FLUE GAS SCRUBBING AND WASTE HEAT RECOVERY SYSTEM

Abstract: A system and method for the reduction of NOx in a flue gas are disclosed. A P4 in water liquid/liquid emulsion is injected into the flue gas to induce phosphorus-accelerated oxidation of the NO in the flue gas. NO2 and phosphorus oxides are subsequently removed from the flue gas stream at a location sufficiently downstream of the injection site that the oxidation of NO in the flue gas is substantially complete prior to the removal of NO2. This significantly improves the NOx recovery rate of the present system and method over those of the prior art. The system can be retrofitted to the waste gas stream of any stationary combustion source regardless of the fuel burned. The system is advantageously used in connection with a wet scrubber for the removal of NO2 and other water soluble flue gas components. Injection of the emulsion results in the creation of ozone by means of the controlled oxidation of white phosphorus. The ozone reacts with nitrogen oxide (NO), which generally accounts for 90 % of flue gas NOx, to produce nitrogen dioxide (NO2). The reaction products (NO2 and the P4O10) can be removed from the flue gas together with SO2 and particulates in the wet scrubber wherein they are efficiently transferred from the gaseous phase to the buffered scrubbing liquid. In the scrubber, the temperature gradient is preferably set through the dew point, so that it recovers both latent as well as sensible heat energy from the flue gas which energy can be sold to commercial or residential consumers to recover at least a part of the capital costs (purchase and operation) associated with the system.

Description: FLUE GAS SCRUBBING AND WASTE HEAT RECOVERY SYSTEM Field of the Invention The patent relates to flue gas scrubbing systems. More particularly, the invention relates to wet scrubbing towers for the removal of undesirable air pollutants (e.g. particulates, acid rain gases, organic toxins, odours, etc.) from a flue gas exhaust stream produced by mdustriaJVcommercia institutional (ICI) boilers, especially for the removal of nitrogen oxides (NO . Background of the Invention The incentive to develop a cost-effective technology designed to reduce NO x emissions from all stationary combustion sources was provided in 1990 through the enactment by the U.S. Congress of the Clean Air Act Amendments (CAAA). A recent publication (EPA-453/R-94-022) by the Environmental Protection Agency (EPA) clearly indicates that the new NO x reducing timetable is to be applied to ICI boilers (which range in heat input size from 0.4 to 1,500 MBtu/hr), specifically those that emit over 25 tons of NO x per year. Such an annual NO x emission rate can be achieved by an oil burning furnace rated at 5MW or a gas-bυjτjing furnace rated at 10 MW. There are a number of ways in which NO x emissions can be reduced in existing boilers. Modifications in the combustion process are usually the simplest and cheapest. Typical examples are a) to switch to a low N-containing fuel; b) to minimize the use of excess air; c) to lower the combustion temperature by injecting water or steam; d) to decrease the residence time in the flame zone; e) to recirculate and reburn all or part of the flue gases; f) to install an after burner; or g) to retrofit with a new low NO x burner. Other NO x reducing technologies involve some form of treatment of the flue gases. The three main sub-groups are a) the selective catalytic reduction (SCR) or the selective non- catalytic reduction (SNCR) reaction between NO x and ammonia (or urea) to N 2 ; b) the wet scrubbing of the gas stream with an oxidant (to convert NO to the soluble NO 2 or with a NO-specific absorber; or c) the creation of short lived but highly reactive free radicals by means of electrical discharge. Of the retrofit technologies currently popular with the owners of ICI boilers, in terms of NO x reduction, the triple modification involving a change to natural gas, installation of a new low NO x burner, and recirculation of the flue gas for a reburn appears to be the best. However, the selective catalytic reduction installation (SCR) appears to be the only flue gas treatment technology receiving favour, despite its high installation costs. The SCR technology is currently recognized both by the industry and the EPA as the Best Available Technology (BAT) because it is able to reduce NO x emissions from both gas- fired and oil-fired boilers by over 80%. Non-catalytic NH 3 induced NO x reduction (SNCR) replaces SCR when coal is burned or when high-sulfur containing fuels are used. The main advantage to SNCR over SCR is that it is twice as cost effective even though it seldom achieves NO x reductions better than 60%. Its main disadvantage is that it requires high flue gas temperatures, generally above 800°C. However, most ICI boilers are now equipped with economizers which reduce the flue gas temperature to 300°C or less. Currently, considerable research activity involves the application of the electrical discharge to flue gases, e.g. pulsed corona discharge, dielectric barrier discharge, DC glow discharge, E-beam, etc. The intention is to produce short lived free radicals that will react spontaneously with NO x molecules, hopefully to reduce most of them to N 2 without also reducing the CO 2 molecules to CO. High installation costs as well as anticipated high operating and maintenance costs appear to be the main impediments to the commercialization of these technologies. A second problem is that the electrical discharge produces the OH radical (as well as O, H, O 3 radicals) which reacts with CO and N 2 to produce the NO, leading to an increase rather than a decrease in NO x . It is a major disadvantage of all the above-described measures and systems for the reduction of NO x emissions that they require either non-recurring or constant, non- recoverable capital expenditures. Thus, a more economical NO x emissions reduction method and system is desired. The creation of oxygen radicals (O or O 3 ) during the oxidation of yellow phosphorus (P 4 ) has been common knowledge for many years (Thad D. Farr, Phosphorus. Properties of the Element and Some of its Compounds, Tennessee Valley Authority, Wilson Dam, Alabama. Chem. Eng. Report #8, 1950; J.R. Van Wazer, Phosphorus and its Compounds, Interscience, New York 1958). The suggestion to introduce P 4 into the spray of a wet scrubber to oxidize NO to N 2 in the flue gas stream from a boiler was made by S.G. Chang and G.C. Liu (Nature. 343:151-3, 1990). Following bench top experimentation, the authors (S.G. Chang and D.K. Lee, Environmental Prog., 11:66-73, 1992) suggested the economic feasibility of reduced NO x emissions by means of the P 4 - induced conversion of NO to NO 2 in a wet scrubber, especially if costs could be recovered through the marketing of the phosphates captured in the scrubbing liquor. However, the conversion of the disclosed bench top experiments to a full-scale industrial application is not readily achievable without overcoming a number of serious engineering problems. P 4 is highly reactive and must always be kept and handled hermetically, i.e. away from air, which poses engineering problems when a constant stream of relatively large amounts is to be handled. Furthermore, to form a liquid/liquid emulsion between P 4 and water, the temperature of the spray must never fall below 45°. The location of the P 4 NO interaction in the spray of the scrubber as suggested by Chang et al. makes it difficult to ensure total confinement of all undesirable reaction products, i.e. ozone and phosphorus oxides. Furthermore, the P 4 /NO interaction in the liquid/gas interface in a wet scrubber makes it difficult to achieve the optimum P/N molar ratio necessary for cost effectiveness. Other problems with the suggested introduction of P 4 into the liquid spray of a wet scrubber are that the reservoir at the bottom of the wet scrubber cannot contain excess P 4 if the reservoir must be clarified or filtered and that the efficiency of the reaction between the oxygen radicals and the NO molecules is dependent on the residence time of the reactants in the spray tower. Finally, the reactions which take place between P 4 and NO are believed to occur in the vapor phase. Thus, addition of the phosphorus to the scrubbing liquid spray would in many respects be disadvantageous. These problems are now overcome with the method and system in accordance with the invention wherein the P 4 /NO interaction occurs in the flue gas manifold upstream of the wet scrubber and independent of any wet scrubbing steps. This relocation and separation permits i) the maximization of safety with respect to P 4 storage and handling; ii) the optimization of the P 4 /NO interaction in the vapor phase; and iii) the containment of all hazardous bi-products. Furthermore, the method and system in accordance with the invention further provides for economical pollution control by combining wet scrubbing operations with waste heat recovery. Thus, a scrubbing system in accordance with the invention combines ozone-induced oxidation of NO to N0 2 with wet scrubbing and heat recovery. The end result is a superior anti-pollution retrofit system which is capable of removing over 80% of the NO x gases along with about 95% of SO, and 99% of particulates, and which also permits energy recovery and utilization if required. Summarv of the Invention It is an object of the present invention to provide an NO x emissions reduction system and method which overcomes the above technological and economical problems. It is another object of the invention to provide an NO x emissions reduction system and method which is combined with waste heat recovery. It is yet a further object of the invention to provide a total pollution control and waste heat recovery system which permits the continued removal of SO x and particulates and which allows for the recovery of associated capital expenditures. Accordingly, a system in accordance with the invention for reducing the NO x content of a flue gas, includes means for preparing a P 4 in water liquid/liquid emulsion; means for injecting a metered amount of the emulsion as a mist into the flue gas; and means for removal of NO 2 and phosphorus oxides from the flue gas. The means for removal is positioned at a selected location downstream of the means for injecting so that the phosphorus-accelerated oxidation of NO in the flue gas induced by injection of the emulsion is substantially complete prior to the removal of NO 2 The means for removal is preferably a wet scrubbing tower and the means for injecting is preferably an atomizer nozzle positioned in the flue gas stream and at a selected location upstream of the scrubbing tower so that the phosphorus accelerated oxidation of NO in the flue gas induced by injection of the emulsion is substantially complete prior to contact of the flue gas with an aqueous scrubbing liquid in the scrubbing tower. The means for preparing the P 4 in water emulsion preferably includes a heated water bath for melting solid phosphorus stored in a container, the container being completely submersible in the bath to prevent contact of the phosphorus with air, an emulsion tank sealed from ambient, a means for supplying liquefied phosphorus from the container to the emulsion tank, and means for admixing the liquefied phosphorus with water at a preselected ratio and in the emulsion tank. In the preferred embodiment, the system preferably further includes means for washing the liquefied P 4 with a solution of an acid-dichromate to remove trace contaminants. The scrubbing tower preferably includes a sump for collecting spent scrubbing liquid and a scrubbing liquid conditioning circuit for recovering from the scrubbing liquid heat energy taken up from the flue gas. According to another aspect of the invention there is provided a method for reducing the NO x content of a flue gas, which includes the steps of preparing a P 4 in water liquid/liquid emulsion; injecting a selected amount of the emulsion as a mist into the flue gas and at a preselected location; and removing NO 2 from the flue gas at a distance downstream from the predetermined location, the distance being selected such that the phosphorus-accelerated oxidation of NO in the flue gas induced by injecting the emulsion is substantially complete prior to the removal of NO 2 . The flue gas is preferably contacted with an aqueous scrubbing liquid for removal of NO 2 and phosphorus oxides. The emulsion is advantageously prepared by heating solid P 4 in a water bath to prevent contact of the phosphorus with air and admixing the liquefied P 4 with water in a preselected ratio and under a N 2 atmosphere. In yet another aspect, the invention provides a system for reducing the NO x content of a flue gas which includes a wet scrubbing tower having a flue gas treatment chamber, a flue gas entry port for introducing a stream of flue gases into the treatment chamber, a spray assembly for introducing scrubbing liquid into the stream of flue gases in the treatment chamber, a scrubbing liquid sump for collecting used scrubbing liquid, and an exhaust for treated flue gases. The phosphorus emulsion injection system includes means for preparing a P 4 in water liquid/liquid emulsion and means for injecting a metered amount of the emulsion as a mist into the flue gas prior to entry into the scrubbing tower, the means for injecting being positioned at a selected location upstream of the flue gas entry port so that the phosphorus accelerated oxidation of NO in the flue gas is substantially complete prior to contact of the flue gas with the scrubbing liquid in the scrubbing tower. Brief Description of the Drawings Other aspects and advantages of the invention will become apparent from the following detailed exemplary description of the preferred embodiment, reference being made to the drawings, wherein Figure 1 is a schematic diagram of the preferred embodiment of an NO x emissions reduction system in accordance with the invention; Figure 2 is a schematic block diagram, illustrating the interaction of the components shown in Figure 1 plus all accessory equipment related to monitoring and control of the key variables to maximize efficiency, safety and containment; Figure 3 is an enlargement of Section A in Figure 1; and Figure 4 is an enlargement of Section B in Figure 1. Detailed Description of the Preferred Embodiment In the preferred embodiment, illustrated schematically in Figure 1, the system in accordance with the invention includes a phosphorus handling and injection system 10 and a wet scrubbing and waste heat recovery system 50. The phosphorus handling and injecting system consists of phosphorus storage and emulsifying stations A and B and a phosphorus emulsion injection arrangement C which will be described in more detail below with reference to Figures 3 and 4 respectively. The wet scrubbing and waste heat recovery system 50 includes a wet scrubbing tower 52 and a scrubbing liquid conditioning and heat recovery circuit 54. In the preferred process in accordance with the invention which is illustrated by way of a flow diagram in Figure 2, a P 4 in water liquid/liquid emulsion is injected into a flue gas stream by way of the injection arrangement C. Injection takes place upstream of the wet scrubbing tower 52 and the exact location is selected such that the phosphorus- accelerated oxidation of NO in the flue gas is substantially complete prior to contact of the flue gas with the scrubbing liquid. The distance of the injection point from the scrubbing tower 52 can be calculated from the speed of the flue gas stream at the injection point and the reaction time required for oxidation of the respective amount of NO present in the flue gas, which time can be determined from data available in the literature. The scrubbing tower 52 removes water soluble gases (including acid gases and greenhouse gases) and particulates from the flue gas and functions also as direct contact gas-to-liquid heat exchanger. The primary scrubbing liquid is preferably water which is chemically treated and pH balanced and is introduced at the top of the tower 52 through spray nozzles 58. The scrubbing liquid then passes downward inside the tower 52, through a structured internal bed 60 (Glitsch, Canada) which provides a large surface for efficient mass and heat transfer. The scrubbing liquid collects in a sump 62 at the base of the tower 52. Hot flue gas is fed into the tower 52 above the sump through a flue gas inlet port 72 and flows upward counter to the downward flow of the scrubbing liquid. The temperature of the liquid is selected to permit water vapour condensation, hence the transfer of both latent and sensible heat from the flue gas to the scrubbing liquid. The heated scrubbing liquid is pumped from the sump 62 to a heat exchanger 64 (Nixon- Vicarb, Newmarket, Ontario). In transferring the liquid through the heat exchanger, the scrubbing liquid is cooled before it is recirculated back to the spray nozzles 58 at the top of the tower 52 while a cooling liquid also circulating through the heat exchanger 64 is heated to the same extent the scrubbing liquid is cooled. The heated cooling liquid can then be employed for the heating of the boiler plant or other buildings, for the preparation of hot utility water, or the like. The energy stored in the cooling liquid which is not used up in the boiler plant and in the scrubbing process, for example for the heating of the phosphorus as will be described in detail below, can be sold to commercial or residential consumers. This allows recovery over time of all or at least a substantial part of the operation and purchase costs of the scrubbing system. Thus, the heat recovery aspect of a system in accordance with the invention provides the system with a significant economical advantage over conventional flue gas scrubbing and especially NO x reduction systems which do not allow for amortization of the purchase, installation and operating costs through the sale of recovered energy. A variable speed exhaust fan 68 located at the exhaust 70 of the tower 52 is automatically controlled to vary the draft through the tower, thereby controlling static pressure and maintaining the required boiler operation parameters. The scrubbing tower 52 is usually installed in close proximity to an existing smoke stack so that the flue gases can be most conveniently and economically redirected from the bottom of the stack (not shown) to the inlet port 72 of the tower. The scrubbing tower 52 is dimensioned to receive the full volume of the exhaust stream, to extract the maximal amounts of sensible and latent heat as the gases are cooled, preferably to 38°C, and to capture particulates, SO 2 and NO 2 . The efficiency of these heat and mass transfers are dependent on the size of the gas/liquid surface interface in the scrubbing tower, the opposing countercurrent temperature gradients (decreasing upward for the gases, increasing downward for the liquid), the selection and maintenance of the liquid/gas ratio, the selection and maintenance of the final exhaust temperature, the selection of the buffer used for the control of the scrubbing liquid pH and the scrubbing liquid temperature. Optimization of the pollution control and heat recovery process is achieved by a monitoring system which includes pressure and temperature sensors 74, 76, a pH sensor 78, (Base Controls, Newmarket, Ontario), the exhaust fan 68, a circulating pump 81 (Pump Tech Inc., Mississauga, Ontario) in the scrubