CA1079495A - Apparatus and method for cleansing noxious constituents from gas streams - Google Patents
Apparatus and method for cleansing noxious constituents from gas streamsInfo
- Publication number
- CA1079495A CA1079495A CA264,092A CA264092A CA1079495A CA 1079495 A CA1079495 A CA 1079495A CA 264092 A CA264092 A CA 264092A CA 1079495 A CA1079495 A CA 1079495A
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- Canada
- Prior art keywords
- container
- gas
- liquid
- drive pipe
- gases
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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
- B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
-
- 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
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
- Separation Of Particles Using Liquids (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
An apparatus and method for chemically altering and scrubbing the noxious constituents from foundry core manufacturing and arc welding operations is disclosed.
An upstanding closed container is provided and a gas washing liquid is disposed within the container to a predetermined level. A horizontal baffle is mounted stationarily within the container at an elevation spaced slightly above the level of the gas washing liquid therein and spaced peripheral portions of the baffle are spaced inwardly of the opposing inner surface of the container. A gas drive pipe extends into the container, downwardly past the baffle, and opens downwardly in a central lower portion of the container, below the baffle and near the bottom of the liquid. The container includes a top cover and an outlet duct is provided which opens outwardly of the container through a central portion of the cover. The gases are pumped into the drive pipe to achieve a critical velocity at the exit of the drive pipe of about 900-6000 linear feet per minute.
Entering the liquid in a substantially vertical downward direction within the critical velocity range, small gas-containing bubbles, on the order of 1/8-3/8 inches is diameter, are formed as the gas stream rises, which bubbles impact against the horizontal baffle. The high velocity gases impart sufficient kinetic energy to the system to enable the necessary chemical reactions and scrubbing to proceed.
An apparatus and method for chemically altering and scrubbing the noxious constituents from foundry core manufacturing and arc welding operations is disclosed.
An upstanding closed container is provided and a gas washing liquid is disposed within the container to a predetermined level. A horizontal baffle is mounted stationarily within the container at an elevation spaced slightly above the level of the gas washing liquid therein and spaced peripheral portions of the baffle are spaced inwardly of the opposing inner surface of the container. A gas drive pipe extends into the container, downwardly past the baffle, and opens downwardly in a central lower portion of the container, below the baffle and near the bottom of the liquid. The container includes a top cover and an outlet duct is provided which opens outwardly of the container through a central portion of the cover. The gases are pumped into the drive pipe to achieve a critical velocity at the exit of the drive pipe of about 900-6000 linear feet per minute.
Entering the liquid in a substantially vertical downward direction within the critical velocity range, small gas-containing bubbles, on the order of 1/8-3/8 inches is diameter, are formed as the gas stream rises, which bubbles impact against the horizontal baffle. The high velocity gases impart sufficient kinetic energy to the system to enable the necessary chemical reactions and scrubbing to proceed.
Description
107~49S
This invention relates to an. apparatus and method for cleaning, scrubbing and deodorizing industrial stack ~ases, especially where a chemical reaction is desired to remove the toY.ic and noxious constituent(s), .such as the stack gases generated in the making of foundry cores and in arc welding operations. ::
Various industrial manufacturing processes often result in unwanted gaseous by-products that must be disposed of prior to releasing the gases to the environment. For example, :~
foundry cores and molds are cured in the chemical core making or cold box process through the utilization of dimethyl-ethylamine -gas (hereafter DMEA) and the gas, after being utilized in the .process of curing the foundry core, has previously been exhausted to the atmosphere. Similarly, in the "exothermic" or "hot process"
for making conventional foundry cores, exhaust gases having high ~uantities of noxious gases, such as formaldehyde and phenols, have previously been passed directly into the atmosphere. However, these gases have objectionable odors and contain constituents -which have serious detrimental effects on the environment. To the same detrimental effect are the exhaust gases from processes ` for forming shell sand cores, arc welding operations as well as .~any other industrial facilities.
Various forms of gas deodorizers and gas washing ~apparatuses have heretofore been designed, some of which are sclosed in U.S. Patents Nos. 242,368, 411,014, 1,182,543, ~ 3.,183,645, 3,811,249 and 3,895,926. Reference should also be : ~made to U.S. Patents Nos. 1,750,800, 2,250,226, 3,216,181, French ~atent No. 543,412, and Italian Patent No. 566,593. Moreover, ~most gas washing and deodorizing apparatus have been designed to 30 ~erform specific functions in `B
..... . . . . . .
107~95 specific operating environments, and are not well suited to perform different functions in other environments, particularly the removal of noxious gases from the exhaust streams from foundry core and shell sand core manufacturing processes, arc welding operations and many other industrial plants.
This invention broadly relates to a gas cleaning and scrubbing apparatus and method, especially suited for chemically altering and scrubbing the noxious components of stack gases generated in the manufacture of foundry cores and molds, arc welding operations and the like.
More specifically, the gas washing apparatus of the present invention includes an upright container or tank which is partially filled with a gas washing liquid. Spaced above the top of the liquid when at rest is a horizontal baffle plate secured within the tank with its peripheral edges spaced slightly inwardly from the opposing inner wall surfaces of the container. The baffle serves to retain the liquid in the lower portion of the container as the gas to be cleaned is bubbling therethrough and to serve as an impact wall against which the rapidly rising bubbles impinge.
The top of the container is covered with a cover plate, upon which is mounted a compressor or turbine blower.
; The inlet of the compressor receives the gas to be washed, which is then pumped at a very high velocity into the gas washing liquid through a drive pipe. The gas enters the liquid from the drive pipe near the bottom of the container, at substantially the horizontal center of the container. The gas then bubbles up through the gas washing liquid within the container. The dimensions of the container, the baffle plate, the high inlet gas velocity, as well as other factors to be 1C~794~S
discussed, are de~igned so as to circulate the gas through the liquid in a particular flow pattern such that the scrubbing action, including any chemical reactions necessary to convert the noxious gases to dissolvable constituents in the gas washing liquid, can be carried to completion with essentially total removal of the noxious components from the exiting gas stream. The cleansed gas escapes outwardly and upwardly around the marginal edges of the baffle into the upper portion of the container for subsequent discharge by means of an outlet stack mounted on the container cover.
The method of washing or deodorizing gases in accordance with the present invention includes providing a gas washing liquid in the bottom portion of a container, subjecting the gas to be washed to a sufficiently high velocity at the point of entry into the gas washing liquid to impart substantial kinetic energy to the gas-liquid system and form a mass of small gas-containing bubbles in the liquid, allowing the mass of small gas-containing bubbles to rise rapidly upwardly through the liquid into an impact plate which restrains the upper level of the gas-containing bubbles below the height the bubbles would assume if not restrained in order to establish a turbulent flow path for the gas bubbles through the liquid, and thereafter allowing the cleansed gas to escape from the liquid.
It is the principal object of this invention to provide a simple and inexpensive gas washing and purifying apparatus and method for cleansing objectionable and noxious gases from industrial waste gases, particularly gases which must undergo a chemical reaction before they can be readily scrubbed from an exhaust gas stream, such as DMEA, formaldehyde, phenols, and the like that are produced in the manufacture of ~079495 foundry cores, arc welding operations, etc.
It is a further object of this invention to provide an apparatus for gas cleaning which may be readily constructed on a large scale and utilized to remove pollutants, or other undesirable products, from noxious gas streams prior to discharge of the gas stream into the atmosphere.
Another object of this invention is to provide a gas washing apparatus through which the gas to be cleansed may be pumped by a suitable gas pumping structure associated with the inlet of the drive pipe of the gas washing apparatus.
A further object of the present invention is to provide a method and apparatus whereby a gas stream is scrubbed of its noxious constituents in a washing liquid by driving the %as stream into the liquid at a very high velocity above a critical minimum velocity and below a critical maximum velocity.
Still another important object of this invention is to provide a gas washing apparatus and method having low power requirements.
A further object of this invention is to provide a gas washing apparatus in accordance with the preceding objects which will conform to conventional forms of manufacture, be of simple construction and easy to use so as to provide a device that will be economically feasible, long lasting and relatively ~ trouble free in operation.
`~ It is still further an object of this invention to provide a simple, reliable, and inexpensive apparatus and method fos chemically reacting the noxious constituents of a gas stream by providing the energy needed to induce and carry out the chemical reaction from the kinetic energy of the gas caused by flowing the gas stream into a gas washing liquid at a :; -4-very high velocity.
Figure 1 is a perspective view of the gas washing apparatus of the present invention with a portion of the wall of the container component thereof being broken away and illustrated in vertical section.
Figure 2 is an enlarged vertical, sectional view taken substantially upon the plane indicated by the section line
This invention relates to an. apparatus and method for cleaning, scrubbing and deodorizing industrial stack ~ases, especially where a chemical reaction is desired to remove the toY.ic and noxious constituent(s), .such as the stack gases generated in the making of foundry cores and in arc welding operations. ::
Various industrial manufacturing processes often result in unwanted gaseous by-products that must be disposed of prior to releasing the gases to the environment. For example, :~
foundry cores and molds are cured in the chemical core making or cold box process through the utilization of dimethyl-ethylamine -gas (hereafter DMEA) and the gas, after being utilized in the .process of curing the foundry core, has previously been exhausted to the atmosphere. Similarly, in the "exothermic" or "hot process"
for making conventional foundry cores, exhaust gases having high ~uantities of noxious gases, such as formaldehyde and phenols, have previously been passed directly into the atmosphere. However, these gases have objectionable odors and contain constituents -which have serious detrimental effects on the environment. To the same detrimental effect are the exhaust gases from processes ` for forming shell sand cores, arc welding operations as well as .~any other industrial facilities.
Various forms of gas deodorizers and gas washing ~apparatuses have heretofore been designed, some of which are sclosed in U.S. Patents Nos. 242,368, 411,014, 1,182,543, ~ 3.,183,645, 3,811,249 and 3,895,926. Reference should also be : ~made to U.S. Patents Nos. 1,750,800, 2,250,226, 3,216,181, French ~atent No. 543,412, and Italian Patent No. 566,593. Moreover, ~most gas washing and deodorizing apparatus have been designed to 30 ~erform specific functions in `B
..... . . . . . .
107~95 specific operating environments, and are not well suited to perform different functions in other environments, particularly the removal of noxious gases from the exhaust streams from foundry core and shell sand core manufacturing processes, arc welding operations and many other industrial plants.
This invention broadly relates to a gas cleaning and scrubbing apparatus and method, especially suited for chemically altering and scrubbing the noxious components of stack gases generated in the manufacture of foundry cores and molds, arc welding operations and the like.
More specifically, the gas washing apparatus of the present invention includes an upright container or tank which is partially filled with a gas washing liquid. Spaced above the top of the liquid when at rest is a horizontal baffle plate secured within the tank with its peripheral edges spaced slightly inwardly from the opposing inner wall surfaces of the container. The baffle serves to retain the liquid in the lower portion of the container as the gas to be cleaned is bubbling therethrough and to serve as an impact wall against which the rapidly rising bubbles impinge.
The top of the container is covered with a cover plate, upon which is mounted a compressor or turbine blower.
; The inlet of the compressor receives the gas to be washed, which is then pumped at a very high velocity into the gas washing liquid through a drive pipe. The gas enters the liquid from the drive pipe near the bottom of the container, at substantially the horizontal center of the container. The gas then bubbles up through the gas washing liquid within the container. The dimensions of the container, the baffle plate, the high inlet gas velocity, as well as other factors to be 1C~794~S
discussed, are de~igned so as to circulate the gas through the liquid in a particular flow pattern such that the scrubbing action, including any chemical reactions necessary to convert the noxious gases to dissolvable constituents in the gas washing liquid, can be carried to completion with essentially total removal of the noxious components from the exiting gas stream. The cleansed gas escapes outwardly and upwardly around the marginal edges of the baffle into the upper portion of the container for subsequent discharge by means of an outlet stack mounted on the container cover.
The method of washing or deodorizing gases in accordance with the present invention includes providing a gas washing liquid in the bottom portion of a container, subjecting the gas to be washed to a sufficiently high velocity at the point of entry into the gas washing liquid to impart substantial kinetic energy to the gas-liquid system and form a mass of small gas-containing bubbles in the liquid, allowing the mass of small gas-containing bubbles to rise rapidly upwardly through the liquid into an impact plate which restrains the upper level of the gas-containing bubbles below the height the bubbles would assume if not restrained in order to establish a turbulent flow path for the gas bubbles through the liquid, and thereafter allowing the cleansed gas to escape from the liquid.
It is the principal object of this invention to provide a simple and inexpensive gas washing and purifying apparatus and method for cleansing objectionable and noxious gases from industrial waste gases, particularly gases which must undergo a chemical reaction before they can be readily scrubbed from an exhaust gas stream, such as DMEA, formaldehyde, phenols, and the like that are produced in the manufacture of ~079495 foundry cores, arc welding operations, etc.
It is a further object of this invention to provide an apparatus for gas cleaning which may be readily constructed on a large scale and utilized to remove pollutants, or other undesirable products, from noxious gas streams prior to discharge of the gas stream into the atmosphere.
Another object of this invention is to provide a gas washing apparatus through which the gas to be cleansed may be pumped by a suitable gas pumping structure associated with the inlet of the drive pipe of the gas washing apparatus.
A further object of the present invention is to provide a method and apparatus whereby a gas stream is scrubbed of its noxious constituents in a washing liquid by driving the %as stream into the liquid at a very high velocity above a critical minimum velocity and below a critical maximum velocity.
Still another important object of this invention is to provide a gas washing apparatus and method having low power requirements.
A further object of this invention is to provide a gas washing apparatus in accordance with the preceding objects which will conform to conventional forms of manufacture, be of simple construction and easy to use so as to provide a device that will be economically feasible, long lasting and relatively ~ trouble free in operation.
`~ It is still further an object of this invention to provide a simple, reliable, and inexpensive apparatus and method fos chemically reacting the noxious constituents of a gas stream by providing the energy needed to induce and carry out the chemical reaction from the kinetic energy of the gas caused by flowing the gas stream into a gas washing liquid at a :; -4-very high velocity.
Figure 1 is a perspective view of the gas washing apparatus of the present invention with a portion of the wall of the container component thereof being broken away and illustrated in vertical section.
Figure 2 is an enlarged vertical, sectional view taken substantially upon the plane indicated by the section line
2-2 of Figure 1.
Figure 3 is an enlarged vertical, sectional view taken substantially upon the plane indicated by the section line 2-2 of Figure 1, and showing the bubbling and circulation pattern of the gas in the gas washing liquid in conformance with the method and apparatus of the present inventionO
Figure 4 is a schematic rendering of the apparatus, used for calculating velocity at the outlet of the drive pipe, and is located with Figure 1 on the first page of drawings.
Figure 5 is a graph illustrating the relationship in accordance with the present invention of the gas inlet velocity and height of gas-carrying bubbles in the washing liquid; Figure 5 is located with Figure 1 on the first page of drawings.
Referring now more specifically to the drawings, wherein like numerals refer to like parts throughout, the numeral 10 generally designates the gas washing apparatus of the instant invention. The apparatus 10 includes an upstanding container or tank 12 preferably having a cyIindrical side wall 14. A bottom wall 16 closes the lower end of the container 12 and a top cover wall or cover plate 18 closes the upper end of the container.
Rubber gaskets (not shown) can be inserted between the top cover plate 18 and the container 12. The bottom wall 16 is supported 30 by short legs 13 welded to the bottom of the container for easy movement and placement of the , B - 5 _ ~ cm/~ h .
.
container.
The interior of the container 12 includes three circumferentially spaced mounting U-brackets 20 (only one shown in the drawings) supported from and projecting downwardly of top cover wall 18, and a horizontal baffle plate 22 supported from the brackets 20 by means of suitable fasteners, not shown.
The baffle plate 22 in plan shape contours substantially to the shape of the horizontal cross-section of the container generally at the height where the baffle plate is positioned. However, the size of the baffle plate is slightly less than the horizontal cross-section so that the edge of the baffle plate is ~lightly spaced around its entire periphery from the adjacent portion of the side wall to allow for escape of the cleansed gas. In the preferred form as shown in the drawings, the container or tank 12 i8 cylindrical and the horizontal baffle plate 22 is circular with a diameter slightly less than the inside diameter of the container 12 whereby an annular gas flow space or opening 28 is provided between the baffle plate 22 and the opposing inner wall surface of the side wall 14. While the width of the annular opening 28 may vary, it has been found that a width of about 1/2-2 inches is preferrable. The baffle plate 22 has an opening 23 at its marginal portion through which a drive pipe 30 is fitted. The baffle plate 22, container 12, and top cover wall 18 are constructed of suitable corrosion-resistant and durable material, such as stainless steel or the like.
The central portion of the top cover wall 18 has a large diameter opening 48 formed therethrough and the inlet end of an outlet duct or stack 50 is secured by bolts (not . .
` shown) through the opening 48. Rubber gaskets (not shown) ; 30 can be inserted between the cover plate 18 and the stack 50.
' 1~)79495 The outlet stack 50 is preferably formed from a polyvinyl chloride (PVC) plastic tube. The stack diameter i8 sufficiently wide to reduce the gas exit flow velocity and to eliminate any pressure buildup that may occur. The stack is of a sufficient height so as to promote condensation and to eliminate any safety problems relating to splashing of the liquid in the container. The top wall 18 further has an inlet filler pipe 51 for communcation with the interior of the container. A removable filler ~ap 53 is provided to seal the interior during operation.
Chemicals can be added to the container through the filler pipe 51 as needed during operation of the unit.
On the top cover wall 18 of the container 12 is a vortex turbine blower 61 mounted on a mounting plate 63. The capacity of the blower 61 will depend upon the design requirements for a particular operation. A Type VB-022C vortex blower manufactured by The Spencer Turbine Company of Windsor, Connecticut, has been found to be a suitably designed blower for the instant invention. The blower 61 has a turbine inlet port 65 and a turbine outlet port 67. The inlet port is connected to a hose or pipe 46 which receives the gas to be washed. The outlet port 67 is connected to drive pipe 30 by means of an elbow shaped section 69.
The drive pipe 30 extends through a hole in the top cover wall 18, through the opening 23 in the baffle plate 22, and into the lower portion of the container. The drive pipe 30 is depicted in Figures 2 and 3 as a pipe having a downward portion 31 parallel to the major axis of the container, a portion 33 approximately at a 45 angle from the vertical, and a further downward portion 35 substantially coaxial with the major axis of the container. The exact shape of the pipe .
~o79495 therefore preferrcd, so long as the bends in the pipe are such that the high-velocity flow of gas through the pipe i9 not unduly impaired or constricted and the outlet portion 37 is located substantially along the major axis of the container (where only one drive pipe is utilized) and spaced slightly above the bottom wall 16. The outlet portion 37 projects downwardly with its outlet opening 38 facing the bottom wall 16 of the container, to produce the desired circulation of the gas in the gas washing liquid. For large capacity units, having large diameters, a plurality of drive pipes may be used as needed.
The gas washing liquid 58 is comprised of a solution, normally water and including any necessary chemicals, adapted to wash and cleanse the particular gas being treated . The solution can encompass a wide range of chemicals, depending on the gases or particulate to be scrubbed. However, the present invention has been found particularly applicable to the scrubbing of gas streams containing amine pollutants, especially DMEA
gas exiting from foundry core and mold manufacturing operations ~B 20 using the chemical or cold box process, such as the ISOCURE 0 process of Ashland Chemical Company of Dublin, Oklahoma. In addition, the apparatus and method of the present invention has been found particularly successful in washing and scrubbing heretofore untreated exhaust gas streams generated in the "exothermic" or "hot" process for making conventional foundry cores and shell sand cores, where the principal pollutants are formaldehyde and phenol and in arc welding operations, where the principal pollutants of the waste gases are nitrogen oxides and carbon monoxide. In the removal of these pollutants from the foregoing gas streams, a 10% by volume blended acidic .
.
':
, ~, ~ - ' .. . .
.
~0794~5 solution (acid in water), having a pH below 7 and preferably below 5, made by combining and diluting 85~ phosphoric acid and 96% sulfuric acid (66 Baume), has been found most satisfactory.
Acid can be periodically added through the filler pipe 51 to maintain the desired pH level. One particular acid combination solution found useful in the present invention is 70 parts H3P04 and 30 parts H2S04 by volume diluted with water to 10% acid by volume. Solutions found useful for treating DMEA gases, are a 10% phosphoric acid solution as well as "K-C
Phosphoric Acid 85% Blend" sold by K.C. Cores, Inc. of Joliet, Illinois. However, it will be understood and appreciated by those skilled in the art that the precise chemical make-up and concentration of the gas washing liquid is not critical since various known chemicals in varying concentrations can be employed in treating a particular gas stream to convert the noxious constituent(s), as needed, to a soluble form for ready scrubbing by the aqueous liquid. It is only necessary that a sufficient quantity of the necessary chemical(s) be present in the liquid to achieve the desired reaction(s).
The bottom of baffle plate 22 and the top or liquid level of liquid 58 when in an at rest or non-operating condition are spaced apart a distance L, as shown in Figure 2. The distance L will vary depending on the gas being treated in any particular unit, but is preferrably 4 inches and normally should be anywhere from 5Z to 20% of the total height of the at rest liquid in the container.
In operation, the gas to be treated is supplied by means of a pipe or hose 46 and is compressed and blown at a high velocity by the vortex blower 61 through the drive pipe 30. In almost all operations, the gas stream to be _g_ "~ , ". ~' ' .-~ .
cleansed does not have sufficient volume to permit acceleration of the gases above the critical minimum velocity at the exit of the drive pipe required for the present invention. Also, where oxygen is needed to carry out the desired chemical reaction(s), it i8 necessary to dilute the exhaust gas stream with a major quantity of air. Therefore, in practically all operations, it is desired to introduce air into the gas stream in sufficient quantities to assure the necessary gas volume for attaining the required gas exit velocity at the 10 drive pipe outlet and sufficient oxygen to allow for any oxidation reactions to proceed without interruption. Air can be introduced into the gas stream by any convenient means, such as a conventional check valve in the inlet hose 46. Another technique is to mount a separate blower on cover 18 whose inlet is open to the atmosphere. The outlet is connected to the drive pipe 30 in parallel with the first blower. By continuously operating the second blower at a speed above that necessary to assure an exit gas velocity above the critical minimum, an exit , gas velocity above the minimum is always assured at the drive ; 20 pipe outlet regardless of a temporary change in the exhaust gas supply through the first blower. Preferably, the second blower is connected to the drive pipe 30 by suitable piping outside the container to connect with elbow section 69.
If additional oxygen is required for the desired chemical reaction(s), an auxiliary hose line (not shown) can also be provided to an oxygen source such as a compressed oxygen container.
The ga~ ~tream entering the drive pipe is expelled ~ from the bottom of the pipe 38 at the center of the cylindrical d 30 housing 12 slightly above the bottom plate 16. The very high 1~79495 velocity and flow rate of the gas stream are such that very small homogeneous bubbles on the order of 1/8 - 3/8 inches in diameter will form in the gas washing liquid thus greatly increasing the reactive surface area of the gas in the liquid.
The gas then bubbles through the gas washing liquid in a particular flow pattern as shown in Figure 3.
The flow pattern of the gas through the liquid, as indicated generally in Figure 3, creates rather large bubbles 71 at the point where the gas is expelled from the pipe due to the high impact of the gas into the liquid. These large bubbles rapidly disperse to form the smaller discreet bubbles which move upward rapidly from the bottom portion of the container at a slight angle from the major axis of the container, a~ shown by arrows 73. The bubbles move in the direction of arrows 73 as they approach the baffle plate 22. There, the baffle plate 22 acts as a retaining wall and serves as an impact wall against which the rapidly rising gas-containing bubbles impinge for tubulent contact. Then, after initial impingement against the baffle plate, and in conjunction with the annular opening 28, the gas is directed toward the sides of the container 14. That iSs as the gas bubbles impact the -baffle plate 22, the gas tends to flow outwardly toward the annular openings 28. As the bubbles approach the sides of the container 14, near the annular opening 28, a small portion of :..
the gas i8 diverted outwardly on top of the plate 22, while other gas is circulated downwardly toward the bottom of the container and back upwardly again as shown by arrows 75. The dimensions of the container 12, the velocity of the gas flow at the outlet 37, and the contents of the washing liquid can be varied depending upon the characteristics of the gas to be ,:
10794~5 c leansed .
The exit velocity of the gas stream at the opening 38 of the drive pipe 30 must be such that the gas particles are subjected to a sufficiently high velocity to provide the necessary kinetic energy to create the needed turbulence for the scrubbing action to be effective and to cause the chemical reaction, if desired, between the gas and the liquid to occur.
It has been found that an exit gas velocity of at least 900 linear feet per minute at the drive pipe outlet is required in order for the gas to attain the necessary kinetic energy. On the other hand, the velocity should not be so great as to cause the washing liquid to "blow out" of the container portion below the baffle, or force the gas to flow through the solution 80 quickly that the chemical reaction cannot be completed. The maximum velocity is related to and should not exceed that velocity which completely fills the container with gas-filled bubbles. It is believed that exit velocities in excess of 6000 linear feet per minute for the gas stream would be unacceptable for the present invention. It has been found, however, that depending upon the size and capacity of the cleansing unit, a gas exit velocity between 1500 and 3000 linear feet per minute is preferred.
" When operating the method of this invention within the exit gas velocity parameters described in the preceding paragraph, it has been noted that the gas-containing bubbles move in the washing liquid of the preferred apparatus of this invention according to the flow path shown in Figure 3. Yet, when the gas exit velocity approaches and drops below the aforesaid 900 lin. ft/min critical minimum, the gas bubble flow pattern changes radically. Instead of forming small discreet 107~49S
gas-containing bubbles which move upwardly around the drive pipe to impact against the baffle 22, the gas exiting from the drive pipe forms into large bubbles which generally remain in tact all the way up through the washing liquid until contacting the baffle 22. Thu8, the believed beneficial results from having small, discreet gas-containing bubbles impact the baffle is lost as the gas exit velocity approaches and drops below 900 lin. ft/min. Therefore, without intending to be limited to this theory, it is presently believed that in order to achieve the beneficial results attendant the present invention, the gas exit velocity at the drive pipe outlet must be sufficiently high to achieve a gas-containing bubble flow pattern through the washing liquid as shown in Figure 3.
Turning to Figure 5, the linear velocity of the gas 8tream entering the blower (which is proportional to the linear velocity at the drive pipe outlet as discussed hereinafter) has been plotted against the height of the bubbles in the washing liquid. It will be noted that within the prescribed limits of the invention, the height of the bubbles in the washing liquid 20 i8 directly proportional to gas velocity. As you approach and surpass the critical maximum 6000 lin. ft/min, the curve then flattens out and is no longer proportional. Within the operative range for the exit gas velocity the height of the bubbles within the liqud is 30-75% of the height of the liquid in an at rest state.
As shown in Figure 3, even when operating within the preferred gas exit velocity range, some of the gas-containing bubbles do rise over the baffle plate, as shown at 77. The liqud component of these bubbles will roll back down into the container, while only a very small proportion of the liquid ?
