a better distribution of the flue gas in the precipitator 7.

(21) To summarize, the arrangement shown in FIG. 2 leads to some major advantages which are mainly, a compact and efficient design, with reduced costs for building and installation. This aspect is of great importance with regard to retrofit in existing power plants, since normally the available space in existing power plants is rare and therefore a compact solution is highly appreciated.

(22) Further on, the pressure drop of the flue gas in the installation shown in FIG. 2 is rather small compared to an installation without first heat exchanger 13, since the pressure drop caused by the first heat exchanger 13 is at least partially compensated by the fact, that no inlet screen plate 39 (see FIG. 3) is required. Consequently in almost each case the ID-fan 9 may remain unchanged and therefore the investment for installing the inventive heat transfer from the flue gas to the feed-water is reduced.

(23) Preferably the first heat exchanger is a so called tubular heat exchanger or plate heat exchanger. The flue gas that flows through the diffuser 31 and the first heat exchanger 13 is automatically distributed equally over the whole cross section area of the precipitator 7. Consequently no inlet screen plates are necessary. Consequently the pressure drop that is normally caused by the inlet screen plates is avoided and therefore at least a part of the pressure drop caused by the first heat exchanger 13 in the flue gas is compensated by avoiding the inlet screen plate.

(24) In FIG. 4 a second embodiment of the combination of first heat exchanger 13 and precipitator 7 are shown. In this embodiment the flue gas 5 flows through the first heat exchanger 13 in a vertical direction and is deflected by a deflector 41 and then enters the precipitator 7 in a more or less horizontal direction. The tubes or plates inside the first heat exchanger 13 as well as the filter interiors of the precipitator are not shown in FIG. 4, since these components are known to a man skilled in the art.

(25) The claimed invention leads to an improved purification efficiency of the precipitator 7 and improved overall efficiency of the power plant due to the heat transfer from the flue gas to the feed-water.

(26) Further on the claimed invention needs only a little additional space upstream and adjacent of the precipitator 7 and therefore can be installed as a retrofit solution in a great number of existing coal-fired steam plants. Since the pressure drop of the flue gas due to the additional first heat exchanger 13 can be kept in a reasonable range the existing fan 9 of the flue gas can remain unchanged. Consequently the investment costs for a retrofit solution are rather attractive compared to the gain of overall efficiency and therefore reduced fuel costs.