Source: http://www.google.com/patents/US7153481?dq=5,241,671
Timestamp: 2014-03-16 23:39:37
Document Index: 450774176

Matched Legal Cases: ['art 209', 'art 211', 'art 209', 'art 211', 'arts 209', 'arts 209', 'arts 209', 'art 109', 'art 111', 'art 109', 'art 111']

Patent US7153481 - Method and device for separating sulphur dioxide from a gas - Google PatentsSearch Images Maps Play YouTube News Gmail Drive More »Sign inAdvanced Patent SearchPatentsA device (1) for separating sulphur dioxide from a gas (4) by means of an absorption liquid has an inlet (2) for gas (4) containing sulphur dioxide, an outlet (18) for gas (16), from which sulphur dioxide has been separated, and as essentially horizontal apertured plate (8), which is arranged to allow...http://www.google.com/patents/US7153481?utm_source=gb-gplus-sharePatent US7153481 - Method and device for separating sulphur dioxide from a gasAdvanced Patent SearchPublication numberUS7153481 B2Publication typeGrantApplication numberUS 10/559,754PCT numberPCT/SE2004/000975Publication dateDec 26, 2006Filing dateJun 17, 2004Priority dateJun 26, 2003Fee statusPaidAlso published asCN1838985A, CN100434141C, EP1641554A1, EP1641554B1, EP2527027A2, EP2527027A3, US20060117953, WO2005007274A1Publication number10559754, 559754, PCT/2004/975, PCT/SE/2004/000975, PCT/SE/2004/00975, PCT/SE/4/000975, PCT/SE/4/00975, PCT/SE2004/000975, PCT/SE2004/00975, PCT/SE2004000975, PCT/SE200400975, PCT/SE4/000975, PCT/SE4/00975, PCT/SE4000975, PCT/SE400975, US 7153481 B2, US 7153481B2, US-B2-7153481, US7153481 B2, US7153481B2InventorsSune Bengtsson, Fredrik Jens Brogaard, Kerstin Forsgren, Rikard Hakansson, Kjell NolinOriginal AssigneeAlstom Technology LtdExport CitationBiBTeX, EndNote, RefManPatent Citations (4), Non-Patent Citations (1), Referenced by (3), Classifications (22), Legal Events (2) External Links: USPTO, USPTO Assignment, EspacenetMethod and device for separating sulphur dioxide from a gasUS 7153481 B2Abstract A device (1) for separating sulphur dioxide from a gas (4) by means of an absorption liquid has an inlet (2) for gas (4) containing sulphur dioxide, an outlet (18) for gas (16), from which sulphur dioxide has been separated, and as essentially horizontal apertured plate (8), which is arranged to allow passage from below of sulphur dioxide containing gas (4) and to carry, on its upper side (12), a flowing layer (14) of the absorption liquid. An outlet box (20) beside the apertured plate (8) is arranged to be passed by liquid, which is distributed in the gas (4) coming from the inlet (2). A first pumping means is arranged to feed a coolant flow to the outlet box (20) and a second pumping means is arranged to feed an absorption liquid flow, which is essentially independent of the coolant flow, to the apertured plate (8) to form the flowing layer (14). In a method of separating sulphur dioxide, the above-described device (1) can be used.
1. A method of separating by means of an aqueous absorption liquid sulphur dioxide from a gas containing sulphur dioxide, said method comprising the steps of:
a. passing the gas containing sulphur dioxide through a contact zone;
b. mixing the gas containing sulphur dioxide with a liquid flowing out of an outlet box while the gas containing sulphur dioxide is passing through the contact zone;
c. then passing the gas containing sulphur dioxide upwards through an essentially horizontal apertured plate arranged beside the outlet box and having a flowing layer of the aqueous absorption liquid provided thereon;
d. feeding a coolant flow to the outlet box so that the coolant flow passes therethrough and flows out into the contact zone; and
e. feeding to the essentially horizontal apertured plate an absorption liquid flow that is essentially independent of the coolant flow so that the flowing layer of the aqueous absorption liquid provided on the essentially horizontal apertured plate is thereby formed by the absorption liquid flow and is operative to effect the separation of sulphur dioxide from the gas containing sulphur dioxide.
a. collecting in a container containing liquid the coolant flow flowing out of the outlet box, the liquid surface of the liquid contained in the container being located at a level below the contact zone;
b. passing the gas containing sulphur dioxide through a passage located under the outlet box and extending between the liquid surface of the liquid contained in the container and the outlet box; and
c. controlling a parameter that is representative of the level of the liquid surface of the liquid contained in the container, and that is thus also representative of the height of the passage in such a manner that the average velocity of the gas containing sulphur dioxide in the passage is in the range of 5�35 m/s.
8. A device for separating by means of an aqueous absorption liquid sulphur dioxide from a gas containing sulphur dioxide, said device comprising:
a. an inlet for the gas containing sulphur dioxide and an outlet for the gas following the separation of sulphur dioxide therefrom;
b. at least one essentially horizontal apertured plate having an upper side and mounted between said inlet and said outlet, said at least one essentially horizontal apertured plate being arranged so as to allow passage of the gas containing sulphur dioxide from below said at least one essentially horizontal apertured plate, said at least one essentially horizontal apertured plate further being arranged so as to enable a flowing layer of the absorption liquid to be carried on said upper side of said at least one essentially horizontal apertured plate;
c. at least one outlet box arranged beside said at least one essentially horizontal apertured plate and so as to enable liquid to be passed thereby;
d. a distributing means arranged in said at least one outlet box to distribute liquid into the gas containing sulphur dioxide coming from said inlet before the gas containing sulphur dioxide is passed upwards and through said at least one essentially horizontal apertured plate;
e. a first pumping means for feeding a coolant flow to said outlet box; and
f. a second pumping means for feeding an absorption liquid flow that is essentially independent of the coolant flow to said at least one essentially horizontal apertured plate so that the flowing layer of the absorption liquid carried on said upper side of said at least one essentially horizontal apertured plate is thereby formed by the absorption liquid.
18. The device as claimed in claim 17 wherein said distributing means comprises at least one nozzle having at least one characteristic measurement selected from a minimum hole diameter and a minimum gap width of 1�8 cm.
TECHNICAL FIELD The present invention relates to a method of separating sulphur dioxide from a gas by means of an aqueous absorption liquid, in which method the gas is first passed through a contact zone, in which the gas is mixed with a liquid flowing out of an outlet box, and is then passed upwards through an essentially horizontal apertured plate which is arranged beside the outlet box and on which a flowing layer of the absorption liquid is provided.
BACKGROUND ART Sulphur dioxide is a gas formed by oxidation of materials containing sulphur, such as coal, oil, natural gas, industrial and domestic waste and peat. Sulphur dioxide can also be produced as a residual product in chemical processes, for instance in metallurgical processes. It is usually not allowed to emit large quantities of sulphur dioxide into the atmosphere, and therefore some kind of cleaning is necessary. One example is flue gas cleaning in power plants and other combustion plants. The flue gas generated in combustion in such plants is usually cleaned by, inter alia, absorption of sulphur dioxide in an absorption liquid. The absorption liquid may contain, for instance, water and one or more of the substances lime, limestone, dolomite, sodium hydroxide solution and similar substances, which are suitable for absorption of sulphur dioxide.
SUMMARY OF THE INVENTION The object of the present invention therefore is to provide an effective method of separating sulphur dioxide, in which method the above drawbacks of prior-art technique are eliminated or significantly reduced.
Preferably, the coolant flow flowing out of the outlet box is collected in a container containing liquid, whose liquid surface is located at a level below the contact zone, a passage, through which the gas is passed horizontally under the outlet box, extending between the liquid surface and the outlet box, and a parameter, which is representative of the level of the liquid surface, and thus the height of the passage, being controlled in such a manner that the average velocity of the gas in the passage is in the range of 5�35 m/s. An advantage of this is that the conditions in the cooling process can be adjusted to the current load in such a manner that good cooling, good wetting of the underside of the apertured plate and a low pressure drop in the gas are achieved.
According to a preferred embodiment, the distributing means comprises at least one nozzle, whose characteristic measure, such as a minimum hole diameter (D) or a minimum gap width (V), is 1�8 cm. These measures have been found to give good distribution of the liquid in the gas.
BRIEF DESCRIPTION OF THE DRAWINGS The invention will now be described in more detail by way of a number of embodiments and with reference to the accompanying drawings.
FIG. 2 is a sectional view in the vertical plane and shows section II�II in FIG. 1.