-- .
~ , .
will be diverted out to the outlet stack 50 with the gas. The gas, escaping around baffle 22, which has now been cleansed, is directed from the container through the outlet stack 50. The outlet stack 50 is of a sufficient height 90 that condensation occurs in the outlet stack and the condensed liquid will fall back into the container. If desired, a fibrous filter, such as the typical home furnace filter, may be inserted at the top of the outlet stack to capture any residual particulate and moisture in the exiting gas stream.
As will be apparent to those of ordinary skill in this art, the interaction between the gas to be cleansed and the liquid in the container can vary, depending upon the results desired. For example, in some cases a chemical reaction will occur, while in other cases only a scrubbing occurs whereby undesirable gases and particulates are scrubbed from the gas stream without chemical conversion.
We shall now describe our invention as applied to the washing and scrubbing of particular exhaust gas streams utilizing specific embodiments of the invention. As stated previously, this invention is particularly suited to scrubbing the dimethylethylamine (DMEA) gases generated in what is known in the foundry industry as the "chemical" or "cold box" process for making foundry cores or molds. One such process is known as the ISOCURE process referred to previously. Briefly, the core ingredients of sand and a small quantity of a binder, ; approximately 1.5X by weight of the sand, such as about equal parts isocyanate and polyurethane, are mixed and placed into a form. A DMEA gas stream, normally containing 12% DMEA and the balance air or CO2 is then passed through the form for 5-10 seconds followed by a 10-20 second air purge to cure the core.
.:
.: - - . .. .
1C~79~95 Heretofore, this DMEA exit gas was passed directly to the atmosphere and efforts to scrub the DMEA gas at reasonable cost were characteristically unsuccessful.
One such chemical or cold foundry core making apparatus was equipped with the present invention as shown in the preferred embodiment. The foundry core making apparatus used about 2.25 pounds of DMEA gas (actual DMEA) per hour. Sufficient air was introduced into the gas stream to produce a gas stream of 55 parts oxygen to one part DMEA. The blower was a Spencer vortex side channel blower having a rated horsepower of 3.7 hp. The inlet port and outlet port diameters were 2 inches. The cylindrical container had a diameter of 30.5 inches and a height of 48 inches. One hundred ten gallons of a gas washing liquid were added to the container, resulting in a liquid height of approximately 36 inches from the bottom of the container. The liquid comprised a 5% phosphoric acid solution.
The drive pipe interconnecting the blower with the interior of the container had a two inch inner diameter and its outlet was positioned three inches from the bottom of the container. The drive pipe outlet was positioned so as to expel the gas to be processed downwardly toward the container bottom wall. The static pressure in the pipe had been calculated to be approximate- -ly 1 to 2 psi due to the head of the liquid solution in the container. The liquid level of the washing acid was such that the baffle plate was 4 inches above the top of the liquid when at rest, and the liquid height above the drive pipe outlet was approximately 33 inches. The outlet stack had a 14 inch diameter to reduce the exit flow velocity and any pressure build-up that may have occured in the system. The gas was rapidly drawn in and accelerated by the blower 61 through the `
10~9495 drive pipe 30. The velocity of the gas at the inlet to the blower was measured with an anomometer to be 2240 linear feet per minute (drive pipe exit velocity of approximately 2000 lin.
ft/min).
The accelerated gas entering the acidic liquid solution had a high enough velocity to ensure that its kinetic energy was greater than the threshold energy needed for the reaction to occur. It was noted that the bubbles resulting from this impact velocity had an average diameter of approximately 1/4 inch and each bubble has been calculated to have remained in the solution for an average of approximately 4.9 seconds.
The reaction occurring in the container was as follows:
CH2 CH3 CH2 ~ CH3 C H2 CH 3 H + N . H + :~ N = O - H ~ -/\ /\ /\
: (insoluble in water) (soluble in water) ;~
';
~079495 Some of the product will stay as amino oxides, and some will go to phosphate salts and carbon dioxide. The gas stream exiting from the foregoing described apparatus showed the following analysis:
pH of vapors 6.9 NH3 0.001 ppm formaldehyde none phenol none C0 none CN none C2 traces-but not a pollutant P (phosphorus in any form) 1.75 ppm amine derivatives only traces, but no odor dimethylethylamine less than .lppm (below odor threshold) balance water vapor During the operation of the foregoing system, if the velocity of the gas stream is too slow or the oxygen intake is too low, then the reaction of the gas washing acid and oxygen with the noxious components of the gas does not go to completion and a syrupy chemical is produced which thickens the washing acid into a gelatinous constituency. In contrast, if too great a volume of gas is fed through the system or the acid concentration drops too low the gas will produce a gray precipitate of aminophosphate. Thus, it is necessary to recharge the washing acid periodically, say, one quart of undiluted acid each eight hours of operation. A drive pipe exit gas velocity of about 1800-2800 linear feet per minute is preferred for normal operation of a system of this size.
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la7s4ss We have found that it is not necessary to completely replace the washing acid in this sy~tem except once every three months and in come cases possibly not until after one year of operation. In view of the importance of the oxygen component in the gas stream for scrubbing the DMEA, the volume of oxygen present must be at least twice the volume of DMEA to be scrubbed.
Further, as an alternate to periodic addition of chemicals to the washing liwuid, the apparatus can be equipped with a feeding mechanism to slowly add chemicals to the system on a continuous basis.
As an alternative to the 5% phosphoric acid solution for the gas washing liquid, equally satisfactory acid solution~ could be any dilute phosphoric acids up to 10% as well as dilute acid blends of phosphoric acid and sulphuric acid.
Other acid formulations could also be equally satisfactory.
In the design of our invented apparatus, we prefer a 2 inch i.d. drive pipe, but of course different sizes can be readily adapted depending upon the overall size of the equipment to be employed. With a 2 inch i.d. drive pipe, we have found that the diameter of the container must be at least 2 feet +10% to ensure at least 1 foot +10% unobstructed washing liquid around the drive pipe outlet. Therefore, in larger units using multiple 2 inch i.d. drive pipes, adjacent drive pipes should be at least 2 feet +10% apart, center to center, and each drive pipe should be at least one foot away ; from the closet portion of the container wall. In addition, with the preferred 2 inch i.d. drive pipe, there must be at least one foot of liquid head in the container above the drive pipe opening and preferrably 2-4 feet, and more if multiple drive pipes are employed. In other words, using a 2 inch i.d.
;, . .
~079495 drive pipe, the at rest liquid level of the washing liquid in the container must be at least one foot, and preferably two to four feet above the drive pipe opening using a single drive p~pe.
Based upon the observations and analyses of the DMEA
gas processing operation as above described the following design parameters would prevail in designing other units of different sizes:
CFM (cubic feet per minute) of gas flow to be treated:
cubic ft. of gas washing liquid = .3 x CFM:
gallons of gas washing liquid = .3 x CFM x 7.48:
Figure 3 is an enlarged vertical, sectional view taken substantially upon the plane indicated by the section line 2-2 of Figure 1, and showing the bubbling and circulation pattern of the gas in the gas washing liquid in conformance with the method and apparatus of the present inventionO
Figure 4 is a schematic rendering of the apparatus, used for calculating velocity at the outlet of the drive pipe, and is located with Figure 1 on the first page of drawings.
Figure 5 is a graph illustrating the relationship in accordance with the present invention of the gas inlet velocity and height of gas-carrying bubbles in the washing liquid; Figure 5 is located with Figure 1 on the first page of drawings.
Referring now more specifically to the drawings, wherein like numerals refer to like parts throughout, the numeral 10 generally designates the gas washing apparatus of the instant invention. The apparatus 10 includes an upstanding container or tank 12 preferably having a cyIindrical side wall 14. A bottom wall 16 closes the lower end of the container 12 and a top cover wall or cover plate 18 closes the upper end of the container.
Rubber gaskets (not shown) can be inserted between the top cover plate 18 and the container 12. The bottom wall 16 is supported 30 by short legs 13 welded to the bottom of the container for easy movement and placement of the , B - 5 _ ~ cm/~ h .
.
container.
The interior of the container 12 includes three circumferentially spaced mounting U-brackets 20 (only one shown in the drawings) supported from and projecting downwardly of top cover wall 18, and a horizontal baffle plate 22 supported from the brackets 20 by means of suitable fasteners, not shown.
The baffle plate 22 in plan shape contours substantially to the shape of the horizontal cross-section of the container generally at the height where the baffle plate is positioned. However, the size of the baffle plate is slightly less than the horizontal cross-section so that the edge of the baffle plate is ~lightly spaced around its entire periphery from the adjacent portion of the side wall to allow for escape of the cleansed gas. In the preferred form as shown in the drawings, the container or tank 12 i8 cylindrical and the horizontal baffle plate 22 is circular with a diameter slightly less than the inside diameter of the container 12 whereby an annular gas flow space or opening 28 is provided between the baffle plate 22 and the opposing inner wall surface of the side wall 14. While the width of the annular opening 28 may vary, it has been found that a width of about 1/2-2 inches is preferrable. The baffle plate 22 has an opening 23 at its marginal portion through which a drive pipe 30 is fitted. The baffle plate 22, container 12, and top cover wall 18 are constructed of suitable corrosion-resistant and durable material, such as stainless steel or the like.
The central portion of the top cover wall 18 has a large diameter opening 48 formed therethrough and the inlet end of an outlet duct or stack 50 is secured by bolts (not . .
` shown) through the opening 48. Rubber gaskets (not shown) ; 30 can be inserted between the cover plate 18 and the stack 50.
' 1~)79495 The outlet stack 50 is preferably formed from a polyvinyl chloride (PVC) plastic tube. The stack diameter i8 sufficiently wide to reduce the gas exit flow velocity and to eliminate any pressure buildup that may occur. The stack is of a sufficient height so as to promote condensation and to eliminate any safety problems relating to splashing of the liquid in the container. The top wall 18 further has an inlet filler pipe 51 for communcation with the interior of the container. A removable filler ~ap 53 is provided to seal the interior during operation.
Chemicals can be added to the container through the filler pipe 51 as needed during operation of the unit.
On the top cover wall 18 of the container 12 is a vortex turbine blower 61 mounted on a mounting plate 63. The capacity of the blower 61 will depend upon the design requirements for a particular operation. A Type VB-022C vortex blower manufactured by The Spencer Turbine Company of Windsor, Connecticut, has been found to be a suitably designed blower for the instant invention. The blower 61 has a turbine inlet port 65 and a turbine outlet port 67. The inlet port is connected to a hose or pipe 46 which receives the gas to be washed. The outlet port 67 is connected to drive pipe 30 by means of an elbow shaped section 69.
The drive pipe 30 extends through a hole in the top cover wall 18, through the opening 23 in the baffle plate 22, and into the lower portion of the container. The drive pipe 30 is depicted in Figures 2 and 3 as a pipe having a downward portion 31 parallel to the major axis of the container, a portion 33 approximately at a 45 angle from the vertical, and a further downward portion 35 substantially coaxial with the major axis of the container. The exact shape of the pipe .
~o79495 therefore preferrcd, so long as the bends in the pipe are such that the high-velocity flow of gas through the pipe i9 not unduly impaired or constricted and the outlet portion 37 is located substantially along the major axis of the container (where only one drive pipe is utilized) and spaced slightly above the bottom wall 16. The outlet portion 37 projects downwardly with its outlet opening 38 facing the bottom wall 16 of the container, to produce the desired circulation of the gas in the gas washing liquid. For large capacity units, having large diameters, a plurality of drive pipes may be used as needed.
The gas washing liquid 58 is comprised of a solution, normally water and including any necessary chemicals, adapted to wash and cleanse the particular gas being treated . The solution can encompass a wide range of chemicals, depending on the gases or particulate to be scrubbed. However, the present invention has been found particularly applicable to the scrubbing of gas streams containing amine pollutants, especially DMEA
gas exiting from foundry core and mold manufacturing operations ~B 20 using the chemical or cold box process, such as the ISOCURE 0 process of Ashland Chemical Company of Dublin, Oklahoma. In addition, the apparatus and method of the present invention has been found particularly successful in washing and scrubbing heretofore untreated exhaust gas streams generated in the "exothermic" or "hot" process for making conventional foundry cores and shell sand cores, where the principal pollutants are formaldehyde and phenol and in arc welding operations, where the principal pollutants of the waste gases are nitrogen oxides and carbon monoxide. In the removal of these pollutants from the foregoing gas streams, a 10% by volume blended acidic .
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~0794~5 solution (acid in water), having a pH below 7 and preferably below 5, made by combining and diluting 85~ phosphoric acid and 96% sulfuric acid (66 Baume), has been found most satisfactory.
Acid can be periodically added through the filler pipe 51 to maintain the desired pH level. One particular acid combination solution found useful in the present invention is 70 parts H3P04 and 30 parts H2S04 by volume diluted with water to 10% acid by volume. Solutions found useful for treating DMEA gases, are a 10% phosphoric acid solution as well as "K-C
Phosphoric Acid 85% Blend" sold by K.C. Cores, Inc. of Joliet, Illinois. However, it will be understood and appreciated by those skilled in the art that the precise chemical make-up and concentration of the gas washing liquid is not critical since various known chemicals in varying concentrations can be employed in treating a particular gas stream to convert the noxious constituent(s), as needed, to a soluble form for ready scrubbing by the aqueous liquid. It is only necessary that a sufficient quantity of the necessary chemical(s) be present in the liquid to achieve the desired reaction(s).
The bottom of baffle plate 22 and the top or liquid level of liquid 58 when in an at rest or non-operating condition are spaced apart a distance L, as shown in Figure 2. The distance L will vary depending on the gas being treated in any particular unit, but is preferrably 4 inches and normally should be anywhere from 5Z to 20% of the total height of the at rest liquid in the container.
In operation, the gas to be treated is supplied by means of a pipe or hose 46 and is compressed and blown at a high velocity by the vortex blower 61 through the drive pipe 30. In almost all operations, the gas stream to be _g_ "~ , ". ~' ' .-~ .
cleansed does not have sufficient volume to permit acceleration of the gases above the critical minimum velocity at the exit of the drive pipe required for the present invention. Also, where oxygen is needed to carry out the desired chemical reaction(s), it i8 necessary to dilute the exhaust gas stream with a major quantity of air. Therefore, in practically all operations, it is desired to introduce air into the gas stream in sufficient quantities to assure the necessary gas volume for attaining the required gas exit velocity at the 10 drive pipe outlet and sufficient oxygen to allow for any oxidation reactions to proceed without interruption. Air can be introduced into the gas stream by any convenient means, such as a conventional check valve in the inlet hose 46. Another technique is to mount a separate blower on cover 18 whose inlet is open to the atmosphere. The outlet is connected to the drive pipe 30 in parallel with the first blower. By continuously operating the second blower at a speed above that necessary to assure an exit gas velocity above the critical minimum, an exit , gas velocity above the minimum is always assured at the drive ; 20 pipe outlet regardless of a temporary change in the exhaust gas supply through the first blower. Preferably, the second blower is connected to the drive pipe 30 by suitable piping outside the container to connect with elbow section 69.
If additional oxygen is required for the desired chemical reaction(s), an auxiliary hose line (not shown) can also be provided to an oxygen source such as a compressed oxygen container.
The ga~ ~tream entering the drive pipe is expelled ~ from the bottom of the pipe 38 at the center of the cylindrical d 30 housing 12 slightly above the bottom plate 16. The very high 1~79495 velocity and flow rate of the gas stream are such that very small homogeneous bubbles on the order of 1/8 - 3/8 inches in diameter will form in the gas washing liquid thus greatly increasing the reactive surface area of the gas in the liquid.
The gas then bubbles through the gas washing liquid in a particular flow pattern as shown in Figure 3.
The flow pattern of the gas through the liquid, as indicated generally in Figure 3, creates rather large bubbles 71 at the point where the gas is expelled from the pipe due to the high impact of the gas into the liquid. These large bubbles rapidly disperse to form the smaller discreet bubbles which move upward rapidly from the bottom portion of the container at a slight angle from the major axis of the container, a~ shown by arrows 73. The bubbles move in the direction of arrows 73 as they approach the baffle plate 22. There, the baffle plate 22 acts as a retaining wall and serves as an impact wall against which the rapidly rising gas-containing bubbles impinge for tubulent contact. Then, after initial impingement against the baffle plate, and in conjunction with the annular opening 28, the gas is directed toward the sides of the container 14. That iSs as the gas bubbles impact the -baffle plate 22, the gas tends to flow outwardly toward the annular openings 28. As the bubbles approach the sides of the container 14, near the annular opening 28, a small portion of :..
the gas i8 diverted outwardly on top of the plate 22, while other gas is circulated downwardly toward the bottom of the container and back upwardly again as shown by arrows 75. The dimensions of the container 12, the velocity of the gas flow at the outlet 37, and the contents of the washing liquid can be varied depending upon the characteristics of the gas to be ,:
10794~5 c leansed .
The exit velocity of the gas stream at the opening 38 of the drive pipe 30 must be such that the gas particles are subjected to a sufficiently high velocity to provide the necessary kinetic energy to create the needed turbulence for the scrubbing action to be effective and to cause the chemical reaction, if desired, between the gas and the liquid to occur.
It has been found that an exit gas velocity of at least 900 linear feet per minute at the drive pipe outlet is required in order for the gas to attain the necessary kinetic energy. On the other hand, the velocity should not be so great as to cause the washing liquid to "blow out" of the container portion below the baffle, or force the gas to flow through the solution 80 quickly that the chemical reaction cannot be completed. The maximum velocity is related to and should not exceed that velocity which completely fills the container with gas-filled bubbles. It is believed that exit velocities in excess of 6000 linear feet per minute for the gas stream would be unacceptable for the present invention. It has been found, however, that depending upon the size and capacity of the cleansing unit, a gas exit velocity between 1500 and 3000 linear feet per minute is preferred.
" When operating the method of this invention within the exit gas velocity parameters described in the preceding paragraph, it has been noted that the gas-containing bubbles move in the washing liquid of the preferred apparatus of this invention according to the flow path shown in Figure 3. Yet, when the gas exit velocity approaches and drops below the aforesaid 900 lin. ft/min critical minimum, the gas bubble flow pattern changes radically. Instead of forming small discreet 107~49S
gas-containing bubbles which move upwardly around the drive pipe to impact against the baffle 22, the gas exiting from the drive pipe forms into large bubbles which generally remain in tact all the way up through the washing liquid until contacting the baffle 22. Thu8, the believed beneficial results from having small, discreet gas-containing bubbles impact the baffle is lost as the gas exit velocity approaches and drops below 900 lin. ft/min. Therefore, without intending to be limited to this theory, it is presently believed that in order to achieve the beneficial results attendant the present invention, the gas exit velocity at the drive pipe outlet must be sufficiently high to achieve a gas-containing bubble flow pattern through the washing liquid as shown in Figure 3.
Turning to Figure 5, the linear velocity of the gas 8tream entering the blower (which is proportional to the linear velocity at the drive pipe outlet as discussed hereinafter) has been plotted against the height of the bubbles in the washing liquid. It will be noted that within the prescribed limits of the invention, the height of the bubbles in the washing liquid 20 i8 directly proportional to gas velocity. As you approach and surpass the critical maximum 6000 lin. ft/min, the curve then flattens out and is no longer proportional. Within the operative range for the exit gas velocity the height of the bubbles within the liqud is 30-75% of the height of the liquid in an at rest state.
As shown in Figure 3, even when operating within the preferred gas exit velocity range, some of the gas-containing bubbles do rise over the baffle plate, as shown at 77. The liqud component of these bubbles will roll back down into the container, while only a very small proportion of the liquid ?
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~ , .
will be diverted out to the outlet stack 50 with the gas. The gas, escaping around baffle 22, which has now been cleansed, is directed from the container through the outlet stack 50. The outlet stack 50 is of a sufficient height 90 that condensation occurs in the outlet stack and the condensed liquid will fall back into the container. If desired, a fibrous filter, such as the typical home furnace filter, may be inserted at the top of the outlet stack to capture any residual particulate and moisture in the exiting gas stream.
As will be apparent to those of ordinary skill in this art, the interaction between the gas to be cleansed and the liquid in the container can vary, depending upon the results desired. For example, in some cases a chemical reaction will occur, while in other cases only a scrubbing occurs whereby undesirable gases and particulates are scrubbed from the gas stream without chemical conversion.
We shall now describe our invention as applied to the washing and scrubbing of particular exhaust gas streams utilizing specific embodiments of the invention. As stated previously, this invention is particularly suited to scrubbing the dimethylethylamine (DMEA) gases generated in what is known in the foundry industry as the "chemical" or "cold box" process for making foundry cores or molds. One such process is known as the ISOCURE process referred to previously. Briefly, the core ingredients of sand and a small quantity of a binder, ; approximately 1.5X by weight of the sand, such as about equal parts isocyanate and polyurethane, are mixed and placed into a form. A DMEA gas stream, normally containing 12% DMEA and the balance air or CO2 is then passed through the form for 5-10 seconds followed by a 10-20 second air purge to cure the core.
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1C~79~95 Heretofore, this DMEA exit gas was passed directly to the atmosphere and efforts to scrub the DMEA gas at reasonable cost were characteristically unsuccessful.
One such chemical or cold foundry core making apparatus was equipped with the present invention as shown in the preferred embodiment. The foundry core making apparatus used about 2.25 pounds of DMEA gas (actual DMEA) per hour. Sufficient air was introduced into the gas stream to produce a gas stream of 55 parts oxygen to one part DMEA. The blower was a Spencer vortex side channel blower having a rated horsepower of 3.7 hp. The inlet port and outlet port diameters were 2 inches. The cylindrical container had a diameter of 30.5 inches and a height of 48 inches. One hundred ten gallons of a gas washing liquid were added to the container, resulting in a liquid height of approximately 36 inches from the bottom of the container. The liquid comprised a 5% phosphoric acid solution.
The drive pipe interconnecting the blower with the interior of the container had a two inch inner diameter and its outlet was positioned three inches from the bottom of the container. The drive pipe outlet was positioned so as to expel the gas to be processed downwardly toward the container bottom wall. The static pressure in the pipe had been calculated to be approximate- -ly 1 to 2 psi due to the head of the liquid solution in the container. The liquid level of the washing acid was such that the baffle plate was 4 inches above the top of the liquid when at rest, and the liquid height above the drive pipe outlet was approximately 33 inches. The outlet stack had a 14 inch diameter to reduce the exit flow velocity and any pressure build-up that may have occured in the system. The gas was rapidly drawn in and accelerated by the blower 61 through the `
10~9495 drive pipe 30. The velocity of the gas at the inlet to the blower was measured with an anomometer to be 2240 linear feet per minute (drive pipe exit velocity of approximately 2000 lin.
ft/min).
The accelerated gas entering the acidic liquid solution had a high enough velocity to ensure that its kinetic energy was greater than the threshold energy needed for the reaction to occur. It was noted that the bubbles resulting from this impact velocity had an average diameter of approximately 1/4 inch and each bubble has been calculated to have remained in the solution for an average of approximately 4.9 seconds.
The reaction occurring in the container was as follows:
CH2 CH3 CH2 ~ CH3 C H2 CH 3 H + N . H + :~ N = O - H ~ -/\ /\ /\
: (insoluble in water) (soluble in water) ;~
';
~079495 Some of the product will stay as amino oxides, and some will go to phosphate salts and carbon dioxide. The gas stream exiting from the foregoing described apparatus showed the following analysis:
pH of vapors 6.9 NH3 0.001 ppm formaldehyde none phenol none C0 none CN none C2 traces-but not a pollutant P (phosphorus in any form) 1.75 ppm amine derivatives only traces, but no odor dimethylethylamine less than .lppm (below odor threshold) balance water vapor During the operation of the foregoing system, if the velocity of the gas stream is too slow or the oxygen intake is too low, then the reaction of the gas washing acid and oxygen with the noxious components of the gas does not go to completion and a syrupy chemical is produced which thickens the washing acid into a gelatinous constituency. In contrast, if too great a volume of gas is fed through the system or the acid concentration drops too low the gas will produce a gray precipitate of aminophosphate. Thus, it is necessary to recharge the washing acid periodically, say, one quart of undiluted acid each eight hours of operation. A drive pipe exit gas velocity of about 1800-2800 linear feet per minute is preferred for normal operation of a system of this size.
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la7s4ss We have found that it is not necessary to completely replace the washing acid in this sy~tem except once every three months and in come cases possibly not until after one year of operation. In view of the importance of the oxygen component in the gas stream for scrubbing the DMEA, the volume of oxygen present must be at least twice the volume of DMEA to be scrubbed.
Further, as an alternate to periodic addition of chemicals to the washing liwuid, the apparatus can be equipped with a feeding mechanism to slowly add chemicals to the system on a continuous basis.
As an alternative to the 5% phosphoric acid solution for the gas washing liquid, equally satisfactory acid solution~ could be any dilute phosphoric acids up to 10% as well as dilute acid blends of phosphoric acid and sulphuric acid.
Other acid formulations could also be equally satisfactory.
In the design of our invented apparatus, we prefer a 2 inch i.d. drive pipe, but of course different sizes can be readily adapted depending upon the overall size of the equipment to be employed. With a 2 inch i.d. drive pipe, we have found that the diameter of the container must be at least 2 feet +10% to ensure at least 1 foot +10% unobstructed washing liquid around the drive pipe outlet. Therefore, in larger units using multiple 2 inch i.d. drive pipes, adjacent drive pipes should be at least 2 feet +10% apart, center to center, and each drive pipe should be at least one foot away ; from the closet portion of the container wall. In addition, with the preferred 2 inch i.d. drive pipe, there must be at least one foot of liquid head in the container above the drive pipe opening and preferrably 2-4 feet, and more if multiple drive pipes are employed. In other words, using a 2 inch i.d.
;, . .
~079495 drive pipe, the at rest liquid level of the washing liquid in the container must be at least one foot, and preferably two to four feet above the drive pipe opening using a single drive p~pe.
Based upon the observations and analyses of the DMEA
gas processing operation as above described the following design parameters would prevail in designing other units of different sizes:
CFM (cubic feet per minute) of gas flow to be treated:
cubic ft. of gas washing liquid = .3 x CFM:
gallons of gas washing liquid = .3 x CFM x 7.48:
3/ CU. f~. of sol.
dlameter of conta mer = 2V 7 54 height of solution = 2.4 x r (radius of container):
height of container = 1.3 x ht. of sol.:
diameter of stack = 2 : diameter and number of drive pipes = D = 12 1 -N1r(2240 : 20 (N=number of drive pipes) (Q=flow rate in CFM) : Turbine(s) size to meet CFM requirements:
. In considering the above design parameters and, in particular, the 0.3 multiple factor for determining the needed ` cubic feet of gas washing liquid, those skilled in the art will ; readily appreciate that variations can be tolerated. In fact, so long as the multiple factor is kept within the range 0.11-0.67 the volume of gas washing liquid should be satisfactory to accomplish the desired scrubbing.
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The foregoing drive pipe exit velocities and aboveratios have all been calculated using the turbine inlet velocity because it is the velocity most readily capable of measurement.
The velocity of the gas impacting the liquid from the outlet of the drive pipe at the bottom of the container, which is the critical parameter, is extremely difficult to measure accurately and therefore only approximate impact velocities have been calculated according to the following analysis. Referring to the schematic rendering in Figure 4, the following calculations were undertaken:
Pl = atmospheric pressure P2 = total pressure in pipe P3 = pressure due to solution head P2 ~ Pl + P3 Pl = 14.4 psia locally P3 = liquid head x spec. grav. of sol. x 0.03613 (where 0.03613 is conversion factor inches of water to psi) = 32 in. x 1.068 x 0.03613 = 1.23 psi P2 = 14.4 + 1.23 = 15.63 psi Based upon the foregoing, the approximate impact velocity V2 : can be calculated from the measured pump inlet velocity Vl by the following formula:
~2 = ~4 4 - l5.63 ~079495 It should be apparent that other size containers can be used. The inlet velocity will vary depending upon the conl:ainer size, and the amount of liquid solution in the container. For example, using a tank having a diameter of 24 inches and a height of 36 inches, 50 gallons of solution are placed inside the container and the preferred blower inlet velocity is 1500 linear-ft/min which is equivalent to a drive pipe exit velocity of about 1380 linear ft/min. Using a container having a diameter of 38 inches and a height of 48 inches, 180 gallons of liquid are placed in the container and the preferred blower inlet velocity i8 3,000 linear fttmin, or a drive pipe exit velocity of about 2760 linear ft/min. In the latter system, two drive pipes could be used which would require a blower inlet velocity of at least approximately 2,000 linear ft/min for each blower.
In another embodiment of our invention, an apparatus substantially identical to that described for scrubbing the DNEA foundry core exhaust gases was assembled adjacent to a batch core oven for curing conventional foundry cores. In this core-making process, about 30 parts sand are mixed with about 5 parts of a conventional phenolic resin and 65 parts of a standard exothermic sand core composite. After formed, the ; core is baked at 400-500F. sufficient to set the resin. As a result, gases containing as much as 1% formaldehyde and 4%
phenols are generated. Following treatment with the apparatus ; and method of the present invention using a 10~ by volume acid concentration of 70 parts phosphoric acid (85%) and 30 parts sulphu~ic acid (92-96X) by volume, the exhaust gas stream ;', ' ' .
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~079495 exiting to the atmosphere had the following analysi.s of potential pollutants:
NH3 none Ami.nes none ~l2S (S from natural gas) & S02 none C0 none phenols none P none formaldehyde none pH of solution 6.9 balance water vapor In a further embodiment of the invention, an apparatus . substantially identical to that described for scrubbing the DMEA
, foundry core exhaust gases was used to wash and scrub the '' noxious gases 8enerated i.n an arc welding operation. The gas washing liquid was a 10% solution (by vol.) of an acid component , comprising 70 parts H3P04 (85% conc.) and 30 parts H2S04 (92-96% conc.) by volume and potassium permanganate in an amount equal to 5% by weight of the acid components. An analysis of the arc welding exhaust gases entering the apparatus : of our invention (measured at the weld) and an analysis of the : gas stream as it exits was as follows:
.~, Before After Unit Unit nitrogen oxides traces none ~ C0 5000ppm 50ppm ., dextrin (binder) none none ;~i Mn (particulate) 30ppm none ;! Fe (particulate) 270ppm 108ppm ¦ 30 Cr (particulate) trace none .; ' .
: -22-.
, Before After Unit Unit phenolic compounds (used as binders) some present none balance water vapor water vapor While the present invention has been described primarily with respect to exhaust gases from foundry core manufacturing processes and arc welding operations, it will be understood that the apparatus and method of this invention can be readily adapted by those skilled in the art to any number of industrial processes generating polluting exhaust gases and especially to those noxious gases which lend themselves to chemical conversion in order that they can be scrubbed from the gas stream. Hence, numerous applications for the present invention will readily occur to those skilled in the art as well a8 numerous modifications without departing from the scope of the invention.
For example, the dimensions of the drive pipe might vary along its length and one or more reservoirs might be employed therein for entrapping specific noxious components.
Further, a high voltage electrode could be added near the , entrance of the drive pipe into the container which ionizes the -1 incoming gases to promote a faster reaction, or chemicals or~ -other catalysts might be added in order to promote the necessary chemical reactions. Monitoring devices such as pH meters and vacuum gauges can also be used with the invention. In addition, the present invention contemplates use of the units in series to treat the gas stream with different chemicals in the washing liquid of each unit to separately scrub the various noxious ~ 30 components.
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dlameter of conta mer = 2V 7 54 height of solution = 2.4 x r (radius of container):
height of container = 1.3 x ht. of sol.:
diameter of stack = 2 : diameter and number of drive pipes = D = 12 1 -N1r(2240 : 20 (N=number of drive pipes) (Q=flow rate in CFM) : Turbine(s) size to meet CFM requirements:
. In considering the above design parameters and, in particular, the 0.3 multiple factor for determining the needed ` cubic feet of gas washing liquid, those skilled in the art will ; readily appreciate that variations can be tolerated. In fact, so long as the multiple factor is kept within the range 0.11-0.67 the volume of gas washing liquid should be satisfactory to accomplish the desired scrubbing.
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~ .
The foregoing drive pipe exit velocities and aboveratios have all been calculated using the turbine inlet velocity because it is the velocity most readily capable of measurement.
The velocity of the gas impacting the liquid from the outlet of the drive pipe at the bottom of the container, which is the critical parameter, is extremely difficult to measure accurately and therefore only approximate impact velocities have been calculated according to the following analysis. Referring to the schematic rendering in Figure 4, the following calculations were undertaken:
Pl = atmospheric pressure P2 = total pressure in pipe P3 = pressure due to solution head P2 ~ Pl + P3 Pl = 14.4 psia locally P3 = liquid head x spec. grav. of sol. x 0.03613 (where 0.03613 is conversion factor inches of water to psi) = 32 in. x 1.068 x 0.03613 = 1.23 psi P2 = 14.4 + 1.23 = 15.63 psi Based upon the foregoing, the approximate impact velocity V2 : can be calculated from the measured pump inlet velocity Vl by the following formula:
~2 = ~4 4 - l5.63 ~079495 It should be apparent that other size containers can be used. The inlet velocity will vary depending upon the conl:ainer size, and the amount of liquid solution in the container. For example, using a tank having a diameter of 24 inches and a height of 36 inches, 50 gallons of solution are placed inside the container and the preferred blower inlet velocity is 1500 linear-ft/min which is equivalent to a drive pipe exit velocity of about 1380 linear ft/min. Using a container having a diameter of 38 inches and a height of 48 inches, 180 gallons of liquid are placed in the container and the preferred blower inlet velocity i8 3,000 linear fttmin, or a drive pipe exit velocity of about 2760 linear ft/min. In the latter system, two drive pipes could be used which would require a blower inlet velocity of at least approximately 2,000 linear ft/min for each blower.
In another embodiment of our invention, an apparatus substantially identical to that described for scrubbing the DNEA foundry core exhaust gases was assembled adjacent to a batch core oven for curing conventional foundry cores. In this core-making process, about 30 parts sand are mixed with about 5 parts of a conventional phenolic resin and 65 parts of a standard exothermic sand core composite. After formed, the ; core is baked at 400-500F. sufficient to set the resin. As a result, gases containing as much as 1% formaldehyde and 4%
phenols are generated. Following treatment with the apparatus ; and method of the present invention using a 10~ by volume acid concentration of 70 parts phosphoric acid (85%) and 30 parts sulphu~ic acid (92-96X) by volume, the exhaust gas stream ;', ' ' .
.
.
~079495 exiting to the atmosphere had the following analysi.s of potential pollutants:
NH3 none Ami.nes none ~l2S (S from natural gas) & S02 none C0 none phenols none P none formaldehyde none pH of solution 6.9 balance water vapor In a further embodiment of the invention, an apparatus . substantially identical to that described for scrubbing the DMEA
, foundry core exhaust gases was used to wash and scrub the '' noxious gases 8enerated i.n an arc welding operation. The gas washing liquid was a 10% solution (by vol.) of an acid component , comprising 70 parts H3P04 (85% conc.) and 30 parts H2S04 (92-96% conc.) by volume and potassium permanganate in an amount equal to 5% by weight of the acid components. An analysis of the arc welding exhaust gases entering the apparatus : of our invention (measured at the weld) and an analysis of the : gas stream as it exits was as follows:
.~, Before After Unit Unit nitrogen oxides traces none ~ C0 5000ppm 50ppm ., dextrin (binder) none none ;~i Mn (particulate) 30ppm none ;! Fe (particulate) 270ppm 108ppm ¦ 30 Cr (particulate) trace none .; ' .
: -22-.
, Before After Unit Unit phenolic compounds (used as binders) some present none balance water vapor water vapor While the present invention has been described primarily with respect to exhaust gases from foundry core manufacturing processes and arc welding operations, it will be understood that the apparatus and method of this invention can be readily adapted by those skilled in the art to any number of industrial processes generating polluting exhaust gases and especially to those noxious gases which lend themselves to chemical conversion in order that they can be scrubbed from the gas stream. Hence, numerous applications for the present invention will readily occur to those skilled in the art as well a8 numerous modifications without departing from the scope of the invention.
For example, the dimensions of the drive pipe might vary along its length and one or more reservoirs might be employed therein for entrapping specific noxious components.
Further, a high voltage electrode could be added near the , entrance of the drive pipe into the container which ionizes the -1 incoming gases to promote a faster reaction, or chemicals or~ -other catalysts might be added in order to promote the necessary chemical reactions. Monitoring devices such as pH meters and vacuum gauges can also be used with the invention. In addition, the present invention contemplates use of the units in series to treat the gas stream with different chemicals in the washing liquid of each unit to separately scrub the various noxious ~ 30 components.
., :
.
-- .
Claims (15)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A gas processing apparatus for scrubbing noxious gases and particulate components from a gas stream which comprises:
(a) a closed container having a bottom, a side wall, and a top cover;
(b) a gas washing liquid disposed within said container to a predetermined level;
(c) a substantially horizontal baffle mounted in said container above the liquid level and including peripheral portions spaced inwardly from the opposing inner surfaces of said container;
(d) at least one drive pipe having an inlet positioned outside of said container and extending into the container with its outlet positioned substantially vertically near the bottom of the container and appreciably below said level for high velocity discharge of gas from said drive pipe downwardly into the bottom portion of said liquid;
(e) pumping means for receiving and pumping a gas stream to be processed into the inlet of said drive pipe;
(f) an outlet duct of greater cross-sectional area than said drive pipe opening outwardly from the interior of said container above said baffle plate; and (g) said baffle being spaced only slightly above the liquid level whereby gas-containing bubbles moving upwardly through said liquid will impact against the undersurface of said baffle and thereby cause a major portion of said gas to pass several times through said liquid before passing outwardly from beneath the outer marginal portions of said baffle.
(a) a closed container having a bottom, a side wall, and a top cover;
(b) a gas washing liquid disposed within said container to a predetermined level;
(c) a substantially horizontal baffle mounted in said container above the liquid level and including peripheral portions spaced inwardly from the opposing inner surfaces of said container;
(d) at least one drive pipe having an inlet positioned outside of said container and extending into the container with its outlet positioned substantially vertically near the bottom of the container and appreciably below said level for high velocity discharge of gas from said drive pipe downwardly into the bottom portion of said liquid;
(e) pumping means for receiving and pumping a gas stream to be processed into the inlet of said drive pipe;
(f) an outlet duct of greater cross-sectional area than said drive pipe opening outwardly from the interior of said container above said baffle plate; and (g) said baffle being spaced only slightly above the liquid level whereby gas-containing bubbles moving upwardly through said liquid will impact against the undersurface of said baffle and thereby cause a major portion of said gas to pass several times through said liquid before passing outwardly from beneath the outer marginal portions of said baffle.
2. The apparatus of claim 1 wherein said at least one drive pipe has an inner diameter on the order of 2 inches and is positioned vertically within said container so as to be spaced from the closest portion of the side wall and any adjacent drive pipe a distance of at least approximately six times the inner diameter of the drive pipe.
3. The apparatus of claim 1 wherein said gas washing liquid comprises an acid and has a pH at or below about 5Ø
4. The apparatus of claim 1 wherein said liquid level is spaced below said horizontal baffle approximately 5-10% of the height of the liquid in said container.
5. A method for scrubbing the noxious constituents from a gas stream which comprises the steps of establishing a gas washing liquid in a closed container at a predetermined level, the liquid having a static level at rest slightly below a baffle plate, pumping a gas stream to be processed downwardly through a drive pipe to exit therefrom at a vertical direction into the liquid near the bottom of said container, whereby gas-containing bubbles are formed in said liquid as the gas rises therein; allowing the bubbles to initially rise out of the gas washing liquid beneath the baffle plate to impact against the baffle plate and to thereafter move horizontally outwardly, while still in bubble form, toward the side walls of the container and emerge from beneath the baffle plate adjacent the sides of the container with some of the gases upwardly escaping from the liquid while a substantial portion of the emerging gas bubbles move in a recirculatory path through the liquid downwardly along the side walls of the container toward the bottom thereof, inwardly over the bottom of the container and toward the center line of exit of gas from the drive pipe and thereafter upwardly, by their buoyant action, through the liquid in a zone surrounding and commingling with the initial rise of gases from the drive pipe.
6. A method as claimed in claim 5 wherein the height of said gas-containing bubbles in said gas washing liquid is approximately 30-75% of the height of said liquid when in an at rest state.
7. A method as claimed in claim 5 wherein the gas washing liquid comprises an acidic solution having a pH about 5Ø
8. A method as claimed in claim 7 wherein said acidic solution comprises an acid selected from the group con-sisting of phosphoric acid and a combination of phosphoric acid and sulphuric acid.
9. A method as claimed in claim 5 wherein the pumping step comprises pumping the gas stream to be processed into the container at a sufficiently high velocity so that the kinetic energy of the gases at the point of entry into the gas washing liquid exceeds the threshold energy necessary for a chemical reaction to occur between one or more constituents of the gas stream and the gas washing liquid.
10. A method as claimed in claim 5, wherein the pumping step comprises pumping oxygen into the container along with the gas stream to be processed.
11. A method as claimed in claim 5 wherein the velocity of the gases entering the gas washing liquid is less than 6000 linear feet/min.
12. A method as claimed in claim 5 wherein the velocity of the gases at the point of entry into the gas washing liquid is about 1500-3000 linear feet/min.
13. A method as claimed in claim 12 wherein the flow rate of the gases into the container is between 22 cu. feet/min and 132 cu. feet/min.
14. A method as claimed in claim 12 wherein the flow rate of the gases into the container is about 44-66 cu. feet/min.
15. A method as claimed in claim 5 wherein the ratio of the volume of gas washing liquid in the container to the flow rate of gases pumped into the container is between 0.11 and 0.67.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US62961775A | 1975-11-05 | 1975-11-05 | |
| US73243276A | 1976-10-14 | 1976-10-14 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1079495A true CA1079495A (en) | 1980-06-17 |
Family
ID=27090983
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA264,092A Expired CA1079495A (en) | 1975-11-05 | 1976-10-25 | Apparatus and method for cleansing noxious constituents from gas streams |
Country Status (8)
| Country | Link |
|---|---|
| JP (1) | JPS5921643B2 (en) |
| AU (1) | AU500662B2 (en) |
| BR (1) | BR7607422A (en) |
| CA (1) | CA1079495A (en) |
| DE (1) | DE2649585C3 (en) |
| GB (2) | GB1550415A (en) |
| IT (1) | IT1205917B (en) |
| MX (1) | MX4046E (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5588825A (en) * | 1978-12-27 | 1980-07-04 | Kubota Ltd | Treating method for exhaust gas |
| EP0490202B1 (en) * | 1990-12-14 | 1993-07-14 | MAN Gutehoffnungshütte Aktiengesellschaft | Activated carbon filter for separating noxious gases, such as dioxins and furans, from flue gases before entering the chimney |
| GB2258623B (en) * | 1991-08-12 | 1995-05-10 | Kuo Tien Sung | A waste gas-purifying device |
| CA2104362A1 (en) * | 1993-08-18 | 1995-02-19 | Tien-Sou Kuo | Smoke/gas exhausting and purifying device |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU461078B2 (en) * | 1971-11-10 | 1975-05-15 | Improvements in or relating to vacuum cleaning systems | |
| US3745745A (en) * | 1972-01-28 | 1973-07-17 | Melvin J | Scrubbing apparatus and method |
| FR2173728B1 (en) * | 1972-02-29 | 1974-10-18 | Ugine Kuhlmann |
-
1976
- 1976-10-25 CA CA264,092A patent/CA1079495A/en not_active Expired
- 1976-10-29 DE DE19762649585 patent/DE2649585C3/en not_active Expired
- 1976-11-02 GB GB4543976A patent/GB1550415A/en not_active Expired
- 1976-11-02 GB GB4355478A patent/GB1550416A/en not_active Expired
- 1976-11-05 IT IT2907276A patent/IT1205917B/en active
- 1976-11-05 BR BR7607422A patent/BR7607422A/en unknown
- 1976-11-05 MX MX505076U patent/MX4046E/en unknown
- 1976-11-05 AU AU19363/76A patent/AU500662B2/en not_active Expired
- 1976-11-05 JP JP51133121A patent/JPS5921643B2/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| GB1550415A (en) | 1979-08-15 |
| IT1205917B (en) | 1989-03-31 |
| AU500662B2 (en) | 1979-05-31 |
| GB1550416A (en) | 1979-08-15 |
| AU1936376A (en) | 1978-05-11 |
| JPS5289569A (en) | 1977-07-27 |
| MX4046E (en) | 1981-11-23 |
| DE2649585A1 (en) | 1977-05-12 |
| DE2649585C3 (en) | 1981-02-19 |
| DE2649585B2 (en) | 1980-06-19 |
| BR7607422A (en) | 1977-10-11 |
| JPS5921643B2 (en) | 1984-05-21 |
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