GB2242421A - Process for the production of metal oxide aerosols - Google Patents
Process for the production of metal oxide aerosols Download PDFInfo
- Publication number
- GB2242421A GB2242421A GB9015112A GB9015112A GB2242421A GB 2242421 A GB2242421 A GB 2242421A GB 9015112 A GB9015112 A GB 9015112A GB 9015112 A GB9015112 A GB 9015112A GB 2242421 A GB2242421 A GB 2242421A
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- GB
- United Kingdom
- Prior art keywords
- metal
- aerosol
- zone
- gaseous stream
- temperature
- Prior art date
- 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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- 239000000443 aerosol Substances 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 47
- 229910044991 metal oxide Inorganic materials 0.000 title claims abstract description 33
- 150000004706 metal oxides Chemical class 0.000 title claims abstract description 33
- 238000004519 manufacturing process Methods 0.000 title claims description 12
- 229910052751 metal Inorganic materials 0.000 claims abstract description 57
- 239000002184 metal Substances 0.000 claims abstract description 57
- 230000008016 vaporization Effects 0.000 claims abstract description 25
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 15
- 230000001590 oxidative effect Effects 0.000 claims abstract description 12
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 10
- 239000007800 oxidant agent Substances 0.000 claims abstract description 10
- 239000002245 particle Substances 0.000 claims description 21
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 14
- 239000011575 calcium Substances 0.000 claims description 14
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 9
- 239000011777 magnesium Substances 0.000 claims description 9
- 239000007787 solid Substances 0.000 claims description 8
- 150000002739 metals Chemical class 0.000 claims description 7
- 239000011261 inert gas Substances 0.000 claims description 6
- 229910052784 alkaline earth metal Inorganic materials 0.000 claims description 4
- 150000001342 alkaline earth metals Chemical class 0.000 claims description 4
- 230000008018 melting Effects 0.000 claims description 3
- 238000002844 melting Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 2
- 239000002594 sorbent Substances 0.000 abstract description 16
- 239000007789 gas Substances 0.000 abstract description 15
- 239000002253 acid Substances 0.000 abstract description 7
- 239000012159 carrier gas Substances 0.000 abstract description 2
- 238000001179 sorption measurement Methods 0.000 abstract 1
- 235000019738 Limestone Nutrition 0.000 description 8
- 238000010521 absorption reaction Methods 0.000 description 8
- 239000006028 limestone Substances 0.000 description 8
- 238000009834 vaporization Methods 0.000 description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 229910052717 sulfur Inorganic materials 0.000 description 7
- 239000011593 sulfur Substances 0.000 description 7
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 6
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000002347 injection Methods 0.000 description 6
- 239000007924 injection Substances 0.000 description 6
- 235000012245 magnesium oxide Nutrition 0.000 description 6
- 239000000395 magnesium oxide Substances 0.000 description 5
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical class [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 235000012255 calcium oxide Nutrition 0.000 description 4
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- 229910052786 argon Inorganic materials 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 3
- 239000000292 calcium oxide Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 3
- 150000002736 metal compounds Chemical class 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000010960 commercial process Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000008092 positive effect Effects 0.000 description 2
- 239000011164 primary particle Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000000523 sample Substances 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 230000019635 sulfation Effects 0.000 description 1
- 238000005670 sulfation reaction Methods 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
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
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/508—Sulfur oxides by treating the gases with solids
-
- 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
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
-
- 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
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- 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
- B01D53/68—Halogens or halogen compounds
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B13/00—Oxygen; Ozone; Oxides or hydroxides in general
- C01B13/14—Methods for preparing oxides or hydroxides in general
- C01B13/20—Methods for preparing oxides or hydroxides in general by oxidation of elements in the gaseous state; by oxidation or hydrolysis of compounds in the gaseous state
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/02—Oxides or hydroxides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/02—Magnesia
- C01F5/04—Magnesia by oxidation of metallic magnesium
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/60—Particles characterised by their size
- C01P2004/61—Micrometer sized, i.e. from 1-100 micrometer
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2004/00—Particle morphology
- C01P2004/60—Particles characterised by their size
- C01P2004/62—Submicrometer sized, i.e. from 0.1-1 micrometer
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Geology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Treating Waste Gases (AREA)
- Oxygen, Ozone, And Oxides In General (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Agricultural Chemicals And Associated Chemicals (AREA)
- Colloid Chemistry (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
A process for producing a metal-oxide aerosol comprises vaporizing the elemental metal eg Ca or Mg in an oxidant free environment under controlled conditions and thereafter oxidizing said vaporized metal under controlled conditions to form an aerosol of said metal-oxide in a carrier gas stream. The aerosol may thereafter be fed to an effluent-containing gaseous stream for removal of effluents by sorption under controlled temperature conditions. Acid gas such as SO2, SO3, NO, NO2, H2S and HCl may be removed from off gases using the aerosol sorbent.