FIG. 3 is a sectional view in the vertical plane and shows section III�III in FIG. 1.
FIG. 4 is a sectional view in the vertical plane and shows section IV�IV in FIG. 1.
FIG. 5 a is a top plan view and shows the area V in FIG. 1.
FIG. 5 b is a top plan view and shows an alternative embodiment of a bottom of an outlet box.
FIG. 12 a is a sectional view in the vertical plane and shows section XII�XII in FIG. 11.
FIG. 12 b is an enlarged partial view in the vertical plane and illustrates the area XIIb shown in FIG. 12 a. FIG. 13 is a sectional view in the vertical plane and schematically shows a device according to a sixth embodiment of the invention.
DESCRIPTION OF PREFERRED EMBODIMENTS FIG. 1 shows schematically a device 1 according to the present invention. The device 1 has an inlet 2 for flue gas 4 from a boiler (not shown). As is best seen in FIG. 2, the flue gas 4 is in a first step passed through a contact zone 6. In the contact zone 6 the flue gas 4 is mixed with a liquid in such a manner that the gas is cooled and essentially saturated with water vapour by part of the liquid being evaporated. The flue gas 4 is then passed on to a horizontal rectangular apertured plate 8. The apertured plate 8 has a number of evenly distributed holes 10, through which the flue gas 4 can pass. On its upper side 12 the apertured plate 8 carries a flowing layer 14 of absorption liquid. As the flue gas 4 passes through the flowing layer 14 of absorption liquid, sulphur dioxide is separated from the flue gas 4. The cleaned flue gas 16 leaves the device 1 through an outlet 18 for cleaned flue gas 16.
The outlet box 20 is designed in such a manner that a desired flow of liquid leaves the nozzles 32. To prevent the flue gas 4 from passing through the nozzles 32 instead of through the holes 10, the outlet box must have a certain hydrostatic pressure Pl. A pressure difference dPr in the flue gas can be measured from a point A, which is located just before the contact zone 6, and a point B, which is located just above the liquid surface 48 in the outlet box 20. The hydrostatic pressure Pl in the outlet box 20 can then be calculated as a height hl, from the bottom 30 of the outlet box 20 to the liquid surface 48 straight above the bottom 30, multiplied by the density of the liquid in the outlet box 20 and the acceleration due to gravity g. To prevent flue gas from passing through the nozzles 32, Pl must be greater than dPr. The liquid leaving the nozzles 32 must have a certain velocity to provide good contact between this liquid and the flue gas 4 in the contact zone 6. It has been found that a liquid velocity of 0.2�3 m/s is appropriate. To provide this liquid velocity, the hydrostatic pressure Pl in the outlet box 20 must be significantly greater than dPr. It has been found that a height hl, which is at least about 100 mm higher than the height required to merely correspond to dPr, is appropriate to provide the abovementioned liquid velocity. It will also be appreciated that, at a small height H, a high pressure drop is obtained in the gap 40, which increases the pressure difference dPr, which in turn requires a great height hl in the outlet box 20.
FIG. 3 shows a first pumping means in the form of a first mammoth pump 50. The mammoth pump 50 has a vertical tube 52 which extends vertically upwards from a level just above the bottom 54 of the container 34 to the outlet box 20. The mammoth pump 50 also has a number of air nozzles 56 which are arranged vertically under the tube 52 and which through a conduit 58 with a control valve 60 arranged on the same is supplied with compressed air. The compressed air lowers the density of the liquid 36 and provides an upward liquid flow, indicated by an arrow CF, in the tube 52. This upward liquid flow will reach the outlet box 20 and be distributed in the same and then flow out in the contact zone 6, as described above. The liquid flow generated by the mammoth pump 50 can thus be called coolant flow since in the contact zone 6 it will flow out and cool the incoming flue gas 4. This coolant flow generated by the first mammoth pump 50 suitably corresponds to an L/G (i.e. liquid flow rate relative to gas flow rate) of about 2�5 litres liquid/m3 flue gas. The control valve 60 is adjusted in such a manner that the height hl in the outlet box 20 results in a suitable L/G and a suitable flow-out velocity from the nozzles 32. A typical value of hl is 0.5�1 m. Thus the valve 60 can be used to adjust the coolant flow rate according to the flow rate of the flue gas 4 and also according to the temperature and water content of the flue gas 4 in such a manner that sufficient cooling of the flue gas 4 and sufficient wetting of the underside 46 of the apertured plate 8 are provided. The width w of the outlet box 20, which is evident from FIG. 2, should at least in the upper portion of the outlet box 20 be sufficient for air bubbles coming along from the mammoth pump 50 to find their way to the liquid surface 48 instead of being entrained downwards by the liquid. To this end, the vertical downwardly directed liquid velocity in the outlet box 20 is suitably about 1 m/s maximum, preferably about 0.5 m/s maximum. Such a velocity has been found suitable to provide good deareation of the liquid, which also increases the density of the liquid. The selection of w is also influenced by the conditions that the longitudinally directed horizontal velocity in the outlet box 20 should not be too high, and that the interior of the outlet box 20 should be accessible for inspection and maintenance.
As shown in FIG. 3, the device 1 also has a second pumping means in the form of an elongate second mammoth pump 62. The mammoth pump 62 has a vertical tube 64 which extends vertically upwards from a level just above the bottom 54 of the container 34 to the upper side 12 of the apertured plate 8. The mammoth pump 62 also has a number of air nozzles 66 which are arranged vertically under the tube 64 and which through a conduit 68 with a control valve 70 arranged on the same are supplied with compressed air. The compressed air lowers the density of the liquid 36 and provides an upward liquid flow, indicated by an arrow AF, in the tube 64. This upward liquid flow will reach the upper side 12 of the apertured plate 8 and form the layer 14 flowing horizontally over the apertured plate 8. The liquid flow generated by the mammoth pump 62 can thus be called absorption liquid flow since on the apertured plate 8 it will separate and absorb sulphur dioxide from the incoming flue gas 4. The absorption liquid flow generated by the second mammoth pump 62 suitably corresponds to an L/G (i.e. liquid flow rate relative to gas flow rate) of about 10�50 litres absorption liquid/m3 flue gas and usually about 15�30 litres absorption liquid/m3 flue gas. The control valve 70 is controlled in such a manner that the layer 14 will have a sufficient thickness to be able to separate the desired amount of sulphur dioxide from the flue gas. A typical thickness of the layer 14 is 0.2�0.3 m, i.e. considerably smaller than the typical liquid height hl in the outlet box 20. The valve 70 is used to adjust the absorption liquid flow rate according to the flow rate of the flue gas 4 and the sulphur dioxide content of the flue gas 4 in such a manner that a stable layer 14 is obtained and sufficient separation of sulphur dioxide is provided. Thus the first mammoth pump 50 and the second mammoth pump 62 can be controlled independently of each other to generate a coolant flow which is adapted to cool the current flue gas 4 and, respectively, an absorption liquid flow rate which is independent of the coolant flow rate and is adapted to separate sulphur dioxide from the current flue gas 4.
The liquid 36 is an absorption liquid which essentially consists of a mixture of limestone, which is supplied to the container 34 from a storage (not shown) of a limestone suspension, and water and also gypsum and calcium sulphite formed in the separation of sulphur dioxide from the flue gas 4. The absorption liquid 36 can be prepared, for instance, in the manner disclosed in the WO 96/00122. As is evident from FIG. 3, both the coolant flow and the absorption liquid flow are supplied from the container 34. Thus both the coolant flow and the absorption liquid flow consist of absorption liquid 36. The content of solids in the absorption liquid can be as high as 20�30% by weight and, in some cases, higher than 30% by weight thanks to the mammoth pumps 50, 62 not having any movable parts which can be subjected to increased wear in case of high solids contents.
In absorption of sulphur dioxide in an absorption liquid containing limestone, calcium sulphite is formed. This should be converted into calcium sulphate, i.e. gypsum, to provide a reusable residual product and to minimise the risk of incrustations in the device, especially on the apertured plate 8. The compressed air flow used in the two mammoth pumps 50, 62 corresponds to an admixture of air of about 20�25% to the liquid that is fed upwards in the respective mammoth pumps 50, 62. In most cases, this amount of air is sufficient to oxidise formed calcium sulphite into gypsum. In some cases, for instance when the flue gas 4 itself has a very low oxygen content, it may be convenient to use a separate oxidation device 82, which by means of nozzles 84 supplies extra oxidation air to the absorption liquid 36 in the container 34.
