Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/34—Chemical or biological purification of waste gases
  • B01D53/46—Removing components of defined structure
  • B01D53/64—Heavy metals or compounds thereof, e.g. mercury
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
  • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
  • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
  • B01D53/10—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
• • C—CHEMISTRY; METALLURGY
  • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
  • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
  • C04B7/00—Hydraulic cements
  • C04B7/36—Manufacture of hydraulic cements in general
• • C—CHEMISTRY; METALLURGY
  • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
  • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
  • C04B7/00—Hydraulic cements
  • C04B7/36—Manufacture of hydraulic cements in general
  • C04B7/364—Avoiding environmental pollution during cement-manufacturing
  • C04B7/365—Avoiding environmental pollution during cement-manufacturing by extracting part of the material from the process flow and returning it into the process after a separate treatment, e.g. in a separate retention unit under specific conditions
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
  • B01D2253/10—Inorganic adsorbents
  • B01D2253/102—Carbon
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2257/00—Components to be removed
  • B01D2257/60—Heavy metals or heavy metal compounds
  • B01D2257/602—Mercury or mercury compounds
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2258/00—Sources of waste gases
  • B01D2258/02—Other waste gases
  • B01D2258/0233—Other waste gases from cement factories

Definitions

• This invention relates to reduction of mercury emissions from cement plants.
• activated carbon can be injected into a gas stream containing mercury vapor.
• mercury vapor contacts activated carbon particles, the mercury is captured and held by the activated carbon particles.
• the particles are then collected by a particulate collection device, such as an electrostatic precipitator or a baghouse filter.
• the mercury captured by the activated carbon particles appears to be stably bonded to the particles.
• the particulates captured by the control device are normally recycled to the cement production process.
• the exhaust gas stream from the cement production process contains particulates, and these particulates are normally collected by the particulate collection device, usually a fabric filter or an electrostatic precipitator. Collected particulates from the cement production process, which include the cement dust, are often recycled from the particulate collection device and used as part of the raw material feed, where the mercury is again volatilized as the raw material is heated. Thus, recycling the cement dust to the raw material feed continually re-introduces mercury into the cement production process and thereby into cement dust and the accompanying exhaust gas stream.
• the exhaust gas itself is sometimes recycled to the cement production process.
• the exhaust gas typically contains a small amount of mercury; returning the exhaust gas to the raw mill introduces additional mercury to the raw material feed.
• This invention provides methods for reducing the emissions of mercury from cement plants at relatively low cost.
• One advantage is that the methods provided herein can be incorporated into existing cement plants without requiring extensive reconfiguration.
• Another advantage of the methods described herein is the removal of mercury early in the cement-making process, which can minimize the need for additional mercury control downstream.
• An embodiment of this invention is a method for reducing emissions of mercury from a cement plant comprising at least a kiln, a particulate collection device, collected particulates, an exhaust gas stream, a heater, and a mercury scrubber, wherein the heater and mercury scrubber are upstream from the kiln.
• the method comprises
• the exhaust gas stream exits the particulate collection device and is not directed into the heater.
• An optional step is the injecting of a mercury sorbent at one or more points between the kiln and the particulate collection device.
• Figure 1 is a schematic diagram of a generalized cement plant configuration.
• Figure 2A is a schematic diagram showing the placement of the heater and mercury scrubber when a preheater tower is present in the cement plant.
• Figure 2B is a schematic diagram of the placement of the heater and mercury scrubber when a preheater tower is not present in the cement plant.
• collected particulates refers to the particulates collected by the particulate collection device of the cement plant, and includes the cement dust.
• FIG. 1 A generalized cement plant configuration showing pertinent parts is shown in Fig. 1.
• raw material feed 8d from the raw material mill 2 (raw mill) is fed to the top of the preheater tower 4 (sometimes called a precalciner tower) and from the preheater tower 4 into the kiln 6.
• Clinker is produced in the kiln, and is discharged from the kiln.
• a gas stream 8a exits from the kiln 6.
• the gas stream 8a enters the bottom of the preheater tower 4 and exits from the top of the preheater tower 4.
• the exhaust gas stream 8b is then cooled, usually by water, often in a conditioning tower and the cooled exhaust gas stream 8b instead travels to a particulate collection device 10. After passing through the particulate collection device 10, the exhaust gas stream 8c exits the cement plant by traveling through the stack 12.
• the phrase "downstream toward the kiln" refers to the various possible combinations for the recycled collected particulates.
• the collected particulates can be combined with the raw material feed at any point downstream from the heater from which the collective particulates are exiting.
• the collected particulates can be recycled to the raw mill rather than into the raw material feed.
• the collected particulates can be combined with the raw material feed before or after the preheater tower.
• the collected particulates can be recycled directly to the kiln.
• the phrase "downstream toward the kiln" encompasses all of these possibilities.
• the cement plants comprise at least a kiln, a particulate collection device, collected particulates, an exhaust gas stream, a heater, and a mercury scrubber, which heater and mercury scrubber are upstream from the kiln.
• the collected particulates are directed through the heater.
• the collected particulates are heated to a temperature high enough to volatilize the mercury present in the collected particulates, which forms volatilized mercury species from the collected particulates.
• the collected particulates are directed downstream toward the kiln, where they are normally combined with the raw material feed, or introduced into the raw mill, the preheater tower, or the kiln; preferably, the collected particulates are introduced into the kiln.
• the volatilized mercury species which are normally in a gas stream, are directed to the mercury scrubber, which removes the mercury, usually from a gas stream.
• particulates from the cement manufacturing process are carried by the exhaust gas stream to the particulate collection device, where the particulates are removed from the exhaust gas stream.
• the collected particulates are directed to the heater, as just described, but the exhaust gas stream exits the particulate collection device and is not directed into the heater.
• Another method of this invention is for reducing emissions of mercury from a cement plant comprising at least a kiln, a particulate collection device, collected particulates, and an exhaust gas stream.
• the method comprises
• the exhaust gas stream exits the particulate collection device and is not directed into the heater.
• FIG. 2A A configuration of a portion of a cement plant for the methods of this invention showing the placement of the heater 14 and mercury scrubber 16 is shown in Fig. 2A and in Fig. 2B.
• raw material feed 8d exits the raw material mill 2.
• Collected particulates 8g are transported from a particulate collection device (not shown) to the heater 14 upstream of the preheater tower 4.
• the collected particulates 8e exit the heater 14, and are combined with the raw material feed 8d, which is fed to the preheater tower 4.
• the gas stream 8f containing volatilized mercury and small particulates is routed to the mercury scrubber 16.
• raw material feed 8d exits the raw material mill 2.
• Collected particulates 8g are transported from the particulate collection device (not shown) to the heater 14 upstream of the kiln 6.
• the collected particulates 8e exit the heater 14 and are combined with the raw material feed 8d, which is fed to the kiln 6.
• the gas stream 8f containing volatilized mercury and small particulates is routed to the mercury scrubber 16. Variations on the methods illustrated in Figs. 2 A and 2B are possible and within the scope of the invention.
• the heater and the mercury scrubber are preferably in close proximity, but such an arrangement may not be possible, depending on the configuration of the particular cement plant.
• the heater can be any type of heater that can heat the raw material feed to the desired temperature. Suitable heaters include rotary kilns, mill heaters, and the like. A heater with a screw feeder inside is preferred in some embodiments, because the screw feeder promotes more uniform heating.
• the collected particulates are directed into the heater and are heated to one or more temperatures at or above the volatilization temperature of mercury from the collected particulates, preferably while being transported inside (through) the heater.
• temperatures of at least about 200°C are generally employed.
• temperatures in the heater are in the range of about 200°C to about 800°C, and more preferably in the range of about 300°C to about 700°C.
• Mercury species typically volatilize from collected particulates at temperatures roughly in the range of 300°C to 700°C. When the temperature is lower than 300°C, volatilization of mercury is possible, but not very efficient. At temperatures of about 700°C or greater, the volatilization of mercury does not increase significantly in proportion to the amount of heat energy expended.
• the collected particulates from which the mercury has been removed are directed toward the kiln.
• the collected particulates can travel through other structures (such as a preheater tower) at the cement plant prior to entering the kiln, or the collected particulates can be stored, if desired (e.g. , if the kiln is shut down for maintenance).
• the volatilized mercury exits the heater, usually as part of a gas stream, and is directed to the mercury scrubber.
• the mercury scrubber contains at least one absorption medium to absorb the mercury directed to the mercury scrubber.
• the absorbent medium is usually a solid mercury sorbent.
• the mercury scrubber also has a moving bed to capture particulates that are contained in the gas stream entering the mercury scrubber.
• Capture of particulate matter by the moving bed protects the absorbent medium (or media) in the mercury scrubber which allows the absorbent media to perform for longer periods of time without replacement or re-activation.
• Suitable sorbents to capture the particulate matter in the moving bed are granular sorbents generally having a size range between about 5 and about 20 U.S. Mesh (0.85 to 4 mm), preferably about 5 to about 7 U.S. Mesh (2.8 to 4 mm). Examples of such sorbents include sand, stone particles, ceramic, glass beans, quartz, and activated carbon.
• Activated carbon for the moving bed includes unaltered activated carbon and chemically-treated activated carbon, including bromine- or sulfur- impregnated activated carbons.
• suitable sorbents include activated carbon sorbents, modified activated carbon sorbents, activated carbon fiber sorbents, metals that react with mercury, sulfur, a metal sulfide reacts with mercury, such as sodium sulfide, potassium sulfide, iron sulfide, zinc sulfide, and the like, and mineral sorbents (e.g. , silica or zeolites).
• the sulfur or metal sulfide can be used in powdered form, granular form, or honeycomb form.
• the mercury sorbent is preferably an activated carbon sorbent.
• Granulated or powdered activated carbon can be employed; granulated activated carbon is preferred.
• the activated carbon sorbent is preferably a bromine-containing activated carbon sorbent.
• Bromine-containing activated carbon sorbents are formed by treating (contacting) the sorbent with an effective amount of a bromine-containing substance for a sufficient time to increase the ability of the activated carbon to adsorb mercury and mercury-containing compounds. Such contacting of the activated carbon sorbent and a bromine-containing substance significantly increases the sorbent's ability to absorb mercury and mercury-containing compounds.
• Treatment of the activated carbon sorbent with bromine-containing substance(s) is preferably conducted such that the sorbent has about 0.1 to about 15 wt bromine. See in this connection U.S. Pat. No. 6,953,494.
• a preferred bromine-containing activated carbon is available commercially from Albemarle Corporation as B-PACTM.
• suitable apparatus include cartridges, fixed beds, moving beds, including continuous cross-flow moving beds, and the like. Fixed beds are preferred.
• the exhaust gas stream is not directed to the heater. This provides certain advantages. The absence of certain the exhaust gas stream from flowing through the heater allows the apparatus holding, supporting, or containing the mercury sorbents to be smaller in size, and minimizes air flow plugging of the apparatus holding, supporting, or containing the mercury sorbents.
• the gas stream containing the volatilized mercury is fed to at least one and then to at least one other of at least two absorbent media (which may be the same or different) present in the mercury scrubber.
• the mercury-containing gas stream can be continuously fed into the mercury scrubber to one absorbent medium, while the other absorbent medium is replaced or recharged, so that as one absorbent medium reaches capacity, the gas stream is switched to the other absorbent medium, which allows mercury-containing gas streams to be continuously processed through the mercury scrubber without material interruption.
• the gas stream discharged from the mercury scrubber is directed to the particulate collection device, or to the stack.
• a mercury sorbent optionally and preferably can be injected between the kiln and the particulate collection device.
• the mercury sorbent is injected after the kiln (and after the preheater tower, if present). After injection, the mercury sorbent eventually reaches the particulate collection device and becomes part of the collected particulates.
• a benefit of this optional step in the methods of this invention is the further reduction of mercury emissions from the exhaust gas stream from the cement plant.
• a particular advantage of sorbent injection is that mercury emissions are decreased whether or not the raw mill is operating.
• the mercury sorbent can be any solid mercury sorbent that is capable of absorbing mercury when injected into a gas stream.
• mercury sorbents include, but are not limited to, activated carbon sorbents, modified activated carbon sorbents, activated carbon fiber sorbents, metals that react with mercury, sulfur, a metal sulfide reacts with mercury, such as sodium sulfide, potassium sulfide, iron sulfide, zinc sulfide, and the like, and mineral sorbents (e.g. , silica or zeolites).
• the injected mercury sorbent is preferably an activated carbon sorbent.
• Granulated or powdered activated carbon can be employed; powdered activated carbon is preferred.
• the activated carbon sorbent is preferably a bromine-containing activated carbon sorbent.
• Bromine-containing activated carbon sorbents are formed by treating (contacting) the sorbent with an effective amount of a bromine-containing substance for a sufficient time to increase the ability of the activated carbon to adsorb mercury and mercury-containing compounds. Such contacting of the activated carbon sorbent and a bromine-containing substance significantly increases the sorbent's ability to absorb mercury and mercury-containing compounds.
• Treatment of the activated carbon sorbent with bromine-containing substance(s) is preferably conducted such that the sorbent has about 0.1 to about 15 wt bromine. See in this connection U.S. Pat. No. 6,953,494.
• a preferred bromine-containing activated carbon is available commercially from Albemarle Corporation as B-PACTM.
• the mercury sorbents are typically injected at a rate of about 0.5 to about 15 lb/MMacf (8xl0 ⁇ 6 to 240xl0 "6 kg/m 3 ).
• Preferred injection rates are about 1 to about 10 lb/MMacf (16xl0 ⁇ 6 to 160xl0 "6 kg/m 3 ); more preferred are injection rates of about 2 to about 5 lb/MMacf (32xl0 ⁇ 6 to 80xl0 "6 kg/m 3 ), though it is understood that the preferred injection rate varies with the particular system configuration.
• the invention may comprise, consist, or consist essentially of the materials and/or procedures recited herein.
• the term "about" modifying the quantity of an ingredient in the compositions of the invention or employed in the methods of the invention refers to variation in the numerical quantity that can occur, for example, through typical measuring and liquid handling procedures used for making concentrates or use solutions in the real world; through inadvertent error in these procedures; through differences in the manufacture, source, or purity of the ingredients employed to make the compositions or carry out the methods; and the like.
• the term about also encompasses amounts that differ due to different equilibrium conditions for a composition resulting from a particular initial mixture. Whether or not modified by the term "about”, the claims include equivalents to the quantities.

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• Analytical Chemistry (AREA)
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• Oil, Petroleum & Natural Gas (AREA)
• Chemical Kinetics & Catalysis (AREA)
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• 2011
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