Description
1 4 Z PROCESS FOR PRODUCTION OF METALAL OXIDE AEROSOnS The present
invention relates to processes f or the production of metal- oxide aerosols, and more particularly, to processes for utilizing the metal-oxide aerosols as an effluent sorbent.
As is well known, acid gas effluents such as S02, S03, NO, N02, H2S and HCl which are present in off gases from numerous chemical reactions represent primary atmospheric pollutants. Heretofore, reduction of acid gas effluents in these gaseous streams to environmentally acceptable levels has proven to be extremely costly.
For example, one of the commercial processes used to control S02 emissions by commercial power plants is infurnace limestone injection. In accordance with this commercial process, limestone is injected into the commercial furnace where it reacts with sulfur oxides to form solid calcium sulfate. The solid calcium sulfate particles are thereafter separated from the flue gases by conventional particulate control devices. The major drawback of the limestone injection process for infurnace S02 capture is its low calcium utilization. While the amount of sulfur removed from the combustion products by in-furnace limestone injection is in the order of 50%, calcium utilization is in the order of only 15 to 25%. As a result, extremely large quantities of limestone must be injected per unit mass of sulfur contained in the fuel. This has proven to be quite costly.
Naturally, it would be highly desirable to provide a mechanism for removing effluents from industrial combustion streams in an economic manner.
It is an object of the invention to provide an improved process for the production of a metal-oxide aerosol.
According to one aspect of the invention there is provided a process for the production of- a metal-oxide aerosol from a corresponding metal comprising vaporizing said metal under vaporizing temperature conditions in a first zone at a temperature greater than or equal to T1, passing said metal vapor in a gaseous stream from said first zone to a second zone, and contacting said metal vapor with an oxidant in said second zone so as to oxidize said metal vapor to form an aerosol comprising solid metal-oxide particles in said gaseous stream.
The present invention may provide a process for the production of an effluent sorbent aerosol material.
It is an advantage of the present invention that it provides a process for the production of an effluent sorbent-oxide aerosol for removing acid gas effluent from a gaseous stream which is highly effective.
The present invention is drawn to a process for the production of a metaloxide aerosol from a corresponding metal and may be drawn to a process for utilizing the 1 i i i 9 i metal-oxide aerosol as an effluent sorbent. The process of the preferred embodiment of the present invention comprises vaporizing a metal of desired sorbent in an oxidant free environment and, preferably, in a gaseous stream of an inert gas under vaporizing temperature conditions at a temperature Tl in a first zone. In this embodiment, the vaporized metal gaseous stream is thereafter passed from the first zone to a second zone wherein the metal vapor stream is contacted with an oxidant so as to oxidize the metal vapor thereby forming an aerosol consisting of solid metal-oxide particles in a gaseous carrier stream. By controlling various parameters of the process, the size of the metal-oxide particles may be controlled so as to produce an optimized metal oxide aerosol. The metal oxide aerosol may thereafter be fed to a gaseous stream containing acid gas effluents and may be contacted L-herewith at a temperature suitable for the reaction between the metal oxide aerosol and the ef f luent to be captured so as to f orm a solid metal compound of the effluent.
Reference is now made to the accompanying drawings, in which - Figure 1 is a schematic illustration of the process of the present invention for producing a metal-oxide aerosol and for removing effluents from a gaseous stream using the metal-oxide aerosol; j Figure 2 is a graph illustrating the effluent absorption capabilities of the process of the present invention employing calcium as the sorbent metal and sulfur as the effluent; Figure 3 is a graph illustrating the effluent absorption capabilities of the process of the present invention employing magnesium as the sorbent metal and sulfur as the effluent.
The present invention relates to a process for the production of a metaloxide aerosol and a process for utilizing the metal-oxide aerosol so produced as an effluent sorbent. The process is particularly useful in removing acid gas effluents such as S02, S03, NO, N02, H2S and HCl which are by-products from various chemical reactions from the off gases of the chemical reactions.
The process of the present invention will be described in detail with reference to Figure 1 and the schematic illustrations shown therein.
The process of the present invention comprises the production of a metaloxide aerosol and its subsequent formation into a solid metal compound of the effluent being captured. While the process will be described and 1 illustrated employing sulfur as the effluent in a combustion gas stream, the process is useful in capturing all the acid gas effluents mentioned above which are by-products of numerous chemical reactions.
With reference to Figure 1, the metal-oxide aerosol is produced by vaporizing a metal of the desired sorbent under vaporizing temperature conditions in a vaporizing zone which is an oxidant free environment and thereafter passing the metal vapor so produced to an oxidizing zone wherein the metal vapor is contacted with an oxidant so as to produce a metal oxide aerosol.
In accordance with the process of the present invention, suitable sorbent metals for use in the process of the present invention are the metals selected from the group consisting of alkaline metals, alkaline earth metals, metals having a valence greater than or equal to the alkaline earth metals and mixtures thereof. Particularly suitable metals are magnesium and calcium with calcium being preferred. It is preferred in the process of the present invention to vaporize the desired metal sorbent in the vaporizing zone in a gaseous stream. It is necessary for Cne gaseous stream to be an inert gaseous stream and may be of any of the following gases: argon, helium, nitrogen, methane, etc. Preferred gases would be argon, nitrogen. Inert gases are required because the vaporization step must take place in a substantially oxidant free environment in order to insure complete vaporization of the metal sorbent. The use of an inert gaseous stream is desirable because it increases the amount of metal vapor in the gaseous stream, that is metal vapor load, which has a positive effect on the particle size on the metal. oxide produced. The flow rate of the gaseous stream should be adjusted so as to produce the desired aerosol characteristic for a suitable particle size of the metal oxide aerosol (smaller than a 0.1 mircon). The required inert gas flow should be adjusted to produce a metal vapor load of 5) g/Nm 3 to 250 g/Nm 3 and preferably 3 about 50 to 150 g/tim The inert gas flow rate depends on several factors such as metal vaiDorization temPerature.(T,), type of metal to be vaporized, quenching rate used in the aerosol formation step, desired aerosol primary particle size, among others. The inert gas flow rate used in the process of the present invention is preferably chosen to provide a suitable metal vapor load i:nat will subsequently produce an adequate aerosol primary particle size of about 0.05 microns mean diameter which is ideally suitable for obtaining a high metal utilization in the effluent absorption step.
i 1 J 1 i 1 i 1 r 1 In accordance with the present invention, it is necessary for the vaporization of the metal in the gaseous stream in the first zone of the furnace to be conducted at controlled temperature conditions T 1 at a pressure P 1 The temperature T 1 is the temperature that is necessary in order to obtain complete metal vaporization, that is, the melting point of the metal, and will vary depending on the metal sorbent to be vaporized. In addition, in order to obtain complete metal vaporization, the vaporizing zone must be substantially oxidant free. Furthermore, the temperature employed for vaporization is preferably significantly higher than the melting point of the metal sorbent employed. This is desirous because an increase in temperature T increases vapor load in the stream 1 fed to the oxidation zone which, as noted above, has a positive effect on the metal oxide particle size. For cost reasons, the temperature of vaporization should be below 2000'C. In accordance with the present invention the vaporization temperature is about between '0500 to 1200'C, preferably 10000 to 13000C for calcium and between 450 to 11SO'C, preferably 750' to 9SO'C for magnesium at atmospheric pressure.
Once the metal vapor is produced in the vaporizing zone, the metal vapor in the gaseous stream with or k without the inert gaseous stream is passed from the first zone of the furnace to a second zone. The metal vapor in the gaseous stream is contacted in the second zone of the furnace with an oxidant such as oxygen, air, CO 2 and the like so as to oxidize the metal vapor to form the aerosol of the present invention which comprises the metal-oxide particles in the gaseous stream of carrier gas. In accordance with the present invention, the formation of the aerosol stream in the second zone should be controlled as to produce the required particle size. It has been found that submicron particle sized metal oxide particles are desirable in order to obtain effective sorbent utilization and correspondingly good effluent capture. A mean particle size of less than 0.1 microns is preferred with particle sizes of less than 0.05 being ideal.