FIG. 5 a shows the area V, indicated in FIG. 1, of the bottom 30 of the outlet box 20. The bottom 30 is provided with a first, seen in the horizontal flow direction of the flue gas 4, row 86 of nozzles 32 and a second, seen in said flow direction, row 88 of nozzles 32. The nozzles 32 have the form of circular holes. The shape of the circular holes can be cylindrical or, at one end, be rounded, bevelled or have some other form suitable for nozzles. The smallest diameter D, i.e. the narrowest cross-section in the nozzles 32, should be about 1�8 cm, preferably about 1�5 cm. With a diameter smaller than about 1 cm, droplets are obtained in the contact between the coolant flow and the flue gas 4, which are so small that they are to a great extent entrained by the flue gas 4 and cause an increased pressure drop and reduced cooling of the flue gas. With nozzles 32 having a diameter greater than about 8 cm, a poor contact is obtained between the coolant flow and the flue gas 4, the saturation of the flue gas with water vapour being insufficient. As is evident from FIG. 5 a, the nozzles 32 in the row 86 are offset relative to the nozzles 32 in the row 88. The purpose is to prevent bands of flue gas 4 from passing the contact zone 6 without water vapour being added.
FIG. 5 b shows an alternative embodiment of the bottom 30 shown in FIG. 5 a. The bottom 130 shown in FIG. 5 b has a first, seen in the horizontal flow direction of the flue gas 4, gap 132 and a second, seen in said flow direction, gap 133. The two gaps 132, 133 overlap each other to prevent bands of flue gas 4 from passing the contact zone 6 without coming into contact with the coolant flow. The smallest gap width V, i.e. the narrowest cross-section in the gap 132, 133, should be about 1�5 cm for the same reasons as stated above for the circular nozzles 32.
FIGS. 7�9 illustrate a third embodiment of the invention in the form of a device 200. As is evident from FIG. 7, the device 200 has a first apertured plate 208A, which is divided into a first part 209A and a second part 211A, and a second apertured plate 208B, which is divided into a first part 209B and a second part 211B. A first elongate outlet box 220A is arranged along a first lateral edge 222A of the first apertured plate 208A, which is also to be seen in FIG. 8. A second elongate outlet box 220B is arranged along a first lateral edge 222B of the second apertured plate 208B. Between the two outlet boxes 220A, 220B, which are oriented towards each other, a gap 221 is formed, in which a gas inlet 202 opens.
The flue gas 204, which through the inlet 202, which is best-seen in FIG. 9, is supplied to the gap 221, will be distributed between the first and the second outlet box 220A, 220B and cooled by the respective coolant flows when passing horizontally under the respective outlet boxes 220A, 220B. The flue gas 204 will then pass through the layers (not shown in FIGS. 7�9) of absorption liquid provided on the parts 209A, 211A and 209B, 211B respectively, whereby sulphur dioxide is separated. The pressure drop in the gas across the layers of absorption liquid provided on the parts 209A, 211A, 209B, 211B is considerably greater than the pressure drop across the outlet boxes 220A, 220B. A control which ensures that the respective second mammoth pumps 262A, 262B pump a flow of the same size to the first apertured plate 208A and to the second apertured plate 208B, i.e. that the layers will have the same thickness on both apertured plates 208A, 208B, will also ensure that the flue gas 204 will be evenly distributed between the two outlet boxes 220A, 220B. The cleaned flue gas 216 then leaves the device 200 through outlets 218 for gas arranged on both sides of the inlet 202. The coolant flows that have flown out of the respective outlet boxes 220A, 220B and the absorption liquid flows that have flown out of the respective parts 209A, 211A, 209B, 211B are collected in a common container 234, from which the liquid is again fed by the respective mammoth pumps 250A, 262A, 250B, 262B.
