CA1258159A - Reduction of nitrogen- and carbon-based pollutants - Google Patents
Reduction of nitrogen- and carbon-based pollutantsInfo
- Publication number
- CA1258159A CA1258159A CA000519894A CA519894A CA1258159A CA 1258159 A CA1258159 A CA 1258159A CA 000519894 A CA000519894 A CA 000519894A CA 519894 A CA519894 A CA 519894A CA 1258159 A CA1258159 A CA 1258159A
- Authority
- CA
- Canada
- Prior art keywords
- urea
- effluent
- process according
- solution
- hexamethylenetetramine
- 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
Links
Landscapes
- Treating Waste Gases (AREA)
Abstract
REDUCTION OF NITROGEN- AND CARBON-BASED
POLLUTANTS
ABSTRACT
Disclosed is a process for reducing nitrogen oxides in an effluent from the combustion of a carbonaceous fuel under oxygen-rich conditions which minimize the production of carbon-based pollutants.
A dispersion of a solution comprising at least one additive compound selected from the group consisting of guanidine, guanidine carbonate, biguanide, guanylurea sulfate, melamine, dicyandiamide, calcium cyanamide, biuret, 1,1'-azobisformamide, methylol urea, methylol urea-urea condensation product, dimethylol urea, methyl urea, dimethyl urea, and hexamethylenetetramine is injected into an effluent at a temperature above 1300°F, and preferably above 1500°F. The concentration of the additive compound in solution, the temperature of the effluent at the point of injection, and the size of the droplets in the dispersion, are selected to provide a reduction in nitrogen oxides. When urea is employed in combination with hexamethylenetetramine, the effectiveness of the urea is enhanced, particularly at temperatures 1800°F and below.
POLLUTANTS
ABSTRACT
Disclosed is a process for reducing nitrogen oxides in an effluent from the combustion of a carbonaceous fuel under oxygen-rich conditions which minimize the production of carbon-based pollutants.
A dispersion of a solution comprising at least one additive compound selected from the group consisting of guanidine, guanidine carbonate, biguanide, guanylurea sulfate, melamine, dicyandiamide, calcium cyanamide, biuret, 1,1'-azobisformamide, methylol urea, methylol urea-urea condensation product, dimethylol urea, methyl urea, dimethyl urea, and hexamethylenetetramine is injected into an effluent at a temperature above 1300°F, and preferably above 1500°F. The concentration of the additive compound in solution, the temperature of the effluent at the point of injection, and the size of the droplets in the dispersion, are selected to provide a reduction in nitrogen oxides. When urea is employed in combination with hexamethylenetetramine, the effectiveness of the urea is enhanced, particularly at temperatures 1800°F and below.
Description
C~ ~5~3 Technical Field The present invention relates to improvements in the combustion of carbonaceous fuels, and more particularly to improvements in firing boilers with reduced emissions of carbon- and nitrogen-based pollutants.
Carbonaceous fuels burn more completely, with reduced emissions of carbon monoxide and unburned hydrocarbons, at oxygen concentrations and combustion air~fuel ratios which permit optimized high flame temperatures. When fossil fuels are used to fire large utility boilers, these temperatures are above 2000F and typically from about 2200F to 3000F. Unfortunately, these high temperatures and hot spots of higher temperature tend to result in the production of thermal NOX -- the temperatures being so high that free radicals of nitrogen and oxygen are formed and chemically combine as nitrogen oxides (NOX).
~L ~ r ~ L rj ~ ~
The flame temperature can be lowered to reduce NOX formation by the use of large excesses of air or fuel, or a hybrid of both processes known as staged combustion. However, these approaches create excessive carbon-based pollutants. There is no known set of conditions which can simultaneously reduce nitrogen- and carbon-based pollutants to acceptable levels without incurring severe economic penalties.
Background Art The need to reduce nitrogen- and carbon-based emissions while maintaining economic operation is a concern wherever carbonaceous fuels are burned. The requirements of each system for efficiency of fuel consumption must, of course, be considered in order to have a practical system.
In US Patent 3,599,427 to Jones et al, there is described a two stage catalytic system for treating the exhaus-t gases of mobile internal combustion engines. In the first catalytic stage, hot exhaust gases directly from an engine are treated at a high temperature to oxidize carbon monoxide and unburned hydrocarbons. The resulting exhaust gases are then cooled and passed through a separate, second catalytic stage to reduce levels of nitrogen monoxide. Prior to contact with the second stage catalyst, ammonia gas and other compounds such as urea, ammonium hydroxide, ammonium carbonate, and hexamethylenetetramine, are mixed with the exhaust gases. Upon contact with the second stage catalyst, nitrogen oxides are reduced to produce nitrogen and water.
&1~
In US Patent 3,846,981, Pacztowski discloses a more detailed, controlled two-stage catalytic system. The operating temperatures for the second catalytic stage where ammonia is utilized, are preferably within the range of from 275F to 900F.
This process and that of Jones et al unfortunately depend on the use of catalysts which create additional costs in terms of initial investment and servicing reguirements.