As noted above, t-he aerosol stream fed from the second zone is contacted with an effluent carrying gaseous stream in a third zone under controlled temperature conditions. The temperature at which the metal oxide aerosol contacts the effluent carrying gaseous stream must be within the temperature range suitable for thle reaction between the metal oxide aerosol and the effluent to be captured so as to form a solid metal compound of the effluent. For example, in j i i j the case of sulfur, the effluent absorption step is carried out under the following conditions: 650' to 12SO'C and preferably between about 9500C to 12000C for calcium oxide aerosol and about between 350' and 850'C and preferably between about 7000 and 8OCC for magnesium. These temperature ranges represent the practical and/or thermodynamic limits for the sulfation of calcium and magnesium oxides.
In accordance with the process of the present invention, sorbent utilization is greater than or equal to about 90% and 50% for Cao aerosol and MgO aerosol, respectively, for a gas stream containing about 2000 ppm of SO 2 The followina examples illustrate specific features of the process of the present invention but in no way are intended to be limiting.
EXAMPLE I
With reference to Figures 1 and 2, 3.5 g of calcium metal was fed to a vaporizing zone. Argon gas was fed to the zone at a gas flow rate of 16.5 ml/sec., a temperature of 25'C and 1 atm. pressure. The zone was heated 1 to a temperature of 1000. Under these conditions a steady production of an aerosol of about 5 mg/min. was measured. The aerosol stream was contacted i i i -10with. a stream of 54 1/min. of heated dry air at a temperature of 950C in an oxidation zone so as to produce a metal oxide aerosol of Cao. The aerosol was inje.cted into a gaseous stream having a measured amount of SO 2 and was contacted with the aerosol stream in an effluent absorption zone. Five separate runs were made with SO 2 concentrations measured in volume parts per million in the air of 250, 500, 750, 2000 and 3500. An electrostatic precipitator sampling probe was located at the end of the absorption zone to capture the aerosol samples. Aerosol samples were taken in order to determine the amount of calcium utilized in sulfur absorption. The results are shown in Figure 2. it is important to note that the residence time used in this experiment, about 0.5 seconds, is well within the time span spent by the flue gases inside industrial boilers to drop from 1200 to 9SO'C. Therefore, the results presented are well within the required industrial time frame. As can be seen from Figure 2, the calcium utilization is greater than 80% at SO 2 concentrations of above 1500 ppm which is far superior to that utilization obtained from in-furnace limestone injection processes. In addition to the foregoing, the temperature at which effluent absorption takes place, that is, 950C for calcium and 800'C for magnesium, are i i i i j i j much lower than those used in in-furnace limestone injection processes thereby making the process of the present invention even more attractive. Finally, the aver.age particle diameter of calcium oxide was measured and found to be 0.015 pm.
EXAMPLE II
The process of Example II was similar to that set forth above with regard to Example I but employed magnesium rather than calcium. The magnesium oxide aerosol was generated and then fed to the five. SO 2 containing air streams set forth above with regard to Example I. In order to vaporize magnesium, the temperature in the first zone was adjusted to 8SO'C. The results are set forth in Figure 3. It can be seen that an aerosol containing magnesium oxide particles is not as effective as an aerosol containing calcium oxide particles at low SO 2 concentrations of SO 2, however, the magnesium oxide aerosol is still superior to known infurnace limestone injection processes. The particle size of the magnesium oxide particle obtained in the aerosol in accordance with this example was 0.020 jim.
1
Claims (11)
1. A process f or the production of a metal-oxide aerosol. from a corresponding metal comprising vaporizing said metal under vaporizing temperature conditions in a first zone at a temperature greater than or equal to T1, passing said metal vapor in a gaseous stream from said f irst zone to a second zone, and contacting said metal vapor with an oxidant in said second zone so as to oxidize said metal vapor to form an aerosol comprising solid metal-oxide particles in said gaseous stream.
2. A process according to claim 1, wherein said metal is selected from the group consisting of alkaline metals, alkaline earth metals, metals having a valence greater than or equal to the alkaline earth metals and mixtures thereof.
3. A process according to claim 1 or 2. wherein said metal is selected from the group consisting of magnesium and calcium.
4. A process acording to claim 1, 2 or 3, wherein a gaseous stream of an inert gas is fd to said first zone during the vaporizing of said metal.
I i i i i i 1 i 1 1
5. A process according to claim 4, wherein the metal vapor load on said gaseous stream is between about 5 gINm3 to 250 g/Nm3.
6. A process according to any preceding claim, wherein temperature T1 is the melting temperature of the metal being vaporized.
7. A process wherein the metal is temperature is between atmospheric pressure.
8. wherein according to any preceding claim, magnesium and the vaporizing about 4500 to 1150oC at A process according to any of claims 1 to 6, the metal is calcium and the vaporizing temperature is between about 6500 to 13000C at atmospheric pressure.
9. A process according to any preceding claim, wherein said aerosol is characterized by a metal-oxide particle size of between about 0.001 to 1. 0 micrometer.
10. A process according to any preceding claim, further including the step of contacting said aerosol with an effluent containing gaseous stream under controlled temperature conditions whereby said metaloxide particles react with said effluent for absorbing same.
11. A process substantially as herein described with reference to and as shown in the accompanying drawings.
Published 1991 at The Patent Office. Concept House. Cardiff Road. Newport. Gwent NP9 1 RH. Further copies may be obtained from Sales Branch. Unit 6. Nine Mile Point. Cikmifelinfach. Cross Keys. Newlport. NPA 7HZ. Printed by Multiplex techniques lid. St Mary Cray. Kent.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US49889290A | 1990-03-26 | 1990-03-26 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB9015112D0 GB9015112D0 (en) | 1990-08-29 |
| GB2242421A true GB2242421A (en) | 1991-10-02 |
Family
ID=23982937
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB9015112A Withdrawn GB2242421A (en) | 1990-03-26 | 1990-07-09 | Process for the production of metal oxide aerosols |
Country Status (11)
| Country | Link |
|---|---|
| JP (1) | JPH03275506A (en) |
| BE (1) | BE1005343A4 (en) |
| BR (1) | BR9003819A (en) |
| CA (1) | CA2020501A1 (en) |
| DE (1) | DE4038195A1 (en) |
| DK (1) | DK160490A (en) |
| ES (1) | ES2020732A6 (en) |
| FR (1) | FR2659873A1 (en) |
| GB (1) | GB2242421A (en) |
| IT (1) | IT1241567B (en) |
| NL (1) | NL9001656A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011156906A2 (en) * | 2010-06-15 | 2011-12-22 | Et-Energy Corp. | Process for treating a flue gas |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5499587A (en) * | 1986-06-17 | 1996-03-19 | Intevep, S.A. | Sulfur-sorbent promoter for use in a process for the in-situ production of a sorbent-oxide aerosol used for removing effluents from a gaseous combustion stream |
| JP4195278B2 (en) * | 2002-12-02 | 2008-12-10 | 宇部マテリアルズ株式会社 | Metallic magnesium melt evaporation apparatus and method for producing high-purity magnesium oxide fine powder using the same |
| JP4855452B2 (en) * | 2008-08-25 | 2012-01-18 | 宇部マテリアルズ株式会社 | Metallic magnesium melt evaporation apparatus and method for producing high-purity magnesium oxide fine powder using the same |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1150506A (en) * | 1966-02-03 | 1969-04-30 | Varta Ag | Powder produced by Vibrated Action upon a Metal Melt with Atomization of the Metal, and a method for its production |
| GB1366104A (en) * | 1970-11-20 | 1974-09-11 | American Cyanamid Co | Submicron metal oxide particles and their process for manufacture |
