CA1290922C - Method of purifying exhaust gas - Google Patents
Method of purifying exhaust gasInfo
- Publication number
- CA1290922C CA1290922C CA000477363A CA477363A CA1290922C CA 1290922 C CA1290922 C CA 1290922C CA 000477363 A CA000477363 A CA 000477363A CA 477363 A CA477363 A CA 477363A CA 1290922 C CA1290922 C CA 1290922C
- Authority
- CA
- Canada
- Prior art keywords
- exhaust gas
- absorbent
- dividing
- dispersing device
- fine particles
- 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.)
- Expired - Fee Related
Links
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
- B01D53/68—Halogens or halogen compounds
Abstract
ABSTRACT OF THE DISCLOSURE
A method of purifying an exhaust gas characterized by dispersing individually independent fine particles of a Ca-type absorbent in a carrier gas to a high concentration by a dividing-dispersing device to which the carrier gas and the absorbent are supplied, the absorbent being up to 10 microns in mean particle diameter, introducing the resulting aerosol of high concentration into the exhaust gas to uniformly mix the aerosol with the exhaust gas and thereafter introducing the exhaust gas into a dust collector, whereby the fine particles of absorbent absorbing harmful acid substances from the exhaust gas are removed together with dust and soot. The absorbent forming secondary agglomerates before reaching the dividing-dispersing device are divided into individually independent primary particles and then dispersed in the carrier gas by the device, so that when introduced into the exhaust gas, the absorbent reacts with the harmful acid substance over an increased area of contact to achieve an improved removal efficiency.
A method of purifying an exhaust gas characterized by dispersing individually independent fine particles of a Ca-type absorbent in a carrier gas to a high concentration by a dividing-dispersing device to which the carrier gas and the absorbent are supplied, the absorbent being up to 10 microns in mean particle diameter, introducing the resulting aerosol of high concentration into the exhaust gas to uniformly mix the aerosol with the exhaust gas and thereafter introducing the exhaust gas into a dust collector, whereby the fine particles of absorbent absorbing harmful acid substances from the exhaust gas are removed together with dust and soot. The absorbent forming secondary agglomerates before reaching the dividing-dispersing device are divided into individually independent primary particles and then dispersed in the carrier gas by the device, so that when introduced into the exhaust gas, the absorbent reacts with the harmful acid substance over an increased area of contact to achieve an improved removal efficiency.
Description
12~V~Z~::
~ETHOD OF PURIFYING EXHAUST GAS
The present invention relates to a dry method of purifying exhaust gases wherein an absorbent of the Ca type is used for absorbing and removing harmful acid substances from the exhaust gas.
Hot exhaust gases discharged from boilers or incinerators for waste materials usually contain 10 to 2000 ppm of harmful acid substances such as sulf~r oxides (SOx), hdyrogen chloride (HCl) and hydrogen fluoride (HF). It is required to remove such substances under pollution control regulations. These harmful acid substances have~heretofore been removed generally by the wet method wherein an absorbing liquid or slurry containing an alkaline absorbent is brought into direct contact with the exhaust gas as cooled to a lower temperature to purify the gas. Although achieving a high removal efficiency, this method has the problem of involving difficulties in treating the resulting waste water, necessitating reheating of the exhaust gas and being expensive in equipment and running costs.
In view of the above problem, various methods have been investigated as substitutes for the wet method. For example, it has been proposed to adsorb harmful substances by active carbon, followed by desorption, or to spray a slurry of slaked lime into the exhaust gas as a semi~wet '~
~9o9~
method. However, these methods still fail to achieve high removal efficiencies. Although research was conducted on a dry method wherein particles of a Ca-type absorbent (quick lime, slaked lime, limestone, dolomite or the like) are diffused through the interior of a hot furnace or flue, this method has not been practiced except where the environ-mental regulations are extremely slack as a special case, because the absorbent is low in reactivity. For example, the reactivity between the absorbent and Sx is up to about 20% if highest, while that of the absorbent with HCl is not higher than 50%. It is generally expected that the reactivity will improve with decreasing particle size, whereas a reduction in the particle size does not lead to a noticeable increase in the reactivity of lime.
An object of the present invention is to provide a dry method of purifying exhaust gases which assures an improved reactivity between a Ca-type absorbent, such as slaked lime or quick lime, and harmful acid substances.
To fulfil the above object, the present invention provides a method of purifying an exhaust gas having a temperature in a range selected from the group consisting of about 150 to 400C and about 900 to 1200C, characterized by dispersing individually independent fine particles of a Ca-type absorbent in a carrier gas to a concentration in the range of about 50 to 500 g/Nm3 by a dividing-dispersing device to which the carrier gas and the absorbent are supplied, the ~ .
