WO1996040436A1 - Procede d'elimination des particules indesirables contenues dans un gaz - Google Patents

Procede d'elimination des particules indesirables contenues dans un gaz Download PDF

Info

Publication number
WO1996040436A1
WO1996040436A1 PCT/US1995/009746 US9509746W WO9640436A1 WO 1996040436 A1 WO1996040436 A1 WO 1996040436A1 US 9509746 W US9509746 W US 9509746W WO 9640436 A1 WO9640436 A1 WO 9640436A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas stream
adhesive
particles
undesired particles
phosphoric acid
Prior art date
Application number
PCT/US1995/009746
Other languages
English (en)
Inventor
Michael Dean Durham
Richard John Schlager
Timothy George Ebner
Robin Michele Stewart
Cynthia Jean Bustard
Sharon Sjostrom
David E. Hyatt
Original Assignee
Ada Technologies, Inc.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Ada Technologies, Inc. filed Critical Ada Technologies, Inc.
Priority to EP95929354A priority Critical patent/EP0831971A4/fr
Priority to AU32737/95A priority patent/AU3273795A/en
Publication of WO1996040436A1 publication Critical patent/WO1996040436A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D51/00—Auxiliary pretreatment of gases or vapours to be cleaned
    • B01D51/02—Amassing the particles, e.g. by flocculation
    • B01D51/04—Amassing the particles, e.g. by flocculation by seeding, e.g. by adding particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D51/00—Auxiliary pretreatment of gases or vapours to be cleaned
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
    • B03C3/01—Pretreatment of the gases prior to electrostatic precipitation
    • B03C3/013—Conditioning by chemical additives, e.g. with SO3