| GB2141701A (en) * | 1983-05-20 | 1985-01-03 | Ube Industries | Process and apparatus for producing a high purity magnesia fine powder |
| GB2168767A (en) * | 1984-12-20 | 1986-06-25 | Dana Corp | Port baffle for engine gasket |
| GB2183622A (en) * | 1985-10-29 | 1987-06-10 | Ube Industries | Process and apparatus for producing high purity magnesium oxide fine particles |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60161329A (en) * | 1984-01-26 | 1985-08-23 | Ube Ind Ltd | Preparation of fine calcia powder having high purity |
| JPS60175537A (en) * | 1984-02-22 | 1985-09-09 | Toyota Motor Corp | Preparation of ultra-fine ceramic particles |
| JPS61122106A (en) * | 1984-11-19 | 1986-06-10 | Ube Ind Ltd | Method for producing finely powdered magnesium oxide |
| JPS6243928A (en) * | 1985-08-21 | 1987-02-25 | Matsushita Electric Ind Co Ltd | Digital communication method |
| US4726940A (en) * | 1986-05-21 | 1988-02-23 | Hitachi Zosen Corporation | Method of purifying exhaust gas |
| JPS6458131A (en) * | 1987-08-28 | 1989-03-06 | Tokyo Electric Co Ltd | Data transmission system |
| JP2792046B2 (en) * | 1987-10-09 | 1998-08-27 | 住友化学工業株式会社 | Optically active amine-boron compound, asymmetric reducing agent containing the same as an active ingredient, and method for producing optically active compound using the same |
-
1990
- 1990-07-03 DK DK160490A patent/DK160490A/en not_active IP Right Cessation
- 1990-07-05 CA CA002020501A patent/CA2020501A1/en not_active Abandoned
- 1990-07-09 GB GB9015112A patent/GB2242421A/en not_active Withdrawn
- 1990-07-19 NL NL9001656A patent/NL9001656A/en not_active Application Discontinuation
- 1990-08-03 BR BR909003819A patent/BR9003819A/en not_active Application Discontinuation
- 1990-08-07 ES ES9002138A patent/ES2020732A6/en not_active Expired - Fee Related
- 1990-09-21 IT IT67707A patent/IT1241567B/en active IP Right Grant
- 1990-10-03 FR FR9012186A patent/FR2659873A1/en active Pending
- 1990-10-12 BE BE9000969A patent/BE1005343A4/en not_active IP Right Cessation
- 1990-11-28 JP JP2328760A patent/JPH03275506A/en active Pending
- 1990-11-30 DE DE4038195A patent/DE4038195A1/en not_active Withdrawn
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1150506A (en) * | 1966-02-03 | 1969-04-30 | Varta Ag | Powder produced by Vibrated Action upon a Metal Melt with Atomization of the Metal, and a method for its production |
| GB1366104A (en) * | 1970-11-20 | 1974-09-11 | American Cyanamid Co | Submicron metal oxide particles and their process for manufacture |
| GB2141701A (en) * | 1983-05-20 | 1985-01-03 | Ube Industries | Process and apparatus for producing a high purity magnesia fine powder |
| GB2168767A (en) * | 1984-12-20 | 1986-06-25 | Dana Corp | Port baffle for engine gasket |
| GB2183622A (en) * | 1985-10-29 | 1987-06-10 | Ube Industries | Process and apparatus for producing high purity magnesium oxide fine particles |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011156906A2 (en) * | 2010-06-15 | 2011-12-22 | Et-Energy Corp. | Process for treating a flue gas |
| WO2011156906A3 (en) * | 2010-06-15 | 2012-02-09 | Et-Energy Corp. | Process for treating a flue gas |
| US8758710B2 (en) | 2010-06-15 | 2014-06-24 | E.T. Energy Corp. | Process for treating a flue gas |
Also Published As
| Publication number | Publication date |
|---|---|
| IT1241567B (en) | 1994-01-18 |
| BE1005343A4 (en) | 1993-07-06 |
| DE4038195A1 (en) | 1991-10-02 |
| DK160490A (en) | 1991-09-27 |
| JPH03275506A (en) | 1991-12-06 |
| FR2659873A1 (en) | 1991-09-27 |
| NL9001656A (en) | 1991-10-16 |
| GB9015112D0 (en) | 1990-08-29 |
| ES2020732A6 (en) | 1991-09-01 |
| CA2020501A1 (en) | 1991-09-27 |
| IT9067707A1 (en) | 1992-03-21 |
| DK160490D0 (en) | 1990-07-03 |
| BR9003819A (en) | 1991-11-12 |
| IT9067707A0 (en) | 1990-09-21 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| WAP | Application withdrawn, taken to be withdrawn or refused ** after publication under section 16(1) |