~9()~ZZ
absorbent being up to 10 microns in mean particle diameter, introducing the resulting aerosol into the exhaust gas having said temperature to uniformly mix the aerosol with the exhaust gas and to produce a particle concentration in the exhaust gas of about 1 to 20 g/Nm3 and thereafter introducing the exhaust gas into a dust collector, whereby the fine particles of absorbent absorbing harmful acid substances from the exhaust gas are removed together with dust and soot.
The principle and embodiments of the present invention will be described below with reference to the accompanying drawings, in which:
Fig. 1 is a graph showing the relationship between the mean diameter of particles and the apparent cohesiveness thereof;
Fig. 2 is a diagram schematically showing an embodiment of system for practicing the method of the present invention;
; Fig. 3 is an enlarged fragmentary view in section showing the system;
Fig. 4 is a view in longitudinal section showing an injector which is an example of dividing-dispersing device for use in the system;
Fig. 5 is a view in longitudinal section showing an orifice tube which is another example of dividing-dispersing device for use in the system;
Fig. 6 is a graph showing the relationship between the mean particle diameter of a Ca-type absorbent (slaked ~J
lX909~2 lime) and the HCl removal ratio thereof; and Fig. 7 is a graph showing the relationship between the mean particle diameter of the absorbent (slaked lime) and the Sx removal ratio thereof.
First, the principle of the present invention will be described.
Generally, individually independent fine particles (hereinafter referred to as "primary particles") of the order of microns in size tend to agglomerate. This tendency increases as the particle size decreases as shown in Fig. 1.
Accordingly, when particles of 1 to 2 microns in size are sprayed into an exhaust gas through a mere pipe or nozzle as in the conventional dry method, these primary particles form secondary agglomerates before being dispersed into the exhaust gas, so that the primary particles behave as coarse particles in the exhaust gas. With the conventional method, therefore, the absorbent failed to achieve noticeably improved reactivity even when reduced in particle size.
On the other hand, it is known that secondary agglomerates, when given a definite amount of dispersing energy in a gas stream, are dispersed in the stream as divided into individual primary particles. From this viewpoint, it is useful to insert a Venturi (means for giving the dispersing energy), for example, in an exhaust gas channel and to spray an absorbent, which is already in the form of secondary ~9092Z
agglomerates, into the channel at a location upstream from the Venturi. The absor~ent can then be divided into primary particles before being uniformly mixed with the exhaust gas to consequently remove harmful acid substances with an improved efficiency. However, to divide secondary agglomerates into the original primary particles, for example, of up to 5 microns in size, it is required to use a greatly constricted Venturi and to increase the velocity of the exhaust gas to as high as several tens to 300 m/sec.
This entails a great pressure loss. Accordingly, to give an increased velocity to the exhaust gas itself which originally is in a large amount requires a great power consumption and therefore is not practical. According to the present inven-tion, an absorbent and a carrier gas are supplied to a dividing-dispersing device which is used for dispersing primary particles of the absorbent in the carrier gas flowing in a small amount at a high speed to obtain an aerosol of high particle concentration, which is then uniformly mixed with an exhaust gas. Thus, a high removal efficiency or ratio can be achieved with small power consumption.
Next, embodiments of the invention will be described.
With reference to Fig. 2, an exhaust gas 1 released from an unillustrated boiler or waste material incinerator through an exhaust gas channel is introduced into a mixing portion 2 provided in the channel. On the ~ ~9092~
other hand, a carrier gas 4 and a Ca-type absorbent S are fed to a dividing-dispersing device 3, which divides the absorbent S into primary particles and disperses them in the carrier gas 4 to a high concentration. The aerosol of high concentration from the device 3 is introduced into the mixing portion 2, where the aerosol is uniformly mixed with the exhaust gas 1. The Ca-type absorbent (e.g. quick lime or slaked lime) reacts with the harmful acid substances (e.g. SO2 and HC1) in the exhaust gas according to the 0 following equations.
CaO + SO2 + 12 2 CaSO4 Ca(OH) + SO + 12 2 - CaSO4 + H2O
CaO + 2HC1 CaC12 + H2O
Ca(OH)2 + 2HCl - CaC12 15 The absorber thus absorbing the harmful acid substances is collected by a dust collector 6 along with soot, dust, etc.
and discharged from a lower portion of the dust collector 6 as indicated at 7. On the other hand, the purified exhaust gas is released to the atmosphere through a chimney 8.
With the system described above, the concentration of primary particles of the absorbent in the carrier gas is 50 to 500 g/Nm3, whereas the absorbent primary particle concentration of the exhaust gas after the mixing has been reduced to 1 to 20 g/Nm3. In other words, the amount of carrier gas can be as small as 1/25 to 1/50 of the amount of ~X90922 exhaust gas. Thus, the amount of power consumption in this case is much smaller than when the exhaust gas itself is caused to flow at an increased velocity. Furthermore, the decrease of the concentration due to the mixing reduces the frequency of collision of the absorbent 2rimary particles, consequently reducing the likelihood that the primary particles will re-agglomerate.
Usable as the dividing-dispersing device 3 is an injector, orifice tube, Venturi tube, jet mill, mechanical crusher permitting the carrier gas to flow therethrough and having a dispersing function, or the like. As shown in Fig. 4, the injector comprises an innter tube 9 and an outer tube 10.
The carrier gas 4 is caused to jet out from the inner tube 9 and thereby given a higher velocity. The negative pressure produced in the outlet portion of the outer tube 10 draws out secondary agglomerates 5a of the absorbent 5 from a duct lOa, divides them into primary particles 5b in the outlet portion and disperses the particles in the carriergas. As shown in Fig. 5, the orifice tube comprises a tube 11 to which the carrier gas 4 and the absorbent 5 in the form of secondary agglomerates 5a are supplied, and an orifice member having an orifice 12. The carrier gas having the secondary agglomerates entrained therein is given an increased velocity when passing through the orifice 12, whereby the agglomerates are divided into primary particles 5b, which ~ X909~2 are dispersed in the carrier gas. The Venturi tube has the same construction as shown in Fig. 5 except that the orifice member is replaced by a Venturi. The tube operates on the same principle as the tube of Fig. 5. In the jet mill, solids as entrained in a carrier gas are caused to collide with one another and thereby reduced to smaller sizes.
Secondary agglomerates can be thereby divided into the original primary particles of specified size, or primary particles so sized as not to form secondary agglomerates can be divided into smaller primary particles. The mechani-cal crusher is used solely for dividing coarse particles into primary particles of specified size and dispersing them in a gas. In any case, the primary particles to be eventually dispersed in the carrier gas need to be up to lO microns in mean diameter. For the present method to remove harmful acid substances with as high an efficiency as the wet method, it is required that the primary particles be up to 5 microns in mean diameter for removing HCl and l to 3 microns in mean diameter when removing SOx.
In practicing the method of the present invention, it is essential to assure that the primary particles of the absorbent once dispersed will not re-agglomerate. For this purpose, it is required to minimize the length of the high-concentration aerosol channel from the dividing-dispersing -device 3 to the mixing portion 2 and to eliminate a greatly -1.~90!~2 bent portion from this channel to thereby preclude anyturbulence. vihen an injector, orifice tube or Venturi tube is used as the dividing-dispersing device 3, the device is preferably so disposed as shown in Fig. 3. In this arrange-ment, the device 3 is attached directly to a bent portion 13aof the exhaust gas channel 13, and the outlet of the device 3 is oriented in the same direction as the flow of exhaust gas flowing downward from the bent portion 13a. Accordingly, the primary particles 5b from the dividing-dispersing device 3 is sprayed directly into the mixing portion 2 without being passed through an intermediate conduit. This almost completely eliminates the likelihood of re-agglomeration.
Preferably, the mixing portion 2 is provided with a diffuser 2a for promoting the dispersion of primary particles 5b in the exhaust gas 1. The portion of the exhaust gas channel 13 from the bent portion 13a to the dust collector 6 has a space of such a volume that the primary particles 5b will be suspended in the exhaust gas 1 for about 1 to about 3 seconds before reaching the dust collector 6. The diffuser 2a, although basically the same as the Venturi, is not intended to give an increased velocity to the exhaust gas 1 and thereby divide secondary agglomerates into primary particles, therefore is not greatly constricted and does not give rise to the problem of pressure loss substantially. Primary particles of the absorbent can be sprayed into the boiler 0~92~
or the waste material incinerator.
Examples of Ca-type absorbents usable in a high temprature range of 900 to 1200 C are limestone [chiefly CaCO3], quick lime [CaO], slaked lime [CaOH], dolomite [CaMg(CO3)2], calcined dolomite [CaMgO2] and slaked dolomite [CaMg(OH)4]. At high temperatures of 900 to 1200 C, lime-stone, slaked lime, dolomite and slaked dolomite instantaneously undergo thermal decomposition (with release of H2O, CO2) to form porous, highly reactive quick lime or calcined dolomite, so that these materials afford better results than quick lime and calcined dolomite (commercial product is usually crystallized). When used at temperatures above 1200 C, quick lime and calcined become progressively crystallized and therefore lower in reactivity. On the other hand, examples of Ca-type absorbers usable in a temperature range of 150 to 400 C are quick lime, slaked lime, calcined dolomite and slaked dolomite, among which slaked lime and slaked dolomite are preferable to use.
Usually, a bag filter or electrical precipitator is used as the dust collector 6.
The advantages of the present methQd will become apparent from the following examples.
Example 1 Slaked lime was used as a Ca-type absorber for the system of Fig. 2, in which the dividing-dispersing device ~ X9092~
was an injector (Model TB-1, product of Atsuji Tekko Co., Ltd.) for preparing an aerosol of high concentration. The injector was inserted in an exhaust gas duct through which a simulated exhaust gas having a temperature of 250 C and containing about 1000 ppm of HCl was flowing, with the outlet of the injector oriented in the direction of flow of the exahust gas. To mix the aerosol with the exhaust gas effectively, the exhaust gas duct was constricted at a location immediately downstream from the injector to form a diffuser. The injector was operated by passing compressed air having a pressure of 5 kg/cm G at a flow rate of 6.0 Nm /hr, and slaked lime was thereby sprayed into the exhaust gas duct at a rate of 5 kg/hr. It took about 2 seconds for the primary particles of slaked lime to reach the dust collector.
The above procedure was repeated with use of slaked limes of varying particle sizes (primary particles of varying diameters). Fig. 6 shows the results.
In Fig. 6, indicated at A are HC1 removal ratios achieved by slaked lime according to the method of the invention, and at B HCl removal ratios achieved by slaked lime according to the conventional dry method. It is seen that the reactivity improves with decreasing particle size more remarkably in the case of the invention than with the conventional method.
~2~0922 Example 2 The same procedure as in Example l was repeated with the exception of the following.
Simulated exhaust gas Contained substance: about 1000 ppm of Sx Temperature: about llOO C
Flow rate: about l900 Nm3/hr Injector Air flow rate: 6.3 Nm /hr Rate of spray of particles: 7.4 kg/hr Fig. 7 shows the results achieved by the above experiment. Indicated at A' and B' in Fig. 7 are the results achieved by the invention and the conventional method, respectively. It is seen that the method of the invention is effective also on SOx.
~ETHOD OF PURIFYING EXHAUST GAS
The present invention relates to a dry method of purifying exhaust gases wherein an absorbent of the Ca type is used for absorbing and removing harmful acid substances from the exhaust gas.
Hot exhaust gases discharged from boilers or incinerators for waste materials usually contain 10 to 2000 ppm of harmful acid substances such as sulf~r oxides (SOx), hdyrogen chloride (HCl) and hydrogen fluoride (HF). It is required to remove such substances under pollution control regulations. These harmful acid substances have~heretofore been removed generally by the wet method wherein an absorbing liquid or slurry containing an alkaline absorbent is brought into direct contact with the exhaust gas as cooled to a lower temperature to purify the gas. Although achieving a high removal efficiency, this method has the problem of involving difficulties in treating the resulting waste water, necessitating reheating of the exhaust gas and being expensive in equipment and running costs.
In view of the above problem, various methods have been investigated as substitutes for the wet method. For example, it has been proposed to adsorb harmful substances by active carbon, followed by desorption, or to spray a slurry of slaked lime into the exhaust gas as a semi~wet '~
~9o9~
method. However, these methods still fail to achieve high removal efficiencies. Although research was conducted on a dry method wherein particles of a Ca-type absorbent (quick lime, slaked lime, limestone, dolomite or the like) are diffused through the interior of a hot furnace or flue, this method has not been practiced except where the environ-mental regulations are extremely slack as a special case, because the absorbent is low in reactivity. For example, the reactivity between the absorbent and Sx is up to about 20% if highest, while that of the absorbent with HCl is not higher than 50%. It is generally expected that the reactivity will improve with decreasing particle size, whereas a reduction in the particle size does not lead to a noticeable increase in the reactivity of lime.
An object of the present invention is to provide a dry method of purifying exhaust gases which assures an improved reactivity between a Ca-type absorbent, such as slaked lime or quick lime, and harmful acid substances.
To fulfil the above object, the present invention provides a method of purifying an exhaust gas having a temperature in a range selected from the group consisting of about 150 to 400C and about 900 to 1200C, characterized by dispersing individually independent fine particles of a Ca-type absorbent in a carrier gas to a concentration in the range of about 50 to 500 g/Nm3 by a dividing-dispersing device to which the carrier gas and the absorbent are supplied, the ~ .
~9()~ZZ
absorbent being up to 10 microns in mean particle diameter, introducing the resulting aerosol into the exhaust gas having said temperature to uniformly mix the aerosol with the exhaust gas and to produce a particle concentration in the exhaust gas of about 1 to 20 g/Nm3 and thereafter introducing the exhaust gas into a dust collector, whereby the fine particles of absorbent absorbing harmful acid substances from the exhaust gas are removed together with dust and soot.
The principle and embodiments of the present invention will be described below with reference to the accompanying drawings, in which:
Fig. 1 is a graph showing the relationship between the mean diameter of particles and the apparent cohesiveness thereof;
Fig. 2 is a diagram schematically showing an embodiment of system for practicing the method of the present invention;
; Fig. 3 is an enlarged fragmentary view in section showing the system;
Fig. 4 is a view in longitudinal section showing an injector which is an example of dividing-dispersing device for use in the system;
Fig. 5 is a view in longitudinal section showing an orifice tube which is another example of dividing-dispersing device for use in the system;
Fig. 6 is a graph showing the relationship between the mean particle diameter of a Ca-type absorbent (slaked ~J
lX909~2 lime) and the HCl removal ratio thereof; and Fig. 7 is a graph showing the relationship between the mean particle diameter of the absorbent (slaked lime) and the Sx removal ratio thereof.
First, the principle of the present invention will be described.
Generally, individually independent fine particles (hereinafter referred to as "primary particles") of the order of microns in size tend to agglomerate. This tendency increases as the particle size decreases as shown in Fig. 1.
Accordingly, when particles of 1 to 2 microns in size are sprayed into an exhaust gas through a mere pipe or nozzle as in the conventional dry method, these primary particles form secondary agglomerates before being dispersed into the exhaust gas, so that the primary particles behave as coarse particles in the exhaust gas. With the conventional method, therefore, the absorbent failed to achieve noticeably improved reactivity even when reduced in particle size.
On the other hand, it is known that secondary agglomerates, when given a definite amount of dispersing energy in a gas stream, are dispersed in the stream as divided into individual primary particles. From this viewpoint, it is useful to insert a Venturi (means for giving the dispersing energy), for example, in an exhaust gas channel and to spray an absorbent, which is already in the form of secondary ~9092Z
agglomerates, into the channel at a location upstream from the Venturi. The absor~ent can then be divided into primary particles before being uniformly mixed with the exhaust gas to consequently remove harmful acid substances with an improved efficiency. However, to divide secondary agglomerates into the original primary particles, for example, of up to 5 microns in size, it is required to use a greatly constricted Venturi and to increase the velocity of the exhaust gas to as high as several tens to 300 m/sec.
This entails a great pressure loss. Accordingly, to give an increased velocity to the exhaust gas itself which originally is in a large amount requires a great power consumption and therefore is not practical. According to the present inven-tion, an absorbent and a carrier gas are supplied to a dividing-dispersing device which is used for dispersing primary particles of the absorbent in the carrier gas flowing in a small amount at a high speed to obtain an aerosol of high particle concentration, which is then uniformly mixed with an exhaust gas. Thus, a high removal efficiency or ratio can be achieved with small power consumption.
Next, embodiments of the invention will be described.
With reference to Fig. 2, an exhaust gas 1 released from an unillustrated boiler or waste material incinerator through an exhaust gas channel is introduced into a mixing portion 2 provided in the channel. On the ~ ~9092~
other hand, a carrier gas 4 and a Ca-type absorbent S are fed to a dividing-dispersing device 3, which divides the absorbent S into primary particles and disperses them in the carrier gas 4 to a high concentration. The aerosol of high concentration from the device 3 is introduced into the mixing portion 2, where the aerosol is uniformly mixed with the exhaust gas 1. The Ca-type absorbent (e.g. quick lime or slaked lime) reacts with the harmful acid substances (e.g. SO2 and HC1) in the exhaust gas according to the 0 following equations.
CaO + SO2 + 12 2 CaSO4 Ca(OH) + SO + 12 2 - CaSO4 + H2O
CaO + 2HC1 CaC12 + H2O
Ca(OH)2 + 2HCl - CaC12 15 The absorber thus absorbing the harmful acid substances is collected by a dust collector 6 along with soot, dust, etc.
and discharged from a lower portion of the dust collector 6 as indicated at 7. On the other hand, the purified exhaust gas is released to the atmosphere through a chimney 8.
With the system described above, the concentration of primary particles of the absorbent in the carrier gas is 50 to 500 g/Nm3, whereas the absorbent primary particle concentration of the exhaust gas after the mixing has been reduced to 1 to 20 g/Nm3. In other words, the amount of carrier gas can be as small as 1/25 to 1/50 of the amount of ~X90922 exhaust gas. Thus, the amount of power consumption in this case is much smaller than when the exhaust gas itself is caused to flow at an increased velocity. Furthermore, the decrease of the concentration due to the mixing reduces the frequency of collision of the absorbent 2rimary particles, consequently reducing the likelihood that the primary particles will re-agglomerate.
Usable as the dividing-dispersing device 3 is an injector, orifice tube, Venturi tube, jet mill, mechanical crusher permitting the carrier gas to flow therethrough and having a dispersing function, or the like. As shown in Fig. 4, the injector comprises an innter tube 9 and an outer tube 10.
The carrier gas 4 is caused to jet out from the inner tube 9 and thereby given a higher velocity. The negative pressure produced in the outlet portion of the outer tube 10 draws out secondary agglomerates 5a of the absorbent 5 from a duct lOa, divides them into primary particles 5b in the outlet portion and disperses the particles in the carriergas. As shown in Fig. 5, the orifice tube comprises a tube 11 to which the carrier gas 4 and the absorbent 5 in the form of secondary agglomerates 5a are supplied, and an orifice member having an orifice 12. The carrier gas having the secondary agglomerates entrained therein is given an increased velocity when passing through the orifice 12, whereby the agglomerates are divided into primary particles 5b, which ~ X909~2 are dispersed in the carrier gas. The Venturi tube has the same construction as shown in Fig. 5 except that the orifice member is replaced by a Venturi. The tube operates on the same principle as the tube of Fig. 5. In the jet mill, solids as entrained in a carrier gas are caused to collide with one another and thereby reduced to smaller sizes.
Secondary agglomerates can be thereby divided into the original primary particles of specified size, or primary particles so sized as not to form secondary agglomerates can be divided into smaller primary particles. The mechani-cal crusher is used solely for dividing coarse particles into primary particles of specified size and dispersing them in a gas. In any case, the primary particles to be eventually dispersed in the carrier gas need to be up to lO microns in mean diameter. For the present method to remove harmful acid substances with as high an efficiency as the wet method, it is required that the primary particles be up to 5 microns in mean diameter for removing HCl and l to 3 microns in mean diameter when removing SOx.
In practicing the method of the present invention, it is essential to assure that the primary particles of the absorbent once dispersed will not re-agglomerate. For this purpose, it is required to minimize the length of the high-concentration aerosol channel from the dividing-dispersing -device 3 to the mixing portion 2 and to eliminate a greatly -1.~90!~2 bent portion from this channel to thereby preclude anyturbulence. vihen an injector, orifice tube or Venturi tube is used as the dividing-dispersing device 3, the device is preferably so disposed as shown in Fig. 3. In this arrange-ment, the device 3 is attached directly to a bent portion 13aof the exhaust gas channel 13, and the outlet of the device 3 is oriented in the same direction as the flow of exhaust gas flowing downward from the bent portion 13a. Accordingly, the primary particles 5b from the dividing-dispersing device 3 is sprayed directly into the mixing portion 2 without being passed through an intermediate conduit. This almost completely eliminates the likelihood of re-agglomeration.
Preferably, the mixing portion 2 is provided with a diffuser 2a for promoting the dispersion of primary particles 5b in the exhaust gas 1. The portion of the exhaust gas channel 13 from the bent portion 13a to the dust collector 6 has a space of such a volume that the primary particles 5b will be suspended in the exhaust gas 1 for about 1 to about 3 seconds before reaching the dust collector 6. The diffuser 2a, although basically the same as the Venturi, is not intended to give an increased velocity to the exhaust gas 1 and thereby divide secondary agglomerates into primary particles, therefore is not greatly constricted and does not give rise to the problem of pressure loss substantially. Primary particles of the absorbent can be sprayed into the boiler 0~92~
or the waste material incinerator.
Examples of Ca-type absorbents usable in a high temprature range of 900 to 1200 C are limestone [chiefly CaCO3], quick lime [CaO], slaked lime [CaOH], dolomite [CaMg(CO3)2], calcined dolomite [CaMgO2] and slaked dolomite [CaMg(OH)4]. At high temperatures of 900 to 1200 C, lime-stone, slaked lime, dolomite and slaked dolomite instantaneously undergo thermal decomposition (with release of H2O, CO2) to form porous, highly reactive quick lime or calcined dolomite, so that these materials afford better results than quick lime and calcined dolomite (commercial product is usually crystallized). When used at temperatures above 1200 C, quick lime and calcined become progressively crystallized and therefore lower in reactivity. On the other hand, examples of Ca-type absorbers usable in a temperature range of 150 to 400 C are quick lime, slaked lime, calcined dolomite and slaked dolomite, among which slaked lime and slaked dolomite are preferable to use.
Usually, a bag filter or electrical precipitator is used as the dust collector 6.
The advantages of the present methQd will become apparent from the following examples.
Example 1 Slaked lime was used as a Ca-type absorber for the system of Fig. 2, in which the dividing-dispersing device ~ X9092~
was an injector (Model TB-1, product of Atsuji Tekko Co., Ltd.) for preparing an aerosol of high concentration. The injector was inserted in an exhaust gas duct through which a simulated exhaust gas having a temperature of 250 C and containing about 1000 ppm of HCl was flowing, with the outlet of the injector oriented in the direction of flow of the exahust gas. To mix the aerosol with the exhaust gas effectively, the exhaust gas duct was constricted at a location immediately downstream from the injector to form a diffuser. The injector was operated by passing compressed air having a pressure of 5 kg/cm G at a flow rate of 6.0 Nm /hr, and slaked lime was thereby sprayed into the exhaust gas duct at a rate of 5 kg/hr. It took about 2 seconds for the primary particles of slaked lime to reach the dust collector.
The above procedure was repeated with use of slaked limes of varying particle sizes (primary particles of varying diameters). Fig. 6 shows the results.
In Fig. 6, indicated at A are HC1 removal ratios achieved by slaked lime according to the method of the invention, and at B HCl removal ratios achieved by slaked lime according to the conventional dry method. It is seen that the reactivity improves with decreasing particle size more remarkably in the case of the invention than with the conventional method.
~2~0922 Example 2 The same procedure as in Example l was repeated with the exception of the following.
Simulated exhaust gas Contained substance: about 1000 ppm of Sx Temperature: about llOO C
Flow rate: about l900 Nm3/hr Injector Air flow rate: 6.3 Nm /hr Rate of spray of particles: 7.4 kg/hr Fig. 7 shows the results achieved by the above experiment. Indicated at A' and B' in Fig. 7 are the results achieved by the invention and the conventional method, respectively. It is seen that the method of the invention is effective also on SOx.
Claims (13)
1. A method of purifying an exhaust gas having a temperature in a range selected from the group consisting of about 150 to 400°C and about 900 to 1200°C, characterized by dispersing individually independent fine particles of a Ca-type absorbent in a carrier gas to a concentration in the range of about 50 to 500 g/Nm3 by a dividing-dispersing device to which the carrier gas and the absorbent are supplied, the absorbent being up to 10 microns in mean particle diameter, introducing the resulting aerosol into the exhaust gas having said temperature to uniformly mix the aerosol with the exhaust gas and to produce a particle concentration in the exhaust gas of about 1 to 20 g/Nm3 and thereafter introducing the exhaust gas into a dust collector, whereby the fine particles of absorbent absorbing harmful acid substances from the exhaust gas are removed together with dust and soot.
2. A method as defined in claim 1 wherein the exhaust gas has a temperature of 900 to 1200°C, and the Ca-type absor-bent is at least one member selected from the group con-sisting of limestone, quick lime, slaked lime, dolomite, calcined dolomite and slaked dolomite.
3. A method as defined in claim 1 wherein the exhaust gas has a temperature of 150 to 400°C, and the Ca-type absor-bent is at least one member selected from the group consisting of quick lime, slaked lime, calcined dolomite and slaked dolomite.
4. A method as defined in claim 1, 2 or 3 wherein the Ca-type absorbent fine particles are up to 5 microns in mean diameter.
5. A method as defined in claim 1, 2 or 3 wherein the Ca-type absorbent fine particles are 1 to 3 microns in mean diameter.
6. A method as defined in claim 1, 2 or 3 wherein the dividing-dispersing device is an injector.
7. A method as defined in claim 1, 2 or 3 wherein the dividing-dispersing device is a pipe having an orifice.
8. A method as defined in claim 1, 2 or 3 wherein the dividing-dispersing device is a Venturi tube.
9. A method as defined in claim 1, 2 or 3 wherein the dividing-dispersing device is a jet mill.
10. A method as defined in claim 1, 2 or 3 wherein the dividing-dispersing device is positioned in a channel for the exhaust gas and has an outlet oriented in the direction of flow of the exhaust gas.
11. A method as defined in claim 1, 2 or 3 wherein the outlet of the dividing-dispersing device is positioned in a bent portion of the exhaust gas channel.
12. A method as defined in claim 1, 2 or 3 wherein the exhaust gas channel is provided downstream from the bent portion with means for promoting the mixing of the aerosol of high concentration with the exhaust gas.
13. A method as defined in claim 1, 2 or 3 wherein the mixing promoting means is a diffuser formed in the exhaust gas channel.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59-72246 | 1984-04-10 | ||
| JP59072246A JPS60216832A (en) | 1984-04-10 | 1984-04-10 | Purification of waste gas by dry lime process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1290922C true CA1290922C (en) | 1991-10-22 |
Family
ID=13483739
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000477363A Expired - Fee Related CA1290922C (en) | 1984-04-10 | 1985-03-25 | Method of purifying exhaust gas |
Country Status (7)
| Country | Link |
|---|---|
| JP (1) | JPS60216832A (en) |
| BE (1) | BE902140A (en) |
| CA (1) | CA1290922C (en) |
| DE (1) | DE3511759A1 (en) |
| FR (1) | FR2562442B1 (en) |
| GB (1) | GB2157192B (en) |
| IT (1) | IT1180740B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114262635A (en) * | 2021-12-09 | 2022-04-01 | 中国石油大学(北京) | Natural gas reinforced desulfurization and decarburization system and method |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62210035A (en) * | 1986-03-07 | 1987-09-16 | Hitachi Zosen Corp | Method for desalting combustion exhaust gas |
| CA1309571C (en) * | 1986-07-14 | 1992-11-03 | Ronald R. Landreth | Method and apparatus for reducing sulfur dioxide content in flue gases |
| DE3624300A1 (en) * | 1986-07-18 | 1988-01-28 | Metallgesellschaft Ag | Process for the preparation of calcium-hydrate-containing sorbents for SO2 absorption from exhaust gases |
| JPH0721273U (en) * | 1992-07-15 | 1995-04-18 | 新日本製鐵株式会社 | Power supply tip for high frequency resistance welding |
| JP5170040B2 (en) * | 2009-09-01 | 2013-03-27 | 株式会社日立製作所 | HF-containing gas dry processing apparatus and processing method |
| JP7193807B2 (en) * | 2020-08-19 | 2022-12-21 | 株式会社ニッセー | Foodstuff derived from orthopteran insects processed to be suitable for eating and method for producing the same |
Family Cites Families (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3721066A (en) * | 1970-12-29 | 1973-03-20 | Teller Environmental Systems | Process for recovery of acid gases |
| DE2437750C3 (en) * | 1974-08-06 | 1983-12-01 | Hünlich, Hans-Werner, Dipl.-Ing., 5600 Wuppertal | Single and multi-stage process for dry absorption and separation of gaseous pollutants from exhaust gases as dry residues |
| FR2285169A1 (en) * | 1974-09-19 | 1976-04-16 | Mitsubishi Heavy Ind Ltd | Preventing corrosion and dust deposition by gas effluents - in glass-melting installation by injecting alkaline powders into gas ducts |
| DE2520045A1 (en) * | 1975-05-06 | 1976-11-25 | Heinz Hoelter | Gas purificn. by addn. of absorbent - in series of stages with sepn. and recycling of absorbent after each stage |
| DE2615828A1 (en) * | 1976-04-10 | 1977-10-13 | Heinz Hoelter | Gas purificn. by addn. of absorbent - in series of stages with sepn. and recycling of absorbent after each stage |
| FR2387073A1 (en) * | 1977-04-12 | 1978-11-10 | Air Ind | PROCESS FOR DEPURING A HOT GAS CURRENT THAT MAY CAUSE CONDENSABLE PARTICLES AND / OR GASEOUS PRODUCTS |
| US4197278B1 (en) * | 1978-02-24 | 1996-04-02 | Abb Flakt Inc | Sequential removal of sulfur oxides from hot gases |
| DE2820357A1 (en) * | 1978-05-10 | 1979-11-15 | Metallgesellschaft Ag | METHOD FOR REMOVING SULFUR OXIDS FROM COMBUSTION EXHAUST GASES |
| DE2910537C2 (en) * | 1979-03-17 | 1982-10-21 | L. & C. Steinmüller GmbH, 5270 Gummersbach | Process for regenerating the dry and fine-grain additives from an exhaust gas purification device |
| AT380645B (en) * | 1983-11-25 | 1986-06-25 | Waagner Biro Ag | METHOD FOR SEPARATING ACID POLLUTANT GASES AND COMBUSTION PLANT FOR CARRYING OUT THE METHOD |
-
1984
- 1984-04-10 JP JP59072246A patent/JPS60216832A/en active Granted
-
1985
- 1985-03-18 GB GB08506958A patent/GB2157192B/en not_active Expired
- 1985-03-25 CA CA000477363A patent/CA1290922C/en not_active Expired - Fee Related
- 1985-03-30 DE DE19853511759 patent/DE3511759A1/en not_active Ceased
- 1985-04-03 IT IT47914/85A patent/IT1180740B/en active
- 1985-04-04 FR FR858505119A patent/FR2562442B1/en not_active Expired - Fee Related
- 1985-04-09 BE BE2/60660A patent/BE902140A/en unknown
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114262635A (en) * | 2021-12-09 | 2022-04-01 | 中国石油大学(北京) | Natural gas reinforced desulfurization and decarburization system and method |
Also Published As
| Publication number | Publication date |
|---|---|
| DE3511759A1 (en) | 1985-10-17 |
| JPH0248289B2 (en) | 1990-10-24 |
| IT8547914A1 (en) | 1986-10-03 |
| IT8547914A0 (en) | 1985-04-03 |
| BE902140A (en) | 1985-07-31 |
| JPS60216832A (en) | 1985-10-30 |
| FR2562442A1 (en) | 1985-10-11 |
| IT1180740B (en) | 1987-09-23 |
| GB2157192A (en) | 1985-10-23 |
| GB8506958D0 (en) | 1985-04-24 |
| FR2562442B1 (en) | 1990-03-23 |
| GB2157192B (en) | 1988-04-13 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKLA | Lapsed |