FIG. 10 shows a fourth embodiment of the invention in the form of a device 300. Flue gas 304 is introduced into the device 300 through an inlet 302. In a first step, the flue gas is cooled and saturated with water vapour when passing horizontally under an outlet box 320 which is of essentially the same type as the outlet box 20 that is shown in FIGS. 1 and 3. The flue gas is then passed upwards through an apertured plate 308 and passes through a flowing layer 314 of absorption liquid provided thereon, whereby sulphur dioxide is separated. Cleaned flue gas 316 leaves the device through an outlet 318. Liquid flowing out of the outlet box 320 is collected in a first container 334. The container 334 is provided with a recirculation pump 351, which advantageously can be a mammoth pump and which through a conduit 353 feeds liquid from the first container 334 to the layer 314. The container 334 contains liquid 336, whose liquid surface 338 is located under the outlet box 320. Between the liquid surface 338 and the bottom of the outlet box 320 a gap 340 is thus formed, through which the flue gas 304 must pass. The level of the liquid surface 338, and thus the width of the gap 340, can be controlled by means of the recirculation pump 351 in such a manner that a gas velocity is provided, which is suitable for the cooling of the flue gas 304 by the liquid flowing out of the outlet box 320. The outlet box 320 is supplied with a coolant flow in the form of absorption liquid 336 from a second container 335. A first pump 350, which can be a mammoth pump, feeds through a conduit 352 the absorption liquid 336, corresponding to an L/G of about 2�5 l/m3 flue gas, from the second container 335 to the outlet box 320. A second pump in the form of a mammoth pump 362, which comprises compressed air nozzles 366, a compressed air line 368 and a control valve 370, feeds an absorption liquid flow in the form of absorption liquid 336 from the second container 335 to the flowing layer 314 and over the apertured plate 308. The absorption liquid flow pumped by the mammoth pump 362 corresponds to about 15�30 l/m3 flue gas. At an end, opposite to the second pump 362, of the apertured plate 308 a return conduit 380 is arranged, which recirculates the absorption liquid to the second container 335. Thus the recirculation pump 351 will pump liquid from the first container 334 to the second container 335 via the layer 314 and the return conduit 380. The absorption liquid which possibly flows through the holes of the apertured plate 308, not shown in FIG. 10, is collected on an inclined bottom 381 and passed to the first container 334. The level in the second container 335, can independently of the level in the first container 334, be set at a level, usually higher than the level in the first container 334, which means that a minimum of pumping work is required to generate the layer 314 and also the coolant flow to the outlet box 320.
FIGS. 11, 12 a and 12 b illustrate a fifth embodiment of the invention in the form of a device 400. The device 400 bears great resemblance to the device 1 shown in FIGS. 1�4 and the parts of the device 400 which have direct equivalences in the device 1 have therefore been given the same designations and will here not be described in more detail. In the device 400 shown in FIG. 11, a flowing layer 414 of absorption liquid is passed horizontally over the rectangular apertured plate 8 in the direction of arrow AL for the purpose of separating sulphur dioxide from the flue gas 4 which passes through the flowing layer 414. The flowing layer 414 is fed to the apertured plate 8 in the manner as described above with reference, above all, to FIG. 3.
FIG. 12 a illustrates an outlet zone 480, which is formed between the guide rail 76 attached to the third lateral edge 74 of the apertured plate 8 and a vertical wall 490 positioned opposite to the lateral edge 74, in the device 400. In the outlet zone 480, where the absorption liquid leaves the apertured plate 8 to flow down into the container 34, a throttle valve 492 is arranged horizontally and adapted to be turned by a motor 493 shown in FIG. 11. The throttle valve 492 has a horizontal shaft 494, which extends parallel to the third lateral edge 74 and which, as best seen in FIG. 12 b, has a first flap blade 495 and a second flap blade 496, said flap blades 495, 496 extending along a common plane. Thus the motor 493 is arranged to turn the throttle valve 492 on the horizontal shaft 494.
FIG. 12 b shows the angle α which is formed between the flap blades 495, 496 and the horizontal plane. As can be seen, a first constriction 497 is formed between the first blade 495 and the guide rail 76, and a second constriction 498 is formed between the second blade 496 and the wall 490. The pressure drop which the absorption liquid must overcome to flow through the outlet zone 480 and down into the container 34 is dependent on the width of these constrictions 497, 498. By means of the motor 493, the angle α and thus the width of the constrictions 497 and 498 can be set. At a small angle α, for instance an angle α of about 20�30�, the width of the constrictions 497, 498 will be small. The absorption liquid will thus be subjected to a high pressure drop when it should flow through the outlet zone 480 and down into the container 34, and thus the thickness of the layer 414 will increase until equilibrium is achieved between the thickness of the layer 414 and the pressure drop in the constrictions 497, 498. If a smaller thickness of the layer 414 is desired, the angle α is increased by means of the motor 493 which turns the shaft 494 and thus the flap blades 495 and 496, for instance to an angle α of about 40�50�, thereby increasing the width of the constrictions 497 and 498 so that the pressure drop decreases, in which case the absorption liquid is subjected to a lower pressure drop when it should flow through the outlet zone 480 and down to the container 34. Thus, the throttle valve 492 shown in FIGS. 11, 12 a and 12 b provides a further possibility of adjusting the thickness of the layer 414. This adjustment has its greatest effect on the thickness T of the layer 414 next to the outlet zone 480. An advantage of the throttle valve 492 thus is that it improves the control of the thickness of the layer 414 and, thus, is complementary to the control of the mammoth pump 62 to provide the thickness of the layer 414 that gives sufficient separation of sulphur dioxide in the current case of operation. A further advantage is that a thickness of the layer 414 will be more even seen over the entire apertured plate 8, which reduces the risk that the separation of sulphur dioxide will be low in the area next to the outlet zone 480.
FIG. 13 illustrates, in a sectional view essentially corresponding to the sectional view shown in FIG. 4, a sixth embodiment of the invention in the form of a device 500. The device 500 bears great resemblance to the device 1 shown in FIGS. 1�4 and the parts of the device 500 which have direct equivalences in the device 1 have therefore been given the same designations and will here not be described in more detail. In the device 500 shown in FIG. 13, a flowing layer 514 of absorption liquid is passed horizontally over the rectangular apertured plate 8 in the direction of arrow AL from an inlet zone 578 to the outlet zone 80 for the purpose of separating sulphur dioxide from the flue gas 4 passing through the flowing layer 514. From a vertical wall 590 located opposite to the second lateral edge 72 extends a guide rail 592 in the outlet zone 578. The guide rail 592 extends essentially horizontally from the wall 590 towards the apertured plate 8 at a level, in the vertical direction, above the apertured plate 8. As shown in FIG. 13, the guide rail 592 is arcuate. The upward liquid flow AF, which is generated by the mammoth pump 62, will be deflected by the guide rail 592 from a vertical flow direction to a horizontal flow direction and form the flow AL which is conducted over the apertured plate 8. The guide rail 592 will damp the pulsations that often arise in a mammoth pump and will result in the mammoth pump 62 generating an even flow over the apertured plate 8. Furthermore, the deflection will cause, by means of the guide rail 592, that the absorption liquid flow, that has a vertical velocity in the tube 64, will obtain a higher initial horizontal velocity when leaving the outlet zone 578 and being passed over the apertured plate 8. This helps to make the thickness of the layer 514 more even over the entire apertured plate 8. It will be appreciated that guide rails of the type illustrated in FIG. 13 are also suited for use in the type of devices 100 and 200 as shown in FIG. 6 and FIGS. 7�9 respectively. For instance, in the device 100 there are suitably arranged a first guide rail extending towards the first part 109 of the apertured plate 108 and a second guide rail extending towards the second part 111 of the apertured plate 108. In the device 100 shown in FIG. 6, such guide rails would have the additional function of improving the distribution of the absorption liquid flow between the first part 109 and the second part 111. Of course, it is also possible to combine, in one and the same device, the throttle valve 492 as shown, for instance, in FIG. 12 a, with the guide rail 592 shown in FIG. 13.
The embodiments with rectangular apertured plates, as described in FIGS. 1�4, FIG. 6 as well as FIGS. 7�9, are well suited to produce module systems. Consequently, for instance 2�4 units of the device 1 can be built in parallel in order to jointly treat a flow of flue gas.
EXAMPLE This Example relates to a test on a pilot scale involving a device of the type described above with reference to FIGS. 1�4 and 5 a. The apertured plate 8, which was made of polypropylene, had a thickness of 30 mm and a free hole area of about 3.6%, the holes 10 having a diameter of 22 mm. The holes 22 were bevelled at the underside 46 of the apertured plate 8. Limestone, that had such a grain size that about 96% passed through a mesh of 44 μm, was supplied to the container 34 in the form of a 25% by weight aqueous suspension. Additional water was supplied to the container 34. The absorption liquid 36 in the container contained in operation about 13% by weight of solids and had a pH of about 5.4.
Flue gas 4 from an oil-fired power plant was cleaned, the incoming gas unsaturated with water vapour had a temperature of about 190� and a sulphur dioxide concentration of about 2000 ppm. The flue gas 4 was passed through the inlet 2 to the gap 40. The liquid surface 38 in the container 34 was adjusted to such a level that the gas velocity in the gap 40 was about 15 m/s. The pressure difference between the point A and the point B was estimated at 4600 Pa. A first mammoth pump 50 fed a coolant flow corresponding to 3 l/m3 of the current flue gas to the outlet box 20. A second mammoth pump 62 fed an absorption liquid flow corresponding to 20 l/m3 of the current flue gas to the inlet zone 78 to form the layer 14. The height hl in the inlet box 20 was 700 mm, corresponding to a hydrostatic pressure Pl of about 7700 Pa. The circular holes 32 in the bottom 30 of the outlet box 20 had a diameter of about 2 cm. The number of circular holes 32 was such that the velocity of the liquid leaving the holes 32 at the current hydrostatic pressure was about 1.5 m/s. As far as could be estimated in a visual check, the gas 4 entrained about 10% of the absorption liquid that left the circular holes 32 in the bottom 30 of the outlet box 20 while the rest of the absorption liquid reached the liquid surface 38. In the course of the test, no clogging of the holes 10 of the apertured plate 8 and no incrustations on the underside 46 of the apertured plate 8 could be observed. A clear flushing effect, that was provided by the absorption liquid entrained by the gas 4, could also be observed on the underside 46. A measurement showed that the gas 4 just under the apertured plate 8 kept a temperature of about 57� and was essentially saturated with water vapour. Thus, the relatively seen limited coolant flow was sufficient to achieve the desired cooling. The gas 16 that left the device 1 had a temperature of about 55� C. and contained about 22 ppm sulphur dioxide. Tests involving changes of the flow rate of flue gas were also performed and demonstrated that the cooling zone 6 as well as the layer 14 operated in a stable manner as the flue gas flow rate was varied.
Patent CitationsCited PatentFiling datePublication dateApplicantTitleUS5693301 *Feb 27, 1995Dec 2, 1997Abb Flakt AbMethod for removing sulphur dioxide from a gasUS5759505 *Apr 13, 1995Jun 2, 1998Abb Flakt Industri AbMethod and device for removing sulphur dioxide from a gasUS7094382 *Jul 4, 2002Aug 22, 2006Alstom Technology LtdMethod and a device for the separation of sulphur dioxide from a gasWO2003004137A1Jul 4, 2002Jan 16, 2003Alstom Switzerland LtdA method and a device for the separation of sulphur dioxide from a gas* Cited by examinerNon-Patent CitationsReference1PCT International Search Report dated Sep. 29, 2004 (PCT/SE2004/000975).Referenced byCiting PatentFiling datePublication dateApplicantTitleUS7560084 *Mar 30, 2007Jul 14, 2009Alstom Technology LtdMethod and device for separation of sulphur dioxide from a gasUS7985281 *Dec 5, 2006Jul 26, 2011Alstom Technology LtdBubbling bed reactor and a method of separating a gaseous pollutant from a gasUS8277545Jun 23, 2010Oct 2, 2012Alstom Technology LtdMethod of reducing an amount of mercury in a flue gas* Cited by examinerClassifications U.S. Classification423/243.01, 422/169, 423/243.09, 422/176, 422/168, 423/243.08International ClassificationB01J10/00, B01D53/18, B01D53/50, B01J10/02, B01D53/78, B01D53/34, B01D53/14Cooperative ClassificationB01D2251/606, B01D2259/124, B01D2251/404, B01D53/78, B01D53/504, B01D53/346European ClassificationB01D53/50B4, B01D53/34Y, B01D53/78Legal EventsDateCodeEventDescriptionMay 21, 2010FPAYFee paymentYear of fee payment: 4Dec 7, 2005ASAssignmentOwner name: ALSTOM TECHNOLOGY LTD, SWITZERLANDFree format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:BENGTSSON, SUNE;BROGAARD, FREDRIK JENS;FORSGREN, KERSTIN;AND OTHERS;REEL/FRAME:017621/0226;SIGNING DATES FROM 20051108 TO 20051118RotateOriginal ImageGoogle Home - Sitemap - USPTO Bulk Downloads - Privacy Policy - Terms of Service - About Google Patents - Send FeedbackData provided by IFI CLAIMS Patent Services©2012 Google