Definitions

  • the present invention is a method and apparatus for removing undesired particles, such as fly ash, from gas streams. More particularly, the present invention embodies an improved approach for removing such undesired particles by selectively introducing adhesives into the gas stream.
  • Electrostatic precipitators and filtration systems are two commonly used devices for the removal of undesired particles from the gas streams produced by plants and refineries.
  • undesired particles refers to any particulate matter that is desired to be removed from a gas stream.
  • undesired particle-laden gases pass negatively charged corona electrodes which impart a negative charge to the undesired particles.
  • the charged particles then migrate towards positively charged collection plates alternately positioned between the corona electrodes.
  • the undesired particles accumulate on the collection plates and are removed by various techniques, including sonic horn blasts or rapping of the collection plates.
  • Electrostatic precipitators may employ one stage for both the charging and collection of undesired particles or multiple stages with the charging and collection being done in different stages.
  • Filtration systems such as baghouses, remove undesired particles from gas streams by passing the gas streams through large filters.
  • the filters have pores large enough to pass the gases in the gas stream but small enough to prevent passage of undesired particles.
  • the filters may be of a fabric, metal, paper or ceramic construction.
  • the undesired particles can be removed from a filter by many techniques including shakers, pulse jets, or reverse gas flow.
  • efficiency and cost are critical considerations. The efficiency of electrostatic precipitators is decreased by undesired particle reentrainment into a gas stream during the removal of undesired particles from the collection plates.
  • ammonia gas and sulfur trioxide may be injected into a gas stream to form ammonium sulfates on the surfaces of undesired particles.
  • This approach has several drawbacks.
  • a possible product of the reaction between ammonia gas and sulfur gas is ammonium bisulfate which fouls the electrostatic precipitator or filtration system components. Such component fouling impairs the operation of the components and increases undesired particle emissions and unit operating costs.
  • the use of ammonia gas in the gas stream may require additional downstream gas purification steps to remove unreacted ammonia gas from the gas stream prior to discharge.
  • Ammonia gas is known to create environmental damage and increase the opacity of the discharged gas stream.
  • odor associated with ammonia may also cause problems in the disposal of the undesired particles after collection.
  • Another approach to reduce undesired particle emissions is to employ a wetted collection surface.
  • wet systems a liquid, typically water, is supplied to the collection surface to enhance undesired particle collection and reduce reentrainment. Unless expensive materials are employed, however, components of wet systems can suffer high corrosion rates due to acid formation.
  • a method for removing undesired particles from a gas stream including the steps of (i) contacting a gas stream containing undesired particles and water vapor with an adhesive composition; (ii) collecting the undesired particles and the adhesive composition on at least one collection surface to form an agglomerate at a temperature greater than the condensation temperature of the water vapor in the gas stream; and (iii) removing the agglomerate from the collection surface.
  • undesired particle refers to any particle that one desires to remove from the gas stream, regardless of the intrinsic value of the particle.
  • Adhesive refers to any substance, inorganic or organic, natural or synthetic, that is capable of adhering or bonding other substances together by surface attachment.
  • Agglomerate refers to a cluster or accumulation of undesired particles and adhesive particles.
  • Condensation temperature refers to the temperature at which a given vapor component of a gas stream condenses into a liquid under ambient pressure.
  • the adhesive in the composition is nontoxic and substantially odorless.
  • An adhesive is typically deemed “nontoxic” if the presence of the adhesive in the resultant agglomerate does not cause the agglomerate to be environmentally unacceptable under the standards and procedures set forth in the Toxicity Characteristic Leaching Procedure ("TCLP") established by the United States Environmental Protection Agency.
  • the TCLP provides analysis procedures for waste materials to detect environmentally unacceptable levels of substances, including inorganic elements, volatile organic compounds, and semi-volatile organic compounds.
  • the TCLP specifies the maximum acceptable concentration for such substances.
  • An adhesive is deemed to be "odorless” if the presence of the adhesive in the agglomerate cannot be detected by the human nose.
  • Preferred adhesives are selected from the group consisting of gums, cellulose, vinyls, and derivatives and mixtures thereof. More preferably, the adhesive should be selected from the group consisting of xanthan gum, carboxymethyl cellulose and mixtures thereof.
  • xanthan gum carboxymethyl cellulose and mixtures thereof.
  • “gum” refers to a carbohydrate high polymer that is insoluble in alcohol and other organic solvents, but generally soluble or dispersible in water.
  • Cellulose refers to a natural carbohydrate high polymer (polysaccharide) containing anhydroglucose units joined by an oxygen linkage to form long molecular chains.
  • the adhesive composition may include a surfactant to enhance agglomerate formation.
  • the adhesive composition may also include a dispersant to control agglomerate porosity, especially in filtration plant applications.
  • surfactant refers to any substance that alters the surface tension of another substance.
  • Dispersant refers to any substance that influences the distance between undesired particles in the agglomerate.
  • the adhesive composition is preferably introduced into the gas stream in a dispersed and uniform manner. In this regard, the adhesive composition can be atomized upon introduction utilizing a "carrier fluid" component.
  • the carrier fluid may be a gas or liquid, such as water, that is a solvent for the adhesive and that vaporizes in the gas stream.
  • a substantial portion of the carrier fluid separates from the adhesive by vaporization prior to reaching the collection surface. Upon separation, dispersed particles of the adhesive will remain in the gas stream with the undesired particles. Upon contact with the collection surface, the adhesive particles and the undesired particles to be removed form the agglomerate.
  • the temperature of the collection surface in the collecting step is greater than both the condensation temperature of the water vapor in the gas stream and any vaporized carrier fluid.
  • a "dry system” refers to a system that employs a substantially dry collection surface (i.e., having substantially no liquid in contact therewith) for undesired particles.
  • the gas stream may be advantageously deflected, as may be desired, prior to contacting the collection surface to achieve, for example, uniform incidence of the particles on the collection surface, thereby yielding an agglomerate of a more uniform thickness.
  • the agglomerate of undesired particles and adhesive particles may be removed from the collection surface, collected in a hopper and removed from the unit. Removal may be accomplished by vibration of the collection surface, removing the collection surface from the collection zone, or contacting the collection surface with a reverse gas stream having a direction of flow substantially opposite to the gas stream.
  • an apparatus for undesired particle removal includes (i) a housing; (ii) an inlet and outlet for the gas stream; (iii) an injection apparatus to inject an adhesive composition into the gas stream; and (iv) one or more collection surfaces supportably positioned within the housing to collect both the undesired particles to be removed and adhesive particles which, in turn, form an agglomerate on the collection surface.
  • the apparatus may include a plurality of collection surfaces and one or more hoppers to collect the agglomerate that is removed from the collection surface.
  • the adhesive injection apparatus is preferably a plurality of dispersion devices (e.g., nozzles) positioned within and/or across the gas stream to uniformly disperse the adhesive composition into the gas stream.
  • the adhesive injection apparatus may be advantageously located upstream of the collection surface at a distance sufficient for a substantial portion of any carrier fluid, preferably about 90% or more by weight, to separate by vaporization from the particles before the particles contact the collection surface.
  • a deflecting apparatus may be provided to deflect and uniformly distribute the gas stream prior to contacting the collection surfaces so as to improve the uniformity of agglomerate build-up on the collection surfaces.
  • Such deflecting apparatus may comprise, for example, a plurality of selectively adjustable baffles (e.g., horizontally, vertically, and/or angularly) disposed across the gas stream.
  • the apparatus may include a power supply; at least one electrode connected to the negative terminal of the power supply and positioned relative to the input gas stream to impart a charge to the undesired particles to be removed and the adhesive particles; and at least one collection surface connected to the positive terminal of the power supply and positioned parallel to the flow of the gas stream.
  • electrostatic injection nozzles such as charged-fog nozzles or those employed in many paint sprayers may be employed to inject the adhesive composition.
  • the use of such nozzles may serve to impart additional charge to adhesive composition droplets upon atomization, thereby increasing the collection of adhesive particles on the collection surfaces, particularly if an anionic or nonionic adhesive is utilized.
  • the carrier fluid in the adhesive composition may also be advantageously utilized to cool the gas stream and undesired particles contained therein.
  • the predetermined injection rate is preferably selected to achieve a desired degree of cooling, while yet allowing for a substantial portion of the carrier fluid to vaporize before reaching the collection surface. It is believed that such an approach may have particular application in low- sulphur content coal burning facilities in view of the relatively low acid dew point of the resulting gas streams.
  • the collection surface may be a filter located transverse to the direction of flow of the gas stream to separate the undesired particles and adhesive particles from the gas stream.
  • a filter located transverse to the direction of flow of the gas stream to separate the undesired particles and adhesive particles from the gas stream.
  • Such filter may be of ceramic, fabric, paper or metal construction.
  • the adhesive injection apparatus and/or filter are selected such that a substantial portion of the adhesive particles dispersed into the gas stream are larger than the pore size of the filter.
  • a process for removing undesired particles from a gas stream includes the following steps: (i) contacting a gas stream with a plurality of droplets comprising phosphoric acid and a carrier fluid, with the droplets having a first Sauter Mean Diameter ranging from about 20 to about 150 microns; (ii) separating the carrier fluid from the droplets, such as by evaporation, to reduce the droplet size to a second Sauter Mean Diameter less than said first Sauter Mean Diameter; and (iii) collecting the undesired particles and phosphoric acid on a collection surface to form an agglomerate.
  • the second Sauter Mean Diameter ranges from about 1 to about 10 microns.
  • the preferred concentration of phosphoric acid in the gas stream ranges from about 1 to about 10 lb/ton of undesired particles.
  • the residence time of the droplets in the gas stream before the collecting step preferably ranges from about 0.25 to about 2.00 seconds.
  • a process in a filtration system embodiment, first contacts a gas stream with a caustic acid and/or salt or precursor thereof, preferably a phosphorous-containing material, and second contacts the undesired particles with a filtration surface to form an agglomerate of undesired particles on the filtration surface.
  • the caustic acid and/or salt or precursor thereof, and particularly the phosphorous-containing material cause an increase in the cohesiveness of the undesired particles and thereby facilitate agglomerate formation.
  • the phosphorous-containing material preferably includes phosphoric acid, elemental phosphorous, and precursors and ixtures thereof.
  • the phosphorous-containing material preferably causes the deposition of phosphoric acid on the undesired particles.
  • a process in a hot-side electrostatic precipitating system embodiment, first contacts a gas stream with a resistivity reduction agent and collects the undesired particles and resistivity reduction agent on a collection surface of the electrostatic precipitating device to form an agglomerate.
  • the temperature of the gas stream at the electrostatic precipitating device is no less than about 600°F.
  • the electrostatic precipitating device is located upstream of the air preheater in utility applications.
  • the resistivity reduction agent preferably is a caustic acid and more preferably is phosphoric acid and precursors thereof.
  • the preferred phosphoric acid concentration ranges from about 0.1 to about 1.0% by weight of the undesired particles in the gas stream.
  • Electrostatic precipitator and filtration system efficiency are increased by less reentrainment of undesired particles.
  • the adhesive particles increase the force of attraction between undesired particles in the agglomerate of undesired particles and adhesive particles.
  • the resulting agglomerate of undesired particles and adhesive particles on the collection surface, or dust cake is not only more cohesive but also more porous.
  • the cohesiveness of the dust cake reduces fragmentation and undesired particle reentrainment during dust cake removal.
  • the resistivity of the resulting dust cake can also be reduced through the use of phosphoric acid resulting in better collection of the undesired particles, relative to untreated particles.
  • the particle cohesion produces increased porosity of the dust cake which reduces the pressure drop across the filter (and therefore requires less frequent filter cleanings) .
  • the cohesiveness of the dust cake also reduces "bleeding" of very fine undesired particles through the filter pores caused by compaction of undesired particles on the filter surface, thus increasing efficiency.
  • the present invention is also particularly advantageous as it preferably yields a "dry system,” which has numerous advantages relative to a wet system.
  • the method not only employs low cost components and additives that improve the efficiency of new electrostatic precipitators and filtration systems but also is readily adaptable to existing units. Further advantages will be apparent to those skilled in the art.
  • Fig. 1 is a perspective view of a first embodiment of the present invention in an electrostatic precipitator
  • Fig. 2 is a cut away view along line A-A of Fig. 1 showing the adhesive injection device spraying droplets of an adhesive composition into the gas stream
  • Fig. 3 is a side view of a collection plate showing an accumulation of adhesive particles and undesired particles on the collection plate;
  • Fig. 4 is a perspective view of a second embodiment of the present invention in a filtration system
  • Fig. 5 is a cut away view along line B-B of Fig. 4 showing an accumulation of adhesive particles and undesired particles on the filter surface;
  • Fig. 6 is a graph showing the relationship between particle temperature and particle resistivity for typical flyash particles
  • Fig. 7 is a plot of relative phosphoric acid concentration (based on a percent by weight of additive relative to undesired particles in the gas stream) against resistivity for a gas stream having a temperature of 300°F;
  • Fig 8 is a plot of relative phosphoric acid concentration (based on a percent by weight of additive relative to undesired particles in the gas stream) against rate of agglomerate formation
  • Fig. 9 is a plot of relative phosphoric acid concentration (based on a percent by weight of additive relative to undesired particles in the gas stream) against resistivity
  • Fig. 10 is a plot of phosphoric acid concentration (based on a percent by weight of additive relative to undesired particles in the gas stream) against resistivity
  • Fig. 11 is a plot of phosphoric acid concentration (based on a percent by weight of additive relative to undesired particles in the gas stream) against resistivity under hot-side conditions.
  • Figs. 1 and 2 depict a first embodiment of the present invention as implemented in an electrostatic precipitator for removal of undesired particles such as fly ash from a gas stream.
  • the electrostatic precipitator comprises housing assembly 6, precipitating assembly 8, and adhesive injection assembly 10.
  • the housing assembly 6 includes an input duct 12, one or more input plenums 14, shell 16, one or more hoppers 18, one or more output plenums 20, and output duct 22.
  • the precipitating assembly 8 includes a plurality of sections 24.
  • Each section 24 includes a plurality of alternately disposed discharge electrodes 26 and collection plates 28, a corresponding plurality of electrical conductors 30, and an interconnected power supply 32.
  • the negative and positive terminals of the power supply 32 are connected to the discharge electrodes 26 and collection plates 28, respectively.
  • the adhesive injection assembly 10 includes a reservoir (not shown) and an interconnected feed line 34 and plurality of nozzles 37. As will be appreciated, the gas stream may be contacted with an adhesive composition continuously or intermittently and by many different I
  • Adhesive injection assembly 10 achieves contacting by atomizing a composition comprising a carrier fluid and an adhesive into the gas stream 36 in the form of droplets 38. Atomization may be realized by a number of different methodologies, including spraying the composition through a nozzle. To enhance charging of the droplets, particularly if an anionic or nonionic adhesive is employed, electrostatic injection nozzles may be utilized. While preferred, a carrier fluid is not required to disperse adhesive particles in gas stream 36. By way of example, adhesive particles 40 may be simply dripped into gas stream 36 by a suitable device (e.g., drip emitters).
  • a suitable device e.g., drip emitters
  • adhesive injection assembly 10 should be located upstream of the precipitating assembly 8.
  • the adhesive injection assembly 10 is disposed so as to provide a sufficient distance between the adhesive injection assembly 10 and the nearest of the collection plates 28 such that, prior to contacting the nearest collection plate 28, a substantial portion of the carrier fluid, preferably about 90% or more by weight, has separated from the adhesive and a substantially uniform dispersion of adhesive particles 40 across the gas stream 36 has been attained.
  • adhesive injection assembly 10 may be advantageously located in input duct 12 with nozzles 37 evenly spaced across and within the gas stream 36 as illustrated.
  • Gas stream 36 may be deflected by baffles 60 prior to contacting collection plates 28 to achieve a more uniform incidence of undesired particles 35 and adhesive particles 40 on collection plates 28, thereby yielding an agglomerate of a more uniform thickness on collection plates 28.
  • Adhesives utilized in the present invention should be nontoxic, substantially odorless, and soluble in a suitable fluid carrier, such as water. Further, the adhesives preferably should be organic compounds, such as polymers. Preferred classes of polymers are gums, cellulose, vinyls and derivatives and mixtures thereof. For polymer adhesives, generally, the desired droplet size 38 upon injection of the adhesive composition via nozzles 37 is from about 10 to about 100 micrometers.
  • gas stream 36 containing undesired particles 35 is passed through input duct 10 and input plenums 14 into electrostatic precipitator shell 16.
  • gas stream 36 Prior to entering electrostatic precipitator shell 16, gas stream 36 passes adhesive injection assembly 10.
  • Adhesive injection assembly 10 disperses droplets 38 containing adhesive particles 40 into gas stream 36.
  • the contacting of the adhesive with the gas stream may be facilitated by use of a carrier fluid.
  • the carrier fluid may be any gas or liquid that is nontoxic, substantially odorless, and capable of transporting the adhesive over a desired distance.
  • the carrier should be a solvent for the adhesive utilized.
  • the carrier fluid is a liquid, such as water, that readily vaporizes at the temperature and pressure to which the gas stream is subjected.
  • the specific desired concentration of the adhesive in the liquid carrier fluid primarily depends on the identity of the carrier fluid, the desired size and amount of adhesive particles 40 to be introduced into the gas stream 36, and the size of the droplet 38 to be injected in the gas stream 36.
  • the concentration of adhesive in the carrier fluid e.g., water
  • the concentration of adhesive in the carrier fluid preferably ranges from about .005% to about 10% by volume, and more preferably from about .05% to about 1% by volume.
  • Lower concentrations may for example be employed in low-sulphur content coal burning applications where, in addition to adhesive particle dispersal, the carrier fluid is advantageously employed to cool the gas stream, thereby reducing the resistivity of the agglomerate and the incidence of sparkover.
  • the adhesive composition should be thoroughly mixed prior to injection into gas stream 36.
  • the specific desired concentration of the adhesive particles 40 to be dispersed in gas stream 36 is established primarily based upon the concentration and size distribution of undesired particles 35 in gas stream 36, the tacticity of the adhesive, and the desired concentration of undesired particles 35 in gas stream 36 after treatment. In general, however, the concentration of adhesive particles 40 relative to undesired particles 35 in gas stream 36 preferably ranges from about .01% to about 1% by weight.
  • droplets 38 are carried downstream by gas stream 36. As the droplets 38 are carried downstream, droplets 38 decrease in size due to vaporization of the liquid carrier fluid and become smaller droplets 38a. As the liquid carrier fluid vaporizes, adhesive particles 40 formerly contained in droplets 38, 38a, will be dispersed and entrained in gas stream 36 along with undesired particles 35. As noted, about 90% or more by weight of the liquid carrier fluid in a given droplet 38 has preferably evaporated before adhesive particles 40 contact collection plates 28.
  • the desired size distribution of adhesive particles 40 produced after vaporization of the liquid carrier fluid is a function of several factors including the size distribution of undesired particles 35, the density of the adhesive, and the viscosity of the adhesive. Preferably, however, the size of the adhesive particles 40 ranges from about 1 to about 10 micrometers.
  • the vaporization time for the liquid carrier fluid in a droplet 38 primarily depends upon the size of droplet 38, the volatility of the liquid carrier fluid, and the temperature, pressure and composition of the gas stream 36. In general, however, the preferable vaporization time for the liquid carrier fluid should be less than about two seconds and in most cases less than about 1 second.
  • the adhesive particles 40 contact collection plates 28.
  • the temperature of both the collection plate surface and the agglomerate of undesired particles 35 and adhesive particles 40 collected on the surface is preferably above the condensation temperature of water vapor in gas stream 36. Further, the temperature of both the collection plate surface and the agglomerate is preferably above the condensation temperature of the vaporized liquid carrier fluid.
  • Gas stream 36 containing undesired particles 35 and dispersed adhesive particles 40 enters electrostatic precipitator shell 16.
  • Discharge electrodes 26 impart a negative electrical charge to undesired particles 35 and adhesive particles 40.
  • the negatively charged particles adhere to the positively charged collection plates 28.
  • Fig. 3 is a side view of a portion of a collection plate 28 that contains an agglomerate of undesired particles 35 and adhesive particles 40. As depicted, after contacting collection plate 28 adhesive particles 40 flow into the interparticle gaps between undesired particles 40, thereby yielding the desired agglomerate.
  • Surfactants may be included in the adhesive composition and, upon contacting the collection plates, will serve to reduce the surface tension of adhesive particles 40 and increase the ability of the adhesive to fill the gaps between undesired particles 35.
  • Useful surfactants in this regard include alkyl aryl polyether and alkyl phenyl- hydroxypolyoxyethylene.
  • Fig. 3 further depicts void spaces 42 which result from the cohesion between undesired particles 35 and adhesive particles 40.
  • the resulting dust cake 44 is a porous agglomerate of undesired particles 35 and adhesive particles 40.
  • the porosity of dust cake 44 may be desirably increased by the addition of a dispersant to the adhesive composition employed.
  • Useful dispersants in this regard include phosphates, such as trisodium phosphate, tetrasodium phosphate, and sodium hexamitaphosphate.
  • the bonding mechanism between the adhesive particles 40 and undesired particles 35 is mechanical and/or ionic in nature.
  • mechanical bonding it is believed that longer polymer chains more efficiently attract and entrap fine undesired particles 35 when compared to shorter polymer chains in the adhesive molecules. For this reason, higher molecular weight adhesive polymers more effectively form clumps of fines in the dust cake 44 than lower molecular weight adhesive polymers.
  • ionic bonding it is believed that the polarity of the polymer impacts the ability of the adhesive molecules to bond to undesired particles 35.
  • dust cake 44 can be removed from collection plate 28 by many techniques, including rapping of the collection plate 28 and sonic horns.
  • the preferred methodology for dust cake removal involves vibration of the collection plate 28. When collection plate 28 is vibrated, dust cake 44 separates from collection plate 28 in large sheets and falls into hoppers 18 for disposal. It is believed that adhesive particles 40 increase the attractive force between undesired particles 35. The increased interparticle forces of attraction induce a high degree of cohesiveness in dust cake 44. The high dust cake cohesiveness is thought to prevent the release of finer undesired particles during dust cake removal.
  • the cohesiveness of dust cake 44 yields many advantages.
  • the decreased incidence of undesired particle reentrainment in the present invention reduces particulate emissions relative to conventional electrostatic precipitators.
  • Second, the cohesive sheets also reduce problems of conventional electrostatic precipitators from handling and storing loosely consolidated, fine undesired particles. Undesired particles 35 are typically only about 10 microns in size.
  • the vaporization of the majority of the liquid carrier fluid before dust cake formation produces a solid mass that avoids problems commonly associated with slurry handling and disposal.
  • a second embodiment of the present invention is a filtration system for removal of undesired particles, such as fly ash from a gas stream.
  • a filtration system 45 includes a housing assembly 46, filtrating assembly 48, and adhesive injection assembly 10.
  • Housing assembly 46 includes an input duct 50, filtration shell 52, output duct 54, and hoppers 56.
  • Filtrating assembly 48 includes a plurality of filters 58 suspended from a header (not shown) .
  • a support apparatus such as a cage, may be used to prevent deflation of filters 58.
  • adhesive injection assembly 10 includes a reservoir (not shown), feed line 34, and nozzles 37. In operation, gas stream 36 enters the filtration shell 52 through the input duct 50.
  • adhesive composition droplets 38 are injected into gas stream 36.
  • a substantial portion of the liquid carrier fluid preferably about 90% or more by weight, in droplets 38 has vaporized, and adhesive particles 40 are dispersed.
  • Filters 58 pass the gaseous components of gas stream 36 but remove undesired particles 35 and adhesive particles 40.
  • filters 58 may be of ceramic, fabric, paper or metal construction.
  • undesired particles 35 and adhesive particles 40 collect on the exterior of filter 58.
  • void spaces 42 are formed as undesired particles 35 and adhesive particles 40 collect on the exterior of filter 58.
  • void spaces 42 substantially reduce the incidence of undesired particles 35 blocking the filter pores.
  • blockages cause a large pressure drop across the filter and necessitate frequent removal of dust cake 44 from filter 58.
  • the porous dust cakes 44 of the present invention reduce the pressure drop across filters 58 and therefore filters 58 require less frequent cleanings. Accordingly, the present invention has a lower incidence of undesired particle reentrainment in gas stream 36 than conventional filtration plants.
  • filters 58 include shaker-cleaning filters, shake-deflate filters, sonic- horns, pulse-jet-cleaned filters, and reverse-air-cleaned filters.
  • a mechanism for cleaning the filters is vibration and the dust cake 44 falls into hoppers 56 for collection.
  • Filters 58 may also be removably mounted to the header so that they may be removed, cleaned, and reinstalled.
  • dust cake 44 facilitates the dust cake's removal. As a result of the increased interparticle cohesion induced by adhesive particles 40, dust cake 44 remains in consolidated chunks after removal. The formation of consolidated chunks of dust cake 44 simplifies the handling and storing of undesired particles when compared to conventional filtration systems.
  • gas stream 36 flows from the filtration shell 52 to output duct 54 for additional treatment or disposal.
  • the additive is the inorganic compound, phosphoric acid, which increases the cohesiveness of undesired particles and decreases undesired particle resistivity.
  • Phosphoric acid is relatively inexpensive compared to many other additives. It not only improves particle cohesion on the collection plates and filters, as noted above for organic adhesives, but also reduces the resistivity of the undesired particles 35, thereby further improving the particle removal efficiency of the electrostatic precipitator. The reduced resistivity reduces the incidence of sparkover in an electrostatic precipitator resulting in increased electric field strengths and current densities.
  • Phosphoric acid can also be used to improve undesired particle collection efficiencies in undesired particle collection systems having nozzle systems already disposed in the gas stream, such as manufacturing facilities in the metallurgical industry.
  • the phosphoric acid reacts with chemical compounds in the gas stream and/or undesired particles to form a hydrophilic material. It is believed that the hydrophilic material reacts with water in the gas stream to form hydrates. The hydrated compounds not only reduce undesired particle resistivity but also increase undesired particle cohesiveness.
  • the effectiveness of droplets of phosphoric acid in reducing undesired particle emissions is surprising and unexpected. As noted below, phosphoric acid has virtually no vapor pressure until around 1,400 to 2,000°F and therefore will condense at the gas stream temperatures commonly encountered in utility and other applications.
  • the specific desired concentration of the phosphoric acid in the liquid carrier fluid preferably ranges from about 0.1 to about 5.0% by volume, more preferably from about .10 to about 2.0% by volume, and most preferably from about .10 to about 1.5% by volume.
  • the preferred carrier fluid has a boiling point less than the temperature of the gas stream to ensure rapid evaporation of the carrier fluid from the phosphoric acid as described above in connection with the adhesive composition.
  • the preferred carrier fluid is water.
  • the phosphoric acid is preferably thoroughly mixed with the carrier fluid to form a fluid composition before injection into the gas stream 36.
  • an adhesive is included in the amounts noted above.
  • phosphoric acid is a caustic acid
  • the injection of the acid upstream of the air preheater can result in undesired particle deposits on the air preheater surfaces which can gum up the preheater and decrease the amount of heat transferred to the boiler.
  • the reduced heat transfer can decrease the efficiency of the boiler.
  • the droplets 38 Preferably, before separation of the carrier fluid from the adhesive the droplets 38 have a Sauter Mean Diameter ranging from about 20 to about 100 microns and more preferably from about 20 to about 50 microns.
  • the droplets After separation of the carrier fluid from the phosphoric acid, the droplets have a Sauter Mean Diameter preferably ranging from about 1 to about 10 microns. Droplets in this size range will be entrained in the gas stream and not settle out of the gas stream on the input duct and other metal surfaces.
  • the nozzles 37 of the adhesive injection assembly 10 are preferably dual fluid nozzles.
  • a pressurized gas such as air or steam, is intermixed with the fluid composition containing the phosphoric acid at the injection interface to form atomized droplets 38 of an extremely small size.
  • the small droplets are injected a sufficient distance upstream of the electrostatic precipitator or baghouse to permit effective conditioning of the gas stream.
  • the residence time of the droplets in the gas stream before contacting the electrostatic precipitator or baghouse ranges from about 0.25 to about 2.00 seconds.
  • the droplets should be substantially uniformly distributed throughout the input duct for best results. This result is effectuated by proper placement of the nozzles 37 in the input duct. It is also important to position the nozzles 37 such that the droplet dispersion pattern does not overlap with adjacent metal surfaces, such as the input duct.
  • the ability of the phosphoric acid to condition the undesired particles is not particularly temperature dependent. For best results, however, it is preferred that the gas stream temperature range between about 212 to about
  • the fluid composition is preferably not heated before injection into the gas stream 36.
  • the droplets 38 absorb thermal energy from the gas stream 36 and thereby act as a heat sink.
  • the subsequent cooling of the gas stream 36 can further reduce the resistivity of the agglomerate and the incidence of sparkover for electrostatic precipitators.
  • the concentration of phosphoric acid in the input duct depends upon the type of particle removal device.
  • the amount of phosphoric acid used in the gas stream preferably ranges from about 1 to about 10 lb/ton of undesired particles.
  • the amount of phosphoric acid used in the gas stream preferably ranges from about 0.5 to about 6.0 lb/ton of undesired particles.
  • the phosphoric acid is preferably contacted with the gas stream as a liquid and not as a vapor. Vaporized phosphoric acid is likely to condense on the input duct and other metal surfaces, causing corrosion and gumming up equipment.
  • phosphoric acid has virtually no vapor pressure until around 1400 to 2000°F and therefore will condense at the gas stream temperatures commonly encountered in utility and other applications (e.g., 180 to 800°F) .
  • Vaporized phosphoric acid is much more sensitive to the surface chemistry of the undesired particles than droplets of a fluid composition containing phosphoric acid.
  • droplets of the fluid composition are not as sensitive to surface chemistry.
  • the droplets of the fluid composition readily spread out through the agglomerate due to capillary forces.
  • Another approach to contacting phosphoric acid with the undesired particles is to combust phosphorous and inject vaporized phosphorous into the gas stream.
  • the gas stream has a temperature of preferably no less than about 350, more preferably no less than about 400, and most preferably no less than about 450°F at an electrostatic precipitating device and is contacted with a resistivity reduction agent and, optionally, a carrier fluid.
  • a resistivity reduction agent is any additive that causes a reduction in undesired particle resistivity in the surface conduction operating region. This region lies to the left of the critical temperature as illustrated in Fig. 6.
  • the resistivity reduction agent and precursors and mixtures thereof preferably include caustic acids and salts thereof, and more preferably phosphoric acid and precursors and mixtures thereof.
  • the resistivity reduction agent is substantially free of ammonia and sodium.
  • the preferred concentration of the phosphoric acid in the gas stream preferably ranges from about 0.1 to about 1.0% by weight of the undesired particles and more preferably is about 0.5 weight percent of the undesired particles in the gas stream.
  • This embodiment is particularly applicable to hot-side electrostatic precipitating devices in utility applications which operate at gas stream temperatures typically in excess of 1500°F and more typically in excess of 600°F.
  • Such devices can exhibit back corona tendencies in the agglomerate located on the collection plates. While not wishing to be bound by any theory, it is believed that such back corona tendencies result from the increase in undesired particle resistivities caused by prolonged exposure to the gas stream. It is often difficult to remove all of the agglomerate and, as a consequence, a portion of the agglomerate can remain on the collection plates for prolonged periods.
  • the resistivity reduction agent is believed to reduce the resistivities in the undesired particles in the agglomerate, thereby decreasing or eliminating the occurrence of back corona.
  • a resistivity reduction agent under hot- side electrostatic precipitating conditions is surprisingly effective. It is believed that under hot-side conditions, charged carriers pass through the undesired particles on the collection plates. This mechanism is referred to as volume conduction and the volume conduction operating region is illustrated in Fig. 6. In this region, the undesired particle resistivity is inversely related to undesired particle temperature. In contrast, under cold- side conditions (e.g., at temperatures no more than about 500°F) , the charged carriers are believed to travel along the surface of the undesired particles and not through the undesired particles. This mechanism is known as surface conduction and the surface conduction operating region is illustrated in Fig. 6.
  • the undesired particle resistivity is directly related to undesired particle temperature.
  • some resistivity reduction agents especially those described herein, are effective under hot-side conditions in reducing resistivity. This is surprising because other surface resistivity modifying agents, such as sulfuric acid, have been shown to be ineffective under hot-side operating conditions.
  • hot-side electrostatic precipitating devices in utility applications are located upstream of the air preheater while cold-side electrostatic precipitating devices are located downstream of the air preheater.
  • the gas stream is contacted with an adhesive composition including phosphoric acid, an adhesive, and a carrier fluid.
  • the adhesive can be any of the adhesives, preferably organic, noted above with respect to the first embodiment.
  • the adhesive composition is injected into the gas stream as a plurality of droplets, with the carrier fluid separating from the adhesive and phosphoric acid.
  • the droplets of adhesive and phosphoric acid contact the undesired particles and assist in formation of the agglomerate.
  • This embodiment has the advantage of combining the dual abilities of phosphoric acid to act as an adhesive and a resistivity reducer with the cohesive nature of the adhesive.
  • Adhesive A sodium carboxymethylcellulose
  • Adhesive B xanthan gum
  • Adhesive A at concentrations of adhesive in the gas stream of approximately 0.05% and 2.5% (wt additive/wt undesired particles) .
  • a decrease in undesired particle loading in the outlet of the electrostatic precipitator was observed for the additive at the 0.05% concentration.
  • An increase in the undesired particle loading leaving the electrostatic precipitator was observed during the injection of the 2.5% concentration.
  • Adhesive B was injected at a concentration of 0.05% and was also found to decrease undesired particle loading at the electrostatic precipitator outlet.
  • the electrostatic precipitator was modified by the installation of baffles at the input and output ducts to distribute the flow of the gas stream more uniformly through the active portions of the electrostatic precipitator.
  • the modification improved electrostatic precipitator efficiency from approximately 50% to over 70%.
  • Adhesive A was injected at a rate to produce a concentration of 0.05% (wt additive/wt undesired particles) . Efficiency improved from about 73% to about 83%. In other words. Adhesive A decreased undesired particle emissions by about 39%. Rapping the collection plates established that the dust cake would dislodge in "flakes". Undesired particle buildup did not prove any more severe than buildup without adhesive present.
  • Example 2 Example 2
  • the simulated flue gas stream was passed though an additives injection chamber and then through a resistivity measurement chamber. Both undesired particles (e.g., fly ash) and other flue gas constituents were added dynamically to create the representative gas composition and undesired particle content.
  • the moisture content of the flue gas was maintained at 10% by volume with a temperature-controlled humidifier upstream of the additives chamber. In the chamber, the additives were sprayed into the flow with a fine mist atomizer.
  • the additive volume injected through the injection nozzle was controlled with a precision peristaltic pump.
  • the simulated flue gas stream contained undesired particles that were added to the flow by a screw feeder with the injection rate being controlled by a variable speed motor. Entrained undesired particles were collected downstream of the additive injection chamber in a resistivity apparatus, e.g., a modified point-plane electrostatic precipitator.
  • a resistivity apparatus e.g., a modified point-plane electrostatic precipitator.
  • an agglomerate was collected by either electrical precipitation or by filtering across an electrically isolated metal frit. The resistivity of the agglomerate was measured by first determining the thickness of the agglomerate, then by applying a measured voltage and current across the agglomerate.
  • a 300 acfm slip stream of the off gas from a trial burn of a Powder River Basin coal in an electrostatic precipitation pilot plant was conditioned in a large spray contact chamber.
  • a mixture of phosphoric acid and corn syrup was injected into the spray contact chamber upstream of the electrostatic precipitator.
  • the pilot plant also supplied a fabric filter test device downstream of the spray chamber. The inlet to the fabric filter test device branched off at the electrostatic precipitator inlet.
  • the electrostatic precipitator was instrumented to continuously monitor voltage, current, flowrate, temperatures and outlet particulate emissions.
  • both a "clean plate” and “dirty plate” voltage/current curve was taken manually. Resistivity was measured continuously at the electrostatic precipitator inlet with a measurement frequency of less than 30 minutes. Resistivity samples were collected by filtering across an electrically isolated metal frit, rather than by point-plane precipitation. After the initial baseline experiment, the mixture was injected into the bottom of the large spray contact chamber with a fine atomizing spray nozzle oriented downstream. This produced a 10°F spray cooling of the flue gas stream. Residence time to the electrostatic precipitator inlet at this location was about 2 seconds. Gas velocity in the chamber was less than 1 foot per second.
  • Spray injection was then switched to water at the same flow rate. Resistivity returned to 4 x 10 11 ohm-centimeters, essentially a repeat of the baseline measurement. Electrostatic precipitator electrical conditions also began to degrade. This confirmed that the improved electrical conditions during additive injection were not a result of water spray cooling. Next, the mixture was injected at a concentration 10 times lower than for the previous test. At this rate, there was no measurable improvement in resistivity from baseline. An intermediate concentration between the high and low was then injected. Resistivity was measured at 1 x 10 11 ohm-centimeters for this condition. Electrical current density increased slightly over the baseline with water spray.
  • the nozzle was moved to the top of the spray chamber and the nozzle configuration was changed to a cluster head with 5 nozzles to determine the effects of residence time and spray droplet size on conditioning.
  • Residence time at this location was increased by more than 12 seconds from the previous test.
  • Conditioning with phosphoric acid from the spray chamber bottom decreased fly ash resistivity to 1.6 x 10 9 ohm-centimeters.
  • the combustor heat exchanger was beginning to plug, which reduced the particulate loading to the spray chamber/electrostatic precipitator. It was concluded that the additional residence time in the spray chamber was not required to achieve good conditioning with phosphoric acid.
  • Fig. 9 shows fly ash resistivity as a function of phosphoric acid concentration at 300°F.
  • Phosphoric acid concentration is expressed in relative terms linearly related to mass of the additive to the total weight of entrained undesired particles.
  • outlet mass emissions were measured continuously by an optical monitor which responds proportionately to back-scattered light from entrained undesired particles in the gas stream. The monitor response decreased from 9% to less than 6% due to conditioning.
  • Flue gas was extracted isokinetically from an 18 inch diameter duct supplying a particulate control pilot plant in operation at a power plant.
  • the slip stream was extracted from the plant duct downstream of the air heater and upstream of a reverse gas baghouse.
  • An atomizing spray nozzle manifold was inserted into the slip stream duct approximately 40 feet in a 90 degree bend upstream of a sample probe. Liquid feed to the nozzle manifold was controlled with a peristaltic pump. Atomizing air pressure was set to a constant 80 psig.
  • the sample probe drew flue gas isokinetically to a portable electrostatic precipitator at a flowrate of approximately 60 acfm. In all, sample residence time from injection to the electrostatic precipitator inlet was less than 2 seconds. Velocity in the duct was 50-60 feet per second and the gas temperature was 250°F. The sample was reheated to a constant 300°F at the electrostatic precipitator inlet.
  • the portable electrostatic precipitator was configured as a single channel wire/plate at a 9 inch plate spacing with standard 0.1 inch diameter bare wires. Special teflon baffles were installed around and beneath the collection plates to minimize sneakage. The flowrate was set to give an SCA of 180 square feet/kacfm. Electrostatic precipitator voltage and current were monitored continuously and voltage/current curves were taken to sparking for each test condition. Multiple resistivity measurements were taken at the electrostatic precipitator inlet for each test condition. Outlet particulate concentrations were monitored by a TRIBOFLOW monitor, which produces a response proportional to the number of charged particles contacting a probe. Fig. 10 presents the resistivity measurements taken during the test.
  • Baseline resistivity at 300°F was mid - 10 11 ohm- centimeters.
  • the additives were injected at 3 different phosphoric acid concentrations. Conditioning with phosphoric acid at the high concentration on the first test day reduced the resistivity to mid - 10 10 ohm-centimeters. Conditioning on the following day at the same concentration reduced the resistivity to mid - 10 9 ohm-centimeters. It is believed that this difference is the result of a change in nozzle alignment.
  • the condition was also repeated by doubling liquid flow and halving additive solution concentration. This had no apparent effect on performance.
  • the condition was also repeated by doubling liquid flow to the nozzle array and halving solution concentration.
  • TRIBOFLOW monitor response was set to 0-20% full- scale. During injection at high concentration over a 2 hour period, the TRIBOFLOW monitor response dropped from 2.75% to 1.75%. After injection stopped, the response increased to 2.5%, indicating an increase in charged undesired particles exiting the electrostatic precipitator.
  • TRIBOFLOW response increased off scale (greater than 20%) .
  • the portable electrostatic precipitator was manually adjusted to higher power levels twice during additive injection. Attempts to increase power to the same power levels at baseline were spark-limited.
  • the change in TRIBOFLOW response and the ability to increase power demonstrated a qualitative improvement in electrostatic precipitator performance from baseline to conditioning with phosphoric acid, consistent with the decrease in fly ash resistivity.
  • the mixture of additives was found to provide increased undesired particle cohesivity and agglomerate porosity and tensile strength relative to untreated undesired particles/agglomerates.
  • the phosphoric acid additive in the mixture was found to provide more desirable undesired particle resistivities for electrostatic precipitator applications.
  • the tests further indicated that undesired particle conditioning to improve resistivity can be effective over a wider temperature range than conventional additives, such as sulfur trioxide.
  • Example 5 A test was conducted to determine if the mixture of phosphoric acid and corn syrup could alleviate electrostatic precipitator performance problems associated with sodium ion depletion in agglomerates deposited on hot- side electrostatic precipitator collection plates.
  • Example 2 the experimental device used in Example 2 above was employed. The test was conducted at a flue gas temperature of 700°F in a 10% moisture, air environment. The undesired particles were from an ash sample from a hot-side electrostatic precipitator at a plant firing a western sub-bituminous coal. As can be seen from Fig. 11, the mixture reduced undesired particle resistivity by up to 2 orders of magnitude. It was thus determined that the amount of resistivity reduction can be controlled by the concentration of phosphoric acid under hot-side conditions. Further laboratory resistivity tests were conducted using a mixture of 75% Si0 2 and 25% A1 2 0 3 powder.
  • This synthetic undesired particle mix was created to entirely eliminate alkali ion charge carriers from the agglomerate and thereby present a worst-case undesired particle condition.
  • the mixture of refractory powders was redispersed on the resistivity measurement frit to form a powder layer (e.g., agglomerate) and was heated to 700°F in a 10% moisture gas stream.
  • the powder layer was conditioned by injecting a liquid additive as an aqueous spray in the spray additive chamber upstream of the resistivity measurement cell at 700°F. Additive was brought into contact with the powder layer by drawing sample gas through the powder layer in the porous sample frit. Baseline tests were also conducted with no flue gas conditioning by injecting a water spray.
  • Resistivity of the undesired particles was 4 x 10 9 ohm-centimeters. Conditioning with phosphoric acid successfully lowered resistivity by an order of magnitude to 4 x 10 8 ohm-centimeters. While the unconditioned powder layer at this temperature exhibited only moderate resistivity, the test demonstrated that the phosphoric acid can effectively reduce resistivity independent of sodium or lithium ion charge carriers at hot-side conditions.
  • a fabric filter test was conducted on a flue gas slipstream taken upstream of an existing particulate control device at a utility power plant firing a Texas lignite coal.
  • the test equipment consisted of a sample probe, an additive contact chamber, an additive injection assembly, and a filter test device. Flue gas was extracted isokinetically from the host plant duct through the sample probe. The host duct temperature at the inlet extraction location ranged from 360 to 400°F. The filter chamber temperature and the additives contact chamber were maintained at 400°F for all tests.
  • an aqueous solution of diluted additive was atomized and injected into the flue gas stream using a small, dual-fluid nozzle. Additive liquid flowrate was metered and controlled with a precision peristaltic pump.
  • the filter device was configured for reverse-gas cleaning with an 8-inch diameter fiberglass bag of a weight and weave to match the bags currently in use in the shake/deflate baghouse of a weight and weave to match the bags currently in use in the shake/deflate baghouse of the host power plant.
  • Relative outlet particulate emissions were measured using a TRIBOFLOWTM monitor installed downstream of the filter chamber. Mass concentration measurements in the filter chamber inlet line during the baseline tests indicated a loading of 11 gr/acf.
  • the phosphoric acid/water solution was injected at a constant rate during the test series.
  • the phosphoric acid solution concentration was incrementally increased, noting the performance at each concentration for at least 4 hours. At very low concentrations a 60% decrease in outlet particle loading was measured. As the concentration was increased, the cleaning frequency decreased and further reductions in outlet emissions occurred. Table 1 summarizes the test results.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Electrostatic Separation (AREA)
  • Treating Waste Gases (AREA)
  • Filtering Materials (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)

Abstract

Procédé d'élimination de particules indésirables (35) contenues dans un flux de gaz (36), consistant à injecter (10), au moyen de buses (37), une composition contenant un adhésif (40) dans le flux de gaz (36), à recueillir les particules indésirables (35) et l'adhésif (40) sur une surface collectrice (28) de façon à former un agglomérat (44), et à éliminer l'agglomérat de la surface collectrice (28).ssage (28).
PCT/US1995/009746 1995-06-07 1995-08-02 Procede d'elimination des particules indesirables contenues dans un gaz WO1996040436A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP95929354A EP0831971A4 (fr) 1995-06-07 1995-08-02 Procede d'elimination des particules indesirables contenues dans un gaz
AU32737/95A AU3273795A (en) 1995-06-07 1995-08-02 Method for removing undesired particles from gas

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US48307695A 1995-06-07 1995-06-07
US483,076 1995-06-07

Publications (1)

Publication Number Publication Date
WO1996040436A1 true WO1996040436A1 (fr) 1996-12-19

Family

ID=23918551

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1995/009746 WO1996040436A1 (fr) 1995-06-07 1995-08-02 Procede d'elimination des particules indesirables contenues dans un gaz

Country Status (4)

Country Link
EP (1) EP0831971A4 (fr)
AU (1) AU3273795A (fr)
CA (1) CA2223999A1 (fr)
WO (1) WO1996040436A1 (fr)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6267802B1 (en) 1999-06-17 2001-07-31 Ada Environmental Solutions, Llc Composition apparatus and method for flue gas conditioning
CN105107629A (zh) * 2015-09-18 2015-12-02 广东电网有限责任公司电力科学研究院 一种用于降低飞灰比电阻的比电阻调节剂及其应用
KR101876489B1 (ko) 2016-12-15 2018-08-09 주식회사 써치앤델브 전기 집진식 유증기 집진 제거기 및 이를 이용한 전기 집진식 유증기 집진 제거 방법
CN114769002A (zh) * 2022-05-30 2022-07-22 浙江安达环保设备有限公司 湿式电除尘器喷淋装置及湿式电除尘器
US11802257B2 (en) 2022-01-31 2023-10-31 Marathon Petroleum Company Lp Systems and methods for reducing rendered fats pour point
US11860069B2 (en) 2021-02-25 2024-01-02 Marathon Petroleum Company Lp Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US11891581B2 (en) 2017-09-29 2024-02-06 Marathon Petroleum Company Lp Tower bottoms coke catching device
US11898109B2 (en) 2021-02-25 2024-02-13 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of hydrotreating and fluid catalytic cracking (FCC) processes using spectroscopic analyzers
US11905468B2 (en) 2021-02-25 2024-02-20 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of fluid catalytic cracking (FCC) processes using spectroscopic analyzers
US11905479B2 (en) 2020-02-19 2024-02-20 Marathon Petroleum Company Lp Low sulfur fuel oil blends for stability enhancement and associated methods
US11970664B2 (en) 2021-10-10 2024-04-30 Marathon Petroleum Company Lp Methods and systems for enhancing processing of hydrocarbons in a fluid catalytic cracking unit using a renewable additive
US11975316B2 (en) 2019-05-09 2024-05-07 Marathon Petroleum Company Lp Methods and reforming systems for re-dispersing platinum on reforming catalyst
US12000720B2 (en) 2018-09-10 2024-06-04 Marathon Petroleum Company Lp Product inventory monitoring
US12031676B2 (en) 2019-03-25 2024-07-09 Marathon Petroleum Company Lp Insulation securement system and associated methods
US12031094B2 (en) 2021-02-25 2024-07-09 Marathon Petroleum Company Lp Assemblies and methods for enhancing fluid catalytic cracking (FCC) processes during the FCC process using spectroscopic analyzers

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104888573B (zh) * 2015-05-27 2017-01-11 潘祖明 一种促进微细颗粒物聚集长大的装置及方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3665676A (en) * 1970-11-12 1972-05-30 Koppers Co Inc Method of and apparatus for chemically conditioning a particle-laden gas stream
US4070424A (en) * 1976-09-21 1978-01-24 Uop Inc. Method and apparatus for conditioning flue gas with a mist of H2 SO4
US4325711A (en) * 1980-05-15 1982-04-20 Apollo Technologies, Inc. Method of conditioning flue gas and separating the particles therefrom
US4738690A (en) * 1985-03-29 1988-04-19 Gus, Inc. Method of removing entrained particles from flue gas and composition of matter
US4888158A (en) * 1988-10-24 1989-12-19 The Babcock & Wilcox Company Droplet impingement device

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4306885A (en) * 1978-02-27 1981-12-22 Apollo Technologies, Inc. Method of conditioning flue gas

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3665676A (en) * 1970-11-12 1972-05-30 Koppers Co Inc Method of and apparatus for chemically conditioning a particle-laden gas stream
US4070424A (en) * 1976-09-21 1978-01-24 Uop Inc. Method and apparatus for conditioning flue gas with a mist of H2 SO4
US4325711A (en) * 1980-05-15 1982-04-20 Apollo Technologies, Inc. Method of conditioning flue gas and separating the particles therefrom
US4738690A (en) * 1985-03-29 1988-04-19 Gus, Inc. Method of removing entrained particles from flue gas and composition of matter
US4888158A (en) * 1988-10-24 1989-12-19 The Babcock & Wilcox Company Droplet impingement device

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP0831971A4 *

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6267802B1 (en) 1999-06-17 2001-07-31 Ada Environmental Solutions, Llc Composition apparatus and method for flue gas conditioning
CN105107629A (zh) * 2015-09-18 2015-12-02 广东电网有限责任公司电力科学研究院 一种用于降低飞灰比电阻的比电阻调节剂及其应用
KR101876489B1 (ko) 2016-12-15 2018-08-09 주식회사 써치앤델브 전기 집진식 유증기 집진 제거기 및 이를 이용한 전기 집진식 유증기 집진 제거 방법
US11891581B2 (en) 2017-09-29 2024-02-06 Marathon Petroleum Company Lp Tower bottoms coke catching device
US12000720B2 (en) 2018-09-10 2024-06-04 Marathon Petroleum Company Lp Product inventory monitoring
US12031676B2 (en) 2019-03-25 2024-07-09 Marathon Petroleum Company Lp Insulation securement system and associated methods
US11975316B2 (en) 2019-05-09 2024-05-07 Marathon Petroleum Company Lp Methods and reforming systems for re-dispersing platinum on reforming catalyst
US11905479B2 (en) 2020-02-19 2024-02-20 Marathon Petroleum Company Lp Low sulfur fuel oil blends for stability enhancement and associated methods
US11920096B2 (en) 2020-02-19 2024-03-05 Marathon Petroleum Company Lp Low sulfur fuel oil blends for paraffinic resid stability and associated methods
US11921035B2 (en) 2021-02-25 2024-03-05 Marathon Petroleum Company Lp Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US11906423B2 (en) 2021-02-25 2024-02-20 Marathon Petroleum Company Lp Methods, assemblies, and controllers for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US11905468B2 (en) 2021-02-25 2024-02-20 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of fluid catalytic cracking (FCC) processes using spectroscopic analyzers
US11898109B2 (en) 2021-02-25 2024-02-13 Marathon Petroleum Company Lp Assemblies and methods for enhancing control of hydrotreating and fluid catalytic cracking (FCC) processes using spectroscopic analyzers
US11885739B2 (en) 2021-02-25 2024-01-30 Marathon Petroleum Company Lp Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US11860069B2 (en) 2021-02-25 2024-01-02 Marathon Petroleum Company Lp Methods and assemblies for determining and using standardized spectral responses for calibration of spectroscopic analyzers
US12031094B2 (en) 2021-02-25 2024-07-09 Marathon Petroleum Company Lp Assemblies and methods for enhancing fluid catalytic cracking (FCC) processes during the FCC process using spectroscopic analyzers
US11970664B2 (en) 2021-10-10 2024-04-30 Marathon Petroleum Company Lp Methods and systems for enhancing processing of hydrocarbons in a fluid catalytic cracking unit using a renewable additive
US11802257B2 (en) 2022-01-31 2023-10-31 Marathon Petroleum Company Lp Systems and methods for reducing rendered fats pour point
CN114769002A (zh) * 2022-05-30 2022-07-22 浙江安达环保设备有限公司 湿式电除尘器喷淋装置及湿式电除尘器

Also Published As

Publication number Publication date
CA2223999A1 (fr) 1996-12-19
EP0831971A4 (fr) 1998-12-16
EP0831971A1 (fr) 1998-04-01
AU3273795A (en) 1996-12-30

Similar Documents

Publication Publication Date Title
US5855649A (en) Liquid additives for particulate emissions control
US5893943A (en) Method and apparatus for decreased undesired particle emissions in gas streams
WO1996040436A1 (fr) Procede d'elimination des particules indesirables contenues dans un gaz
US6797035B2 (en) Oxidizing additives for control of particulate emissions
US5137546A (en) Process and apparatus for electrostatic purification of dust- and pollutant-containing exhaust gases in multiple-field precipitators
US6267802B1 (en) Composition apparatus and method for flue gas conditioning
CA1156937A (fr) Lit filtrant et methode de captage des cendres volantes et des poussieres
AU643794B2 (en) Process and apparatus for purifying dust-and pollutant- containing exhaust gases
US6106592A (en) Wet electrostatic filtration process and apparatus for cleaning a gas stream
US5601791A (en) Electrostatic precipitator for collection of multiple pollutants
KR100679186B1 (ko) 대전된 액적 가스 세척 장치 및 방법
US4029482A (en) Electrostatic removal of airborne particulates employing fiber beds
US4070162A (en) Method of agglomerating particles in gas stream
US4146371A (en) Electrofluidized bed agglomerator and method of agglomerating
CZ163898A3 (cs) Čisticí elektrostatická pistole pro elektrostatické nabíjení suchého sorbentu a jeho vstřikování do proudu znečištěného proudu plynu
US8398744B2 (en) Method and apparatus for air pollution control
US4325711A (en) Method of conditioning flue gas and separating the particles therefrom
KR100561550B1 (ko) 정전분사세정집진방법 및 그 장치
KR200343967Y1 (ko) 정전분사세정집진장치
DE19542859A1 (de) Oberflächenfiltration- und -filter
CA1134286A (fr) Separateur a lit de fibres avec intervention d'une charge electrostatique
CN101310867A (zh) 一种改善除尘器效率的粉尘预处理方法及其装置
Lamb et al. Electrical stimulation of fabric filtration
DE3640743A1 (de) Verfahren und vorrichtung zur feinstreinigung von abgasen
JPH0439367B2 (fr)

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AM AT AU BB BG BR BY CA CH CN CZ DE DK EE ES FI GB GE HU IS JP KE KG KP KR KZ LK LR LT LU LV MD MG MN MW MX NO NZ PL PT RO RU SD SE SG SI SK TJ TM TT UA UZ VN

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): KE MW SD SZ UG AT BE CH DE DK ES FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN ML MR NE SN TD TG

DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
121 Ep: the epo has been informed by wipo that ep was designated in this application
WWE Wipo information: entry into national phase

Ref document number: 1995929354

Country of ref document: EP

ENP Entry into the national phase

Ref document number: 2223999

Country of ref document: CA

Ref country code: CA

Ref document number: 2223999

Kind code of ref document: A

Format of ref document f/p: F

WWP Wipo information: published in national office

Ref document number: 1995929354

Country of ref document: EP

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

WWW Wipo information: withdrawn in national office

Ref document number: 1995929354

Country of ref document: EP