In US Patent 3,900,554, Lyon discloses a non-catalytic system for reducing nitrogen monoxide (NO) in a combustion effluent. Lyon discloses that ammonia and specified ammonia precursors, including ammonium carbonate also disclosed by Jones, et al, or their aqueous solutions, can be injected into the effluent for mixing with the nitrogen monoxide at a temperature within the range of 1600F to 2000F.
In one embodiment of the disclosed process, a reducing agent, such as hydrogen gas or various hydrocarbons, can be mixed with the effluent to permit the reduction reaction to occur at temperatures as low as 1300F, thereby assuring avoidance of high temperature oxidation of ammonia to nitrogen monoxide. Lyon points out that at temperatures above 2000F, the use of ammonia was counterproductive -- increasing NO rather than decreasing it.
Unfortunately, large industrial boilers operate at temperatures significantly above 2000F, and access to the interior of the heat exchangers where the 1600F to 2000F temperature exists following the flame zone of the boilers is not practical without major redesign due to exterior water jacketing and interior water tubes. At the exhaust end of the boilers, the temperature is reduced far below the minimum temperature of 1300F which can be used when a reducing agent is employed. Thus, the effective temperature range cannot be readily accessed for non-catalytic operability of Lyon's teaching in many large industrial boilers and certain other NOx-producing combustion equipment.
In US Patent 3,961,018, Williamson discloses the purification of acid gas-containing streams at low temperatures approaching ambient. Williamson discloses contacting the gas stream with an amine vapor in sufficient concentration such that its partial pressure is at least 5% of the total pressure of the gas stream. This system thus requires large amounts of the treating gas and requires equipment for separating that gas from the effluent upon completing the treatment.
In a somewhat different environment, Goldstein et al, in US Patent 4,0~1,597 indicate that temperatures within the range of 1000 to 1300F are effective when using urea for reducing brown fumes caused by nitrogen dioxide ~NO2) from catalyst treatment effluents. One example in the patent employs a 30 weight percent aqueous solution of urea. Again, however, the temperature range of 1000~F to 1300F is not practical for treatment of effluents from many types of combustion equipment.
In US Patent 4,325,924, Arand et al disclose the non-catalytic urea reduction of nitrogen oxides in fuel-rich combustion effluents. They indicate that under fuel-rich conditions, aqueous solutions 5 ~ 3 of urea at concentrations of greater than 10%, and preferably greater than 20%, are effective nitrogen oxide reducers at temperatures in excess of 1900F.
Unfortuna~ely, this effluent from staged combustion results in the production of high levels of carbonaceous pollutants.
In US Patent 4,208,386, on the other hand, Arand et al disclose that for oxygen-rich effluents, the temperature is in the range of from 1300F to 2000F for urea added dry or as a solution in water alone or with an alkanoic solvent. The use of the alkanoic solvent is said to enable reduction of the effective operating temperature to below 1600F. No function, other than carrier for the urea, was disclosed for the water.
Operation under fuel-rich conditions has the disadvantages that combustion has been incomplete and carbon-based pollutants are excessive. Thus, despite the apparent ability of ~rand et al to add the urea solution to fuel-rich effluents at temperatures abov~ 1900F for reduction of nitrogen-based pollutants, this fuel-rich operation has economic and environmental penalties. And, operation under oxygen-rich conditions to achieve the desirable economies of fuel utilization and reduced carbon-based pollutants, causes practical difficulties in supplying the urea, ammonia or other useful material to a boiler under conditions where it will have its intended effect of reducing the levels of nitrogen oxide pollutants. Moreover, the present invention shows that urea is not as effective as would be desired in reducing levels of nitrogen oxides.
5~
Accordingly, there is a present need for a process which enables the more efficient reduction of nitrogen-based pollutants while operating under efficient oxygen-rich conditions which minimize carbon-based pollutants.
Disclosure of Invention The present invention provides a process for reducing the concentration of nitrogen oxides in an oxygen-rich effluent from the combustion of a carbonaceous fuel. The process co~prises inj~cting a solution comprising at least one additive compound selected from the group consisting of guanidine, guanidine carbonate, biguanide, guanylurea sulfate, melamine, dicyandiamide, calcium cyanamide, biuret, l,l'-azobisformamide, methylol urea, methylol urea-urea condensation product, dimethylol urea, methyl urea, dimethyl urea, and hexamethylene-tetramine, into said effluent. The temperature of the effluent at the point of injection, the concentration of the additive compound in the solution, and the size of the droplets in the dispersion, are selected to achieve reduction in nitrogen oxide levels in the effluent. A preferred embodiment of the invention provides for introducing an aqueous solution of hexamethylenetetramine and urea. Injection is preferably done at a plurality of spaced positions and at a uniform droplet size within the range of from about 10 to about 10,000 microns Sauter mean diameter. Variations of particle sizes within this broad range have been found effective to achieve uniform mixing of the additive compound with the effluent gas at a temperature in excess of 1300F.
15~3 For the purposes of this description, all temperatures herein are measured using an unshielded K-type thermocouple. Droplet sizes are determined with a Malvern 2200 instrument, utilizing a Franhofer diffraction, laser-based system. And, unless otherwise indicated, all parts and percentayes are based on the weight of the composition at the particular point of reference.
In addition to khe named additive compounds, which can be employed alone or in combination, urea and materials such as ammonium carbonate, ammonium oxalate, ammonia, hydrazine, ammonium hydroxide, and various amines can be employed with the named additive compounds.
Aqueous solutions are preferred according to the present invention due to their economy and can be employed with suitable effectiveness in most situations. The effective solutions will vary from saturated to dilute. While water will be an effective solvent for most applications, there are instances where other solvents may be advantageous in combination with water.
The temperature of the effluent will have an influence on the concentration of the solution. At temperatures of from about 1300F to about 2000F, the solution will tend to operate effectively at high concentration, e.g., from 25 to 40 weight percent. On the other hand, at temperatures in excess of 2000F, the solution will tend toward very dilute solutions. At these high temperatures, the water may comprise greater than 80%, 85% or 90% by weight of the solution, with the additive compound ~.~5~315~
comprising as low as from about 0.5 to about 10% by weight of the solution.
It has been found that at temperatures within the above range, and particularly below 1800F with fine atomization of the solution, hexamethylene-tetramine is utilized to a greater extent than urea, being almost totally consumed during its interaction with N0x under proper conditions. It is further surprising that, when used in combination with urea, hexamethylenetetramine actually increases the utilization of the urea in reducing NOX. Thus, hexamethylenetetramine is an enhancer for urea utilization in addition to being a superior N0x reducing agent in its own right.
Combinations of the named additive compounds are employed as N0x reduction optimization and economics dictate. Preferably, hexamethylene-tetramine will be present in an amount of at least about 25% based on the combined weight of it and the other active N0x reducer such as urea. Weight ratios of hexamethylenetetramine to urea of from about 1:3 to 3:1 are exemplary.
The solution of additive compound will be dispersed uniformly within the effluent gas stream at a point where the effluent is at a temperature above 1300F, and preferably above 1500F. Large industrial boilers of the type employed for utility power plants and other large facilities, will typically be water jacketted and have access only at limited points. In the most typical situation, the boiler interior can be accessed only in the area of the flame and at an area above the flame, where the temperatures at full load are typically within the range of from about 2200F to about 2600~F. For boilers operating efficlently with gas, the temperature at this point of access will typically fall within the range of from about 2100F to about
Carbonaceous fuels burn more completely, with reduced emissions of carbon monoxide and unburned hydrocarbons, at oxygen concentrations and combustion air~fuel ratios which permit optimized high flame temperatures. When fossil fuels are used to fire large utility boilers, these temperatures are above 2000F and typically from about 2200F to 3000F. Unfortunately, these high temperatures and hot spots of higher temperature tend to result in the production of thermal NOX -- the temperatures being so high that free radicals of nitrogen and oxygen are formed and chemically combine as nitrogen oxides (NOX).
~L ~ r ~ L rj ~ ~
The flame temperature can be lowered to reduce NOX formation by the use of large excesses of air or fuel, or a hybrid of both processes known as staged combustion. However, these approaches create excessive carbon-based pollutants. There is no known set of conditions which can simultaneously reduce nitrogen- and carbon-based pollutants to acceptable levels without incurring severe economic penalties.
Background Art The need to reduce nitrogen- and carbon-based emissions while maintaining economic operation is a concern wherever carbonaceous fuels are burned. The requirements of each system for efficiency of fuel consumption must, of course, be considered in order to have a practical system.
In US Patent 3,599,427 to Jones et al, there is described a two stage catalytic system for treating the exhaus-t gases of mobile internal combustion engines. In the first catalytic stage, hot exhaust gases directly from an engine are treated at a high temperature to oxidize carbon monoxide and unburned hydrocarbons. The resulting exhaust gases are then cooled and passed through a separate, second catalytic stage to reduce levels of nitrogen monoxide. Prior to contact with the second stage catalyst, ammonia gas and other compounds such as urea, ammonium hydroxide, ammonium carbonate, and hexamethylenetetramine, are mixed with the exhaust gases. Upon contact with the second stage catalyst, nitrogen oxides are reduced to produce nitrogen and water.
&1~
In US Patent 3,846,981, Pacztowski discloses a more detailed, controlled two-stage catalytic system. The operating temperatures for the second catalytic stage where ammonia is utilized, are preferably within the range of from 275F to 900F.
This process and that of Jones et al unfortunately depend on the use of catalysts which create additional costs in terms of initial investment and servicing reguirements.
In US Patent 3,900,554, Lyon discloses a non-catalytic system for reducing nitrogen monoxide (NO) in a combustion effluent. Lyon discloses that ammonia and specified ammonia precursors, including ammonium carbonate also disclosed by Jones, et al, or their aqueous solutions, can be injected into the effluent for mixing with the nitrogen monoxide at a temperature within the range of 1600F to 2000F.
In one embodiment of the disclosed process, a reducing agent, such as hydrogen gas or various hydrocarbons, can be mixed with the effluent to permit the reduction reaction to occur at temperatures as low as 1300F, thereby assuring avoidance of high temperature oxidation of ammonia to nitrogen monoxide. Lyon points out that at temperatures above 2000F, the use of ammonia was counterproductive -- increasing NO rather than decreasing it.
Unfortunately, large industrial boilers operate at temperatures significantly above 2000F, and access to the interior of the heat exchangers where the 1600F to 2000F temperature exists following the flame zone of the boilers is not practical without major redesign due to exterior water jacketing and interior water tubes. At the exhaust end of the boilers, the temperature is reduced far below the minimum temperature of 1300F which can be used when a reducing agent is employed. Thus, the effective temperature range cannot be readily accessed for non-catalytic operability of Lyon's teaching in many large industrial boilers and certain other NOx-producing combustion equipment.
In US Patent 3,961,018, Williamson discloses the purification of acid gas-containing streams at low temperatures approaching ambient. Williamson discloses contacting the gas stream with an amine vapor in sufficient concentration such that its partial pressure is at least 5% of the total pressure of the gas stream. This system thus requires large amounts of the treating gas and requires equipment for separating that gas from the effluent upon completing the treatment.
In a somewhat different environment, Goldstein et al, in US Patent 4,0~1,597 indicate that temperatures within the range of 1000 to 1300F are effective when using urea for reducing brown fumes caused by nitrogen dioxide ~NO2) from catalyst treatment effluents. One example in the patent employs a 30 weight percent aqueous solution of urea. Again, however, the temperature range of 1000~F to 1300F is not practical for treatment of effluents from many types of combustion equipment.
In US Patent 4,325,924, Arand et al disclose the non-catalytic urea reduction of nitrogen oxides in fuel-rich combustion effluents. They indicate that under fuel-rich conditions, aqueous solutions 5 ~ 3 of urea at concentrations of greater than 10%, and preferably greater than 20%, are effective nitrogen oxide reducers at temperatures in excess of 1900F.
Unfortuna~ely, this effluent from staged combustion results in the production of high levels of carbonaceous pollutants.
In US Patent 4,208,386, on the other hand, Arand et al disclose that for oxygen-rich effluents, the temperature is in the range of from 1300F to 2000F for urea added dry or as a solution in water alone or with an alkanoic solvent. The use of the alkanoic solvent is said to enable reduction of the effective operating temperature to below 1600F. No function, other than carrier for the urea, was disclosed for the water.
Operation under fuel-rich conditions has the disadvantages that combustion has been incomplete and carbon-based pollutants are excessive. Thus, despite the apparent ability of ~rand et al to add the urea solution to fuel-rich effluents at temperatures abov~ 1900F for reduction of nitrogen-based pollutants, this fuel-rich operation has economic and environmental penalties. And, operation under oxygen-rich conditions to achieve the desirable economies of fuel utilization and reduced carbon-based pollutants, causes practical difficulties in supplying the urea, ammonia or other useful material to a boiler under conditions where it will have its intended effect of reducing the levels of nitrogen oxide pollutants. Moreover, the present invention shows that urea is not as effective as would be desired in reducing levels of nitrogen oxides.
5~
Accordingly, there is a present need for a process which enables the more efficient reduction of nitrogen-based pollutants while operating under efficient oxygen-rich conditions which minimize carbon-based pollutants.
Disclosure of Invention The present invention provides a process for reducing the concentration of nitrogen oxides in an oxygen-rich effluent from the combustion of a carbonaceous fuel. The process co~prises inj~cting a solution comprising at least one additive compound selected from the group consisting of guanidine, guanidine carbonate, biguanide, guanylurea sulfate, melamine, dicyandiamide, calcium cyanamide, biuret, l,l'-azobisformamide, methylol urea, methylol urea-urea condensation product, dimethylol urea, methyl urea, dimethyl urea, and hexamethylene-tetramine, into said effluent. The temperature of the effluent at the point of injection, the concentration of the additive compound in the solution, and the size of the droplets in the dispersion, are selected to achieve reduction in nitrogen oxide levels in the effluent. A preferred embodiment of the invention provides for introducing an aqueous solution of hexamethylenetetramine and urea. Injection is preferably done at a plurality of spaced positions and at a uniform droplet size within the range of from about 10 to about 10,000 microns Sauter mean diameter. Variations of particle sizes within this broad range have been found effective to achieve uniform mixing of the additive compound with the effluent gas at a temperature in excess of 1300F.
15~3 For the purposes of this description, all temperatures herein are measured using an unshielded K-type thermocouple. Droplet sizes are determined with a Malvern 2200 instrument, utilizing a Franhofer diffraction, laser-based system. And, unless otherwise indicated, all parts and percentayes are based on the weight of the composition at the particular point of reference.
In addition to khe named additive compounds, which can be employed alone or in combination, urea and materials such as ammonium carbonate, ammonium oxalate, ammonia, hydrazine, ammonium hydroxide, and various amines can be employed with the named additive compounds.
Aqueous solutions are preferred according to the present invention due to their economy and can be employed with suitable effectiveness in most situations. The effective solutions will vary from saturated to dilute. While water will be an effective solvent for most applications, there are instances where other solvents may be advantageous in combination with water.
The temperature of the effluent will have an influence on the concentration of the solution. At temperatures of from about 1300F to about 2000F, the solution will tend to operate effectively at high concentration, e.g., from 25 to 40 weight percent. On the other hand, at temperatures in excess of 2000F, the solution will tend toward very dilute solutions. At these high temperatures, the water may comprise greater than 80%, 85% or 90% by weight of the solution, with the additive compound ~.~5~315~
comprising as low as from about 0.5 to about 10% by weight of the solution.
It has been found that at temperatures within the above range, and particularly below 1800F with fine atomization of the solution, hexamethylene-tetramine is utilized to a greater extent than urea, being almost totally consumed during its interaction with N0x under proper conditions. It is further surprising that, when used in combination with urea, hexamethylenetetramine actually increases the utilization of the urea in reducing NOX. Thus, hexamethylenetetramine is an enhancer for urea utilization in addition to being a superior N0x reducing agent in its own right.
Combinations of the named additive compounds are employed as N0x reduction optimization and economics dictate. Preferably, hexamethylene-tetramine will be present in an amount of at least about 25% based on the combined weight of it and the other active N0x reducer such as urea. Weight ratios of hexamethylenetetramine to urea of from about 1:3 to 3:1 are exemplary.
The solution of additive compound will be dispersed uniformly within the effluent gas stream at a point where the effluent is at a temperature above 1300F, and preferably above 1500F. Large industrial boilers of the type employed for utility power plants and other large facilities, will typically be water jacketted and have access only at limited points. In the most typical situation, the boiler interior can be accessed only in the area of the flame and at an area above the flame, where the temperatures at full load are typically within the range of from about 2200F to about 2600~F. For boilers operating efficlently with gas, the temperature at this point of access will typically fall within the range of from about 2100F to about
2 6 0 0 n F, and when fired with coal or oil, will typically fall within the range of about 2050F to 2400~F. At these temperatures, the effective introduction of additive compound solutions can be accomplished at lower concentrations and employing dispersions having larger droplet sizes.
The additive compound solutions according to the present invention are preferably injected at a number of spaced points from nozzles which are effective to uniformly form and disperse droplets of the solutions within the flowing effluent stream to achieve uniform mixing. Preferably, the size of the droplets of solution will be within the range of from about 10 to about 10,000, and preferably within the range of from about 50 to 10,000 microns Sauter mean diameter. At temperatures below 2000~F, droplet slzes of less than 150 microns are quite effective, while at higher temperatures the droplets should be larger, preferably larger than 500 microns.
The concentration of the additive compound or compounds within the effluent gas should be sufficient to provide a reduction in nitrogen oxide levels. Typically, the additive compound will be employed at a molar ratio of nitrogen in the additive compound to the baseline nitrogen oxide level of from about 1 to 10 to 2 to 1, and will more preferably be within the range of from about 1 to 4 to 3 to 2.
Best Mode for Carryinq out the Invention The following examples further illustrate and explain the invention by detailing the operation not only of a small scale burner, but also of a commercial utility boiler system, with reduction in nitrogen oxide emmissions.
Example 1 A home heating burner fitted with a 1.25 gallon per hour nozzle firing a slight excess of oxygen, was run for an initial period of time to establish baseline operating conditions, with oxygen (2) and nitrogen oxides (NOX) measured and recorded as shown in the table below in two independent tests. In the test with urea, after reaching an operating temperature of 1550F, a 7.2% (w/v) urea solution was sprayed at a rate of 240 ml/hour into the effluent at a point about six feet downstream of the burner nozzle, and values for 2 and NOX were recorded at the temperatures indicated. In the test with hexamethylenetetramine (HMTA), again after reaching a temperature of 1550F, a 9.5% (w/v) solution of hexamethylenetetramine was sprayed into the effluent at the same rate and point as the spray in test 1, and again values for 2 and NOX were recorded at the indicated temperatures. For each test, the supply of solution was terminated when the indicated temperature reached 2000F. The results are shown in table 1.
TABLE I
_ _ _ . _ _ UREA HMTA
Temp 0 N-0 ~- ~- --- NOx ~~ % N0 5 (F) (~) (ppm) red. (~) (ppm) red X
15504.7132 - 4.8 132 1600 - - - 4.7 ~5 36 17004.9 98 26 4.6 70 47 1800 - 107 19 4.6 87 34 20~04.9llQ 17 4.9 86 35 ~ Corrected to 3.0~ oxygen excess in effluent.
Example 2 A Babcock & Wilcox 110 megawatt utility boiler was fired with residual fuel oil through ten Peabody burnexs to achieve 80 megawatt output. At 7 locations, about 48 feet above the uppermost burners, a series of medium-to-course droplet forming atomizers were positioned to inject treatment solutions into the effluent which was at an average temperature of about 1600F. The following runs were made:
(1) a baseline run with no treatment solution;
(2) a 15 weight percent solution oE hexamethy-lenetetramine ~HMTA) in water supplied at a molar ratio of HMTA to baseline NOX of 0.125 and injected at 5 psi to give droplets having a Sauter mean diameter of from about 150 to 200 microns;
The additive compound solutions according to the present invention are preferably injected at a number of spaced points from nozzles which are effective to uniformly form and disperse droplets of the solutions within the flowing effluent stream to achieve uniform mixing. Preferably, the size of the droplets of solution will be within the range of from about 10 to about 10,000, and preferably within the range of from about 50 to 10,000 microns Sauter mean diameter. At temperatures below 2000~F, droplet slzes of less than 150 microns are quite effective, while at higher temperatures the droplets should be larger, preferably larger than 500 microns.
The concentration of the additive compound or compounds within the effluent gas should be sufficient to provide a reduction in nitrogen oxide levels. Typically, the additive compound will be employed at a molar ratio of nitrogen in the additive compound to the baseline nitrogen oxide level of from about 1 to 10 to 2 to 1, and will more preferably be within the range of from about 1 to 4 to 3 to 2.
Best Mode for Carryinq out the Invention The following examples further illustrate and explain the invention by detailing the operation not only of a small scale burner, but also of a commercial utility boiler system, with reduction in nitrogen oxide emmissions.
Example 1 A home heating burner fitted with a 1.25 gallon per hour nozzle firing a slight excess of oxygen, was run for an initial period of time to establish baseline operating conditions, with oxygen (2) and nitrogen oxides (NOX) measured and recorded as shown in the table below in two independent tests. In the test with urea, after reaching an operating temperature of 1550F, a 7.2% (w/v) urea solution was sprayed at a rate of 240 ml/hour into the effluent at a point about six feet downstream of the burner nozzle, and values for 2 and NOX were recorded at the temperatures indicated. In the test with hexamethylenetetramine (HMTA), again after reaching a temperature of 1550F, a 9.5% (w/v) solution of hexamethylenetetramine was sprayed into the effluent at the same rate and point as the spray in test 1, and again values for 2 and NOX were recorded at the indicated temperatures. For each test, the supply of solution was terminated when the indicated temperature reached 2000F. The results are shown in table 1.
TABLE I
_ _ _ . _ _ UREA HMTA
Temp 0 N-0 ~- ~- --- NOx ~~ % N0 5 (F) (~) (ppm) red. (~) (ppm) red X
15504.7132 - 4.8 132 1600 - - - 4.7 ~5 36 17004.9 98 26 4.6 70 47 1800 - 107 19 4.6 87 34 20~04.9llQ 17 4.9 86 35 ~ Corrected to 3.0~ oxygen excess in effluent.
Example 2 A Babcock & Wilcox 110 megawatt utility boiler was fired with residual fuel oil through ten Peabody burnexs to achieve 80 megawatt output. At 7 locations, about 48 feet above the uppermost burners, a series of medium-to-course droplet forming atomizers were positioned to inject treatment solutions into the effluent which was at an average temperature of about 1600F. The following runs were made:
(1) a baseline run with no treatment solution;
(2) a 15 weight percent solution oE hexamethy-lenetetramine ~HMTA) in water supplied at a molar ratio of HMTA to baseline NOX of 0.125 and injected at 5 psi to give droplets having a Sauter mean diameter of from about 150 to 200 microns;
(3) the same conclitions as (2~, but injecting a hexamethylenetetramine solution at a concentration of only 6%; and
(4) the same as (3), but employing a 15 weight percent solution of HMTA in water and supplying it at a molar ratio of HMTA to NOX of O .5.
The tests are summarized, and the results recorded in Table 2.
TAB~ 2 Run HMTAMolar ~atio NO NO Reduction (Wt. %) (HMTA to NO)(ppm) (%) (1) -- __ 222 -~
(2) 15 0.125 ~84 17 (3) 6 0.125 187 16 (4) 15 0.5 101 55 Corrected to 3.0% oxygen excess in the effluent.
Example 3 The boiler referred to in Example 2 was fired to 108 megawatt output. Treatment solutions were injected into the effluent at an average effluent temperature of about 2100F. The products of combustion contained a level of NO which equated to about 10 moles per hour.
~S~
The following runs were made:
The tests are summarized, and the results recorded in Table 2.
TAB~ 2 Run HMTAMolar ~atio NO NO Reduction (Wt. %) (HMTA to NO)(ppm) (%) (1) -- __ 222 -~
(2) 15 0.125 ~84 17 (3) 6 0.125 187 16 (4) 15 0.5 101 55 Corrected to 3.0% oxygen excess in the effluent.
Example 3 The boiler referred to in Example 2 was fired to 108 megawatt output. Treatment solutions were injected into the effluent at an average effluent temperature of about 2100F. The products of combustion contained a level of NO which equated to about 10 moles per hour.
~S~
The following runs were made:
(5) a baseline run with no treatment solution;
(6) a 3.5% solution of urea in water supplied at a molar ratio of urea to bas~line NO of 0.20 and S injected to 5 psi to gi~e droplets having a Sauter mean diameter of from about 150 to 200 microns, this solution supplying about 2 moles of urea per hour;
(7) as (6), but employing a co~bination of urea and hexamethylenetetramine (HMTA) at a molar ratio of chemicals to baseline N0 of 0.18, this solution supplying about 1 mole per hour of urea and about 0.8 moles per hour of HMTA.
The tests are summarized, and the results recorded in Table 3.
Run HMTA Urea Molar Ratio N0 N0 Reduction (Wt. %) (Wt. %) (to N0) (ppm) (%) (5) ~ 299.6 --(6) -- 3.5 0.2 226.45 24.5 (7) 1.75 1.75 0.18 174 41.9 It can be noted from the data in Table 3 that the 24.4% reduction of NO achieved when using urea, utilizes only about half of the urea; but that the 41.9% reduction achieved when the combinatlon is employed evidenc~s nea~ complete utilization of both the urea and HMTA.
Exam~le 4 The procedure of Example 1 is repeated for the additive compounds and combinations of them set forth in Table 4 below. The temperatures of the effluent, concentration of solutions, and feed rates are changed from Example 1 as indicated in Table 4.
TAB~ 4 -Concen- Feed --N0x (ppm)--tration Rate Temp Base % Reduc-Additive Compound (w/v) (ml~hr) (F) Line Treated tion Biuret 11.4% 280 1800- 123 77 37.4 ~ 1850 Dimethylol Urea 2Q% 280 1800- 122 75 38.6 20 Guanidine 10%280 1800- 120 80 33.3 Carbonate , 1850 Guanylurea 14.1% 280 1800- 121 71 41.4 Sulfate 1850 XMTA 12% 280 1800- 120 79 34.2 ~ 1850 Methylol Urea 15% 280 1800- 122 70 42.7 Urea 10% 280 1800- 122 72 41 30 Dimethyl Urea 14.7% 420 1790 -- -- 42 Methyl Urea 12.3% 420 1785 -- -- 43 Urea + HMTA 7% & 3% 420 1780 -- -- 37.5 l,l'-azobis- 18.5% 420 1790 -- -- 52 formanide 35 Melamine 3.5% 560 1800 115 90 21.8 Additives were not completely soluble under conditions tested and N0 levels fluctuated with the indicated treated levelXbeing the low value.
~5~15~
The above description is for the purpose of teaching the person of ordinary skill in the art how to practice the present invention, and it is not intended to detail all those obvious modifications and variations of it which will become apparent to the skilled worker upon reading the description. It is intended, however, that all such obvious modifications and variations be included within the scope of the present invention which is defined by the following claims.
The tests are summarized, and the results recorded in Table 3.
Run HMTA Urea Molar Ratio N0 N0 Reduction (Wt. %) (Wt. %) (to N0) (ppm) (%) (5) ~ 299.6 --(6) -- 3.5 0.2 226.45 24.5 (7) 1.75 1.75 0.18 174 41.9 It can be noted from the data in Table 3 that the 24.4% reduction of NO achieved when using urea, utilizes only about half of the urea; but that the 41.9% reduction achieved when the combinatlon is employed evidenc~s nea~ complete utilization of both the urea and HMTA.
Exam~le 4 The procedure of Example 1 is repeated for the additive compounds and combinations of them set forth in Table 4 below. The temperatures of the effluent, concentration of solutions, and feed rates are changed from Example 1 as indicated in Table 4.
TAB~ 4 -Concen- Feed --N0x (ppm)--tration Rate Temp Base % Reduc-Additive Compound (w/v) (ml~hr) (F) Line Treated tion Biuret 11.4% 280 1800- 123 77 37.4 ~ 1850 Dimethylol Urea 2Q% 280 1800- 122 75 38.6 20 Guanidine 10%280 1800- 120 80 33.3 Carbonate , 1850 Guanylurea 14.1% 280 1800- 121 71 41.4 Sulfate 1850 XMTA 12% 280 1800- 120 79 34.2 ~ 1850 Methylol Urea 15% 280 1800- 122 70 42.7 Urea 10% 280 1800- 122 72 41 30 Dimethyl Urea 14.7% 420 1790 -- -- 42 Methyl Urea 12.3% 420 1785 -- -- 43 Urea + HMTA 7% & 3% 420 1780 -- -- 37.5 l,l'-azobis- 18.5% 420 1790 -- -- 52 formanide 35 Melamine 3.5% 560 1800 115 90 21.8 Additives were not completely soluble under conditions tested and N0 levels fluctuated with the indicated treated levelXbeing the low value.
~5~15~
The above description is for the purpose of teaching the person of ordinary skill in the art how to practice the present invention, and it is not intended to detail all those obvious modifications and variations of it which will become apparent to the skilled worker upon reading the description. It is intended, however, that all such obvious modifications and variations be included within the scope of the present invention which is defined by the following claims.
Claims (20)
OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
l. A process for reducing the concentration of nitrogen oxides in an oxygen-rich effluent from the combustion of a carbonaceous fuel, which process comprises injecting a solution comprising at least one additive compound selected from the group consisting of guanidine, guanidine carbonate, biguanide, guanylurea sulfate, melamine, dicyandiamide, calcium cyanamide, biuret,
1,1'-azobisformamide, methylol urea, methylol urea-urea condensation product, dimethylol urea, methyl urea, dimethyl urea, and hexamethylene-tetramine, at a concentration and a temperature effective to achieve reduction in nitrogen oxide levels in the effluent.
2. A process according to claim 1 wherein the temperature of the effluent is greater than 1300°F
at the point of injection.
at the point of injection.
3. A process according to claim 1 wherein the solvent comprises water.
4. A process according to claim 1 wherein the additive compound comprises hexamethylenetetramine and the solution is injected into the effluent in amounts sufficient to provide a molar ratio of hexamethylenetetramine to nitrogen oxides of from 1:6 to 2:1.
5. A process according to claim 4 wherein the ratio of hexamethylenetetramine to nitrogen oxides is from 1:4 to 1:1.
6. A process according to claim 1 wherein the solution comprises hexamethylenetetramine and urea.
7. A process according to claim 6 wherein the weight ratio of hexamethylenetetramine to urea is from 1:3 to 3:1.
8. A process according to claim 1 wherein the solution is injected as a dispersion at a number of points, the droplets within the dispersion being within the range of from about 10 to about 10,000 microns Sauter mean diameter.
9. A process according to claim 8 wherein the droplets are greater than about 50 microns.
10. A process according to claim 1 wherein the dispersion is injected into the effluent at a temperature of from 2000°F to 2500°F.
11. A process according to claim 10 wherein the solution comprises at least 80% solvent, based on the weight of the solution.
12. A process according to claim 11 wherein the solution comprises at least 90% solvent, based on the weight of the solution.
13. A process for reducing the concentration of nitrogen oxides in an oxygen-rich effluent from the combustion of a carbonaceous fuel, which process comprises injecting an aqueous solution of urea and hexamethylenetetramine at an effluent temperature effective, and at concentrations of urea and hexamethylenetetramine in the solution and of the solution within the effluent which are effective, to reduce the level of nitrogen oxides in the effluent.
14. A process according to claim 13 wherein the temperature of the effluent is between 1300 F and 1800°F at the point of injection.
15. A process according to claim 14 wherein the solution is injected into the effluent in amounts sufficient to provide a molar ratio of hexamethy-lenetetramine to nitrogen oxides of from 1:6 to 2:1.
16. A process according to claim 14 wherein the ratio of hexamethylenetetramine to nitrogen oxides is from 1:4 to 1:1.
17. A process according to claim 13 wherein the weight ratio of hexamethylenetetramine to urea is from 1:3 to 3:1.
18. A process according to claim 13 wherein the solution is injected as a dispersion at a number of points, the droplets within the dispersion being within the range of from about 10 to about 10,000 microns Sauter mean diameter.
19. A process according to claim 18 wherein the droplets are greater than about 50 microns.
20. A process according to claim 18 wherein the dispersion is injected into the effluent at an effluent temperature of from 2000 F to 2500 F and the solution comprises at least 90% solvent.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US78482785A | 1985-10-04 | 1985-10-04 | |
| US784,827 | 1985-10-04 | ||
| US81153285A | 1985-12-20 | 1985-12-20 | |
| US811,532 | 1985-12-20 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1258159A true CA1258159A (en) | 1989-08-08 |
Family
ID=27120333
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000519894A Expired CA1258159A (en) | 1985-10-04 | 1986-10-06 | Reduction of nitrogen- and carbon-based pollutants |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1258159A (en) |
-
1986
- 1986-10-06 CA CA000519894A patent/CA1258159A/en not_active Expired
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4751065A (en) | Reduction of nitrogen- and carbon-based pollutants | |
| US4719092A (en) | Reduction of nitrogen-based pollutants through the use of urea solutions containing oxygenated hydrocarbon solvents | |
| CA1304914C (en) | Reduction of nitrogen- and carbon-based pollutants through the use of urea solutions | |
| US4927612A (en) | Reduction of nitrogen- and carbon-based pollutants | |
| US4842834A (en) | Process for reducing the concentration of pollutants in an effluent | |
| US3900554A (en) | Method for the reduction of the concentration of no in combustion effluents using ammonia | |
| FI88463C (en) | Multistage procedure for reducing the concentration of pollutants in exhaust gases | |
| CA2063811C (en) | Nitrogen oxides reduction using a urea hydrolysate | |
| US4849192A (en) | Methods for preventing formation of sulfuric acid and related products in combustion effluents | |
| AU6408086A (en) | Reduction of nitrogen- and carbon-based pollutants | |
| US4743436A (en) | Methods for preventing ammonium bisulfate formation during the noncatalytic reduction of nitric oxide | |
| EP0333833A4 (en) | Process for the reduction of nitrogen oxides in an effluent | |
| US5087431A (en) | Catalytic decomposition of cyanuric acid and use of product to reduce nitrogen oxide emissions | |
| CA1258159A (en) | Reduction of nitrogen- and carbon-based pollutants | |
| US4873066A (en) | Low temperature process for the reduction of nitrgen oxides in an effluent | |
| RU2403081C1 (en) | Method of uncatalysed flue gas purification of nitrogen oxides | |
| US4888165A (en) | Process for the reduction of nitrogen oxides in an effluent using a heterocyclic hydrocarbon | |
| JPS63502085A (en) | Reduction of nitrogen-based and carbon-based pollutants | |
| Knol et al. | Reduction of nitrogen oxides by injection of urea in the freeboard of a pilot scale fluidized bed combustor | |
| WO1988007497A1 (en) | Process for the reduction of nitrogen oxides in an effluent using a heterocyclic hydrocarbon |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |