US20020116908A1 - Mobile granular bed filtration apparatus for hot gas conditioning - Google Patents
Mobile granular bed filtration apparatus for hot gas conditioning Download PDFInfo
- Publication number
- US20020116908A1 US20020116908A1 US09/972,684 US97268401A US2002116908A1 US 20020116908 A1 US20020116908 A1 US 20020116908A1 US 97268401 A US97268401 A US 97268401A US 2002116908 A1 US2002116908 A1 US 2002116908A1
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- United States
- Prior art keywords
- filtration
- tubular member
- granular
- gas
- inlet
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- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/30—Particle separators, e.g. dust precipitators, using loose filtering material
- B01D46/32—Particle separators, e.g. dust precipitators, using loose filtering material the material moving during filtering
- B01D46/38—Particle separators, e.g. dust precipitators, using loose filtering material the material moving during filtering as fluidised bed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2273/00—Operation of filters specially adapted for separating dispersed particles from gases or vapours
- B01D2273/20—High temperature filtration
Definitions
- a variety of hot gas filters are known.
- One branch of prior art is concerned with fixed bed filters.
- hot gases pass through a mass of filtering granules.
- These filters require frequent cleaning and regeneration of the filtering media as the filters quickly become plugged.
Abstract
Description
- 1. Field of the Invention
- The present invention relates to the treatment of hot gases from either combustion, gasification or pyrolysis processes. More specifically, the invention relates to a granular bed filtration apparatus for conditioning the above said gases.
- 2. Description of the Prior Art
- Classical power plants and incinerators produce electrical power by generating steam with hot combustion gases in a boiler and using the steam to drive steam turbines. Advanced high efficiency power generation methods are based on gasification or pyrolysis of appropriate feedstocks and use of the resulting synthetic gas either in burners coupled with gas turbines or in internal combustion engines. The gas turbines fed with hot combustion gases are prone to rapid deterioration because of particulate and corrosive particles contained in the combustion gases. Thus, it is necessary to filter and otherwise condition the hot combustion gases before their entry into the power turbines.
- In a preliminary treatment, hot gases exiting a combustion chamber are generally submitted to a cyclonic treatment to remove particulate material larger than about 10 μm. Smaller particles remain in the gas stream and must also be removed to avoid corrosion, pitting and other deterioration of the turbines. These smaller particles are the target of specialized hot gas filters.
- A variety of hot gas filters are known. One branch of prior art is concerned with fixed bed filters. In a fixed bed filter, hot gases pass through a mass of filtering granules. These filters require frequent cleaning and regeneration of the filtering media as the filters quickly become plugged.
- Another branch of prior art is concerned with mobile bed filtering equipment where the filtering granules are constantly moved. Movement is generally achieved by pneumatic recirculation and gravitational cascade between baffles. This technique allows better interception of small particulate matter and allows filtering granule regeneration without interrupting the filtering operation. For example, U.S. Pat. No. 4,017,278 proposes the use of two concentric vertical cylindrical parts. The inner wall being perforated to permit only the passage of the gas while the outer wall is appropriately louvered to allow particles passing through with the gas while maintaining granular filtering material trapped in the annular space and in continuous movement downwards. The granules leaving the filter from the bottom of the filter being recycled back pneumatically after being cleaned in a cyclonic collector. However, the recirculation of filtration particles requires additional energy and instrumentation.
- Yet another branch of prior art is concerned with fluid-bed filters. In fluid-bed filters, the filtering material is kept fluidized by the flow of hot gas. For example, U.S. Pat. No. 4,157,959 proposes a three-stage filtration method. In a first stage a cylindrical fixed bed of granules is used to filter out particles from an upward flowing gas stream; during this operation a particles layer (cake) is built at the bottom of the fixed bed, which is kept immobile by means of an adjustable rod/plate combination. In a second stage, the plate is raised, allowing the particle bed to be converted to a bubbling fluidized one. The filtration continues up to maximum allowable pressure drop occurring when the filter requires cleaning. In the last and third step, the filtering granules are regenerated. The main drawback of such technique is the requirement for moving parts and the downtime associated with filtering granule regeneration.
- Thus, despite advances in the art, there remains an important need for an improved hot gas filtration system capable of overcoming the drawbacks of the prior art.
- One object of the present invention is to provide a hot gas filtration apparatus which combines the benefits of a mobile granular filtration bed and a fluidized bed.
- A further object is to provide a hot gas filtration apparatus capable of operating at elevated temperatures and preferably without moving parts and without the requirement for recirculating pumps.
- The present invention provides a granular filtration apparatus for the removal of particulate material from hot gas by contacting said hot gas with granular filtration material. The apparatus being of the type having a filtration chamber containing granular filtration material and having a tapered lower portion comprising at least one inlet tubing for feeding therein hot gases to be filtered and at least one outlet tubing for drawing filtered hot gas. The main features of the present invention consist of a filtration unit mounted in the filtration chamber above each inlet tubing. The filtration unit comprising a first tubular member mounted above the inlet tubing so as to prevent granular material from entering or blocking said inlet tubing and a second tubular member having a bottom and a top end and being mounted essentially in a co-axial and spaced relationship above the first tubular member. During operation, the granular filtration material is siphoned up and fluidized by the hot gases as they travel up the second tubular member, the granular filtration material enters the bottom end of the second tubular member through the space between the first and second tubular member, exits at the top end of the second tubular member and falls to the tapered lower portion of the filtration chamber to be eventually recirculated and fluidized by the hot gases.
- The invention also provides a novel gas inlet distribution plate fastened between the bottom tapered portion of the filtration chamber. The distribution plate is provided with a plurality of gas distribution tuyeres and is encased with the first tubular member as described above.
- Other features and further scope of applicability of the present invention will become apparent from the detailed description given hereinafter. It should be understood, however, that this detailed description, while indicating preferred embodiments of the invention, is given by way of illustration only, since various changes and modifications within the spirit and scope of the invention will become apparent to those skilled in the art.
- FIG. 1 is a perspective view of the filter of the present invention;
- FIG. 2 is a top view of the filter;
- FIG. 3 is a side elevation view of the filter;
- FIG. 4 is cut-away perspective view of the filter showing internal components;
- FIG. 5 is a magnified view of FIG. 4 showing in detail the hot gas feed to the filter;
- FIG. 6 is a cross-sectional, side elevation view of the filter, in operation;
- FIG. 7 is pictorial representation of the gas sampling train used to evaluate the particle retention efficiency of the filter.
- Before describing the present invention in detail, it is to be understood that the invention is not limited in its application to the details of construction and parts illustrated in the accompanying drawings and described herein. The invention is capable of other embodiments and of being practiced in various ways. It is also to be understood that the phraseology or terminology used herein is for the purpose of description and not limitation.
- The present invention provides a novel hot gas filter for recuperating particulate matter in hot gas prior to its use. The filter of the present invention combines the operation of a fluidized bed filter with a slowly moving granular bed filter. Thus, in operation, the filtration bed of the filter of the present invention is mobile, homogenized and its surface is being renewed continuously.
- Unlike other mobile granular bed filters, the filter of the present invention has no internal or external mobile mechanical parts. This feature is advantageous since it avoids mechanical sealing and operation failures due to high temperatures and frequently chemically aggressive environments.
- Now referring to the drawings, more specifically to FIGS. 1, 2 and3 the present invention comprises a
cylindrical vessel 10 with a conical shape bottom 12. The vessel contains granular filtering material. Advantageously, the granular filtering material can be quartz, preferably 24 mesh size, or sand, preferably of high sphericity and preferably also 24 mesh size. Of course, other granular filtration material may also be used. - A
hot gas inlet 14 is operatively connected to bottom 12. A filteredgas outlet 16 is situated in the vertical wall ofvessel 10. It is to be understood that the number of gas inlets and outlets is a function of the size of the vessel. For vessels of diameter less than 1 m, 1-2 inlets and outlets are sufficient while for bigger vessels, up to 4 outlets are recommended. - During installation,
vessel 10 is moved into position while suspended onloop 18.Anchor plates 20 secure the vessel to a rigid holding structure (not shown). - Spent particulate material can be removed through
pipe 22. This removal can be assisted by backflushingpipes 24 which are connected to a compressed air or inert gas source. - Referring now to FIG. 4, there is shown a cross-sectional view of the inside of
vessel 10. -
Inlet 14 is provided with agas distribution plate 26 comprising a number oftuyeres 28 favoring equal gas distribution.Gas entering vessel 10 throughtuyeres 28 travels up atube 30 having on open top. Directly abovetube 30 istube 32, open at both ends.Tubes tubes tubes -
Tube 30 is fastened togas distribution plate 26.Tube 32 is fastened to the internal wall ofvessel 10 bysupport rods 34. - Although the preferred shape of
tubes tubes cylinders - The exact position of
gas outlet 16 including its height from the bottom of the vessel is a function of various parameters. These parameters include: the total height of the central fluid-bed tubes tubes - Referring now to FIG. 6, in operation, hot gas will enter through
tuyeres 28, travel uptube 30 and continue uptube 32. This will effectively siphon granular material uptube 32 and form a fluidized bed therein. As gas exits the top oftube 32, it will entrain the fluidized granular material which will fall down towards the bottom 12 ofvessel 10. This will create a constant recirculation of granular filtration material invessel 10. Gas exiting fromoutlet 16 will have had contact with granular material going uptube 32 and falling down aroundtube 32. It is to be understood that the dimensions ofcylinder 32 will need to be sufficient to ensure appropriate contact time between the gas and the filtering granules. The contact time will preferably be about 2 seconds. - It is to be noted that some of the granules resting in the bottom12 of
vessel 10 serve as a support material for the fluidized granules rather than directly participate in the filtration. - Thus, the novel hot gas filter uses an “impact” rather than ‘surface layer’ mechanism to filter particles of size down to 1 micron or less with high efficiencies. The entrained fluidized-bed column advantageously a) continuously renews the filtering media and b) homogenizes the bulk of the filtering media;
- The novel filter apparatus is advantageously equipped with an appropriate system of tubes, valves and automation instrumentation ensuring its continuous operation, regeneration cycles, and back flushes if need be. It is to be understood that tube diameters will be sufficiently large to avoid fouling and that inclination angles will also be selected to provide proper operation. The materials used for making the various parts of
filtration vessel 10 will be selected for their capacity to withstand erosion and high temperature regimes. Advantageously, portions of the filtration vessel exposed to high temperature will be lined with suitable insulating and refractory material. - Finally, as previously mentioned,
vessel 10 is provided with various back flushingpipes 24 bringing in back flushing air or inert gas pulses.Pipes 24 are connected togas outlet 16, the top ofvessel 10 and upstream ofgas inlet 12. The purpose of flushingpipes 24 is to periodically clean the inlets and outlets, when necessary. The frequency of these flushes is a function of the amount and nature of the material filtered out of the gas. In the worst cases one flush per day was found to be sufficient. - The apparatus of the present invention was tested on a pilot plant scale. Reference is now made to FIG. 7. The tests relate to the filtration of a producer gas to remove particles. The gas comes from a bubbling fluid bed gasifier fed with residual polyethylene. The hot gas received a pretreatment in a primary cyclone used to remove the coarser particles. The gasifier is fed with 30 kg of Polyethylene per hour and air at a stoichiometric ratio of 0,3. It operates at a temperature of about 760° C. and produces about 120Nm3 of producer gas/h. A slip stream of this gas, equal to about 10% of the main flow is diverted through the mobile fed filter, using a HIBON└ liquid ring suction/compression gas pump.
- The examples presented below illustrate four different tests:
- a) low sphericity fresh quartz as filtering media;
- b) high sphericity fresh Ottawa sand as filtering media;
- c) high sphericity regenerated Ottawa sand as filtering media;
- d) behavior of filter with time.
- Pilot tests were conducted at temperatures between 400 and 550° C. Higher temperatures (up to 850° C.) are possible.
- The tests showed that with high sphericity sands each operation-regeneration cycle was approximately 60 hours and consequently preferable over low sphericity sands where the operation-regeneration cycle was about 24 hours.
- To evaluate the filtration capabilities and efficiency of the filter, the producer gas was sampled upstream and downstream of the filter. For this purpose two identical isokinetic sampling trains depicted in FIG. 7 were used. These samplers allow for both particles and condensable tar evaluation. The particles are retained by a glass fiber filter operated at temperature above 400° C. This precaution was taken in order to avoid deposition of high molecular weight condensable tar which could be measured as particles and thus biasing the sampling results. In order to check the filtration efficiency as function of the filtration time dual samples were taken.
- Table 1 below summarizes the main parameters and results of these experiments.
TABLE 1 Tests with novel Granular Mobile Bed Filter Parameters Units Test 1 Test 2Test 3Test 4Tests Code NA-38 NA-47 NA-49 & 53 NA-49 & 53 Date 04/20/98 07/29/98 09/01/98 12/01/98 Duration (h) 13 55 52 52 Sampling time (h) 9 to 12 1 to 3 4 to 8 45-48 Sampling duration (h) 3 3 3.5 3 Temperature (° C.) 510 430 420 420 Gas flowrate (Nm3/h) 18 10 10 15 Pressure drop range (kPa) 6.8-24.5 5.1-23.8 8.2-26.9 8.2-26.9 Filtering media Fresh Quartz Fresh Ottawa Regen. Regen. (24 mesh) Sand (24 mesh) Ottawa sand Ottawa sand (24 mesh) (24 mesh) Particles load before (mg/Nm3) 2994 5412 2482 3945 Particles load after (mg/Nm3) 73 300 148 227 Particles removal (% w/w) 97.6 94.5 94.0 94.2 Efficiency -
Example of head pressure balance calculations Units PRESSURE LOSS ACROSS THE QUASI FIXED BED Granular media data Initial porosity (fixed bed) ε 0,39 Diameter Dp 7,00E-04 m 0,0276 in Nature Quartz 24 mesh Density Ps 2459 kg/m3 Test conditions Temperature T 20 ° C. Pressure P 103800 Pa Gas flow rate (normal conditions) Qn 2,000E + 01 Nm3/h Gas flow rate (actual conditions) Qa 0,0060 m3/s Mass velocity G 123,0 lb/h*ft2 Gas data Viscosity μ 1,80E-05 Pa.s Density pg 1,29E + 00 kg/m3 Solids density ps 2,46E + 03 kg/m3 Quasi fixed-bed data Diameter DF 0,23 M Length L 0,32 M Hypothesis 1 Gas velocity constant along the bed 2 Turbulent flow across the bed 3 K2 ∞ 150 (Ergun equation) 4 K4 ∞ 1,75 (Ergun equation) 5 Sphericity (y) 0,67 Preliminary Calculations Actual flow rate Qa 0,006 m3/s m/s s Gas Velocity V 0,136 Residence Time T 2,358 Pressure losses ΔP 3,5 Kpa (near three times than through the fixed bed) PRESSURE LOSS ACROSS THE QUASI FIXED BED Granular media data Initial porosity (fixed bed) ε 0,39 Diameter Dp 7,00E-04 m 0,0276 in Nature Quartz 24 mesh Density Ps 2459 kg/m3 Test conditions Temperature T 20 ° C. Pressure P 103800 Pa Gas flow rate (normal conditions) Qn 2,00E + 01 Nm3/h Gas flow rate (actual conditions) Qa 0,0060 m3/s Mass velocity G 123,0 lb/h*ft2 Gas data Viscosity μ 1,80E-05 Pa.s Density pg 1,29E + 00 kg/m3 Solids density ps 2,46E + 03 kg/m3 Fluid Bed Data Diameter Dlf 0,0762 m Length Llf 0,4 m Mass velocity at minimum fluidization Gmf 173,80 lb/h*ft2 Reynolds number Nre 6,49 Friction factor Fm 4 Shape factor _s 0,67 Void space factor at minimum Emf 0,39 fluidization Exponent N 1 Preliminary Calculations Actual flow rate Qa 0,0060 m3/s m/s s Gas Velocity V 1,3 Residence Time T 0,306 Pressure losses calculation Pressure losses ΔP 1,1 KPa - Advantageously, the filter of the present invention will be mounted in parallel with similar units. Hence, one filter may be temporarily decommissioned for maintenance purposes without interrupting the production of hot gas from the gasifier.
- Although the invention has been described above with respect with one specific form, it will be evident to a person skilled in the art that it may be modified and refined in various ways. It is therefore wished to have it understood that the present invention should not be limited in scope, except by the terms of the following claims.
Claims (10)
Applications Claiming Priority (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA2,268,376 | 1999-04-07 | ||
CA2268376 | 1999-04-07 | ||
CA2268376 | 1999-04-07 | ||
ES9901970A ES2172367B1 (en) | 1999-04-07 | 1999-09-02 | MOBILE GRANULAR MILK FILTRATION DEVICE FOR HOT GAS CONDITIONING |
ES9901970 | 1999-09-02 | ||
PCT/CA2000/000389 WO2000061263A1 (en) | 1999-04-07 | 2000-04-07 | Mobile granular bed filtration apparatus for hot gas conditioning |
Related Parent Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CA2000/000389 Continuation WO2000061263A1 (en) | 1999-04-07 | 2000-04-07 | Mobile granular bed filtration apparatus for hot gas conditioning |
Publications (2)
Publication Number | Publication Date |
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US6436161B1 US6436161B1 (en) | 2002-08-20 |
US20020116908A1 true US20020116908A1 (en) | 2002-08-29 |
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ID=25680886
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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US09/972,684 Expired - Lifetime US6436161B1 (en) | 1999-04-07 | 2001-10-05 | Mobile granular bed filtration apparatus for hot gas conditioning |
Country Status (7)
Country | Link |
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US (1) | US6436161B1 (en) |
EP (1) | EP1169108B1 (en) |
AT (1) | ATE260132T1 (en) |
AU (1) | AU3799700A (en) |
DE (2) | DE60008511D1 (en) |
ES (1) | ES2173819T3 (en) |
WO (1) | WO2000061263A1 (en) |
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US20060223184A1 (en) * | 2005-04-05 | 2006-10-05 | Frutos Anthony G | Supports useful in incorporating biomolecules into cells and methods of using thereof |
ES2539761T3 (en) | 2006-04-05 | 2015-07-03 | Woodland Biofuels Inc. | System and method to convert biomass into ethanol through synthesis gas |
KR100914887B1 (en) * | 2007-11-09 | 2009-08-31 | 한국에너지기술연구원 | Tapered Regeneration Reactor Of CO2 Capture System using Dry-sorbent |
ES2399677T3 (en) * | 2010-06-16 | 2013-04-02 | Siemens Aktiengesellschaft | Installation with gas turbine and steam turbine, and the corresponding method |
PL3099398T3 (en) * | 2014-01-31 | 2018-01-31 | Amec Foster Wheeler Energia Oy | A method of and a scrubber for removing pollutant compounds from a gas stream |
EP4355688A1 (en) * | 2021-06-17 | 2024-04-24 | SOCPRA - Sciences et Génie s.e.c. | Carbon sequestration system and process and pyrolysis process and reactor |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4017278A (en) * | 1974-09-30 | 1977-04-12 | Combustion Power Company, Inc. | Method and apparatus for removing finely divided solids from gas |
CH614128A5 (en) * | 1976-05-06 | 1979-11-15 | Gimag Ag | |
US4157959A (en) * | 1977-08-15 | 1979-06-12 | Kansas State University Research Foundation | Method of filtration using convertible (semifluidized) beds |
US4191544A (en) * | 1978-03-17 | 1980-03-04 | The Babcock & Wilcox Company | Gas cleaning apparatus |
US6290752B1 (en) * | 1998-10-22 | 2001-09-18 | Von Roll Umwelttechnik Ag | Device and process for adsorption or chemisorption of gaseous constituents from a gas flow |
-
2000
- 2000-04-07 AT AT00916729T patent/ATE260132T1/en not_active IP Right Cessation
- 2000-04-07 EP EP00916729A patent/EP1169108B1/en not_active Expired - Lifetime
- 2000-04-07 AU AU37997/00A patent/AU3799700A/en not_active Abandoned
- 2000-04-07 DE DE60008511T patent/DE60008511D1/en not_active Expired - Lifetime
- 2000-04-07 WO PCT/CA2000/000389 patent/WO2000061263A1/en active IP Right Grant
- 2000-04-07 DE DE1169108T patent/DE1169108T1/en active Pending
- 2000-04-07 ES ES00916729T patent/ES2173819T3/en not_active Expired - Lifetime
-
2001
- 2001-10-05 US US09/972,684 patent/US6436161B1/en not_active Expired - Lifetime
Also Published As
Publication number | Publication date |
---|---|
ES2173819T1 (en) | 2002-11-01 |
ATE260132T1 (en) | 2004-03-15 |
DE1169108T1 (en) | 2002-10-02 |
WO2000061263A1 (en) | 2000-10-19 |
AU3799700A (en) | 2000-11-14 |
EP1169108A1 (en) | 2002-01-09 |
ES2173819T3 (en) | 2004-10-01 |
DE60008511D1 (en) | 2004-04-01 |
EP1169108B1 (en) | 2004-02-25 |
US6436161B1 (en) | 2002-08-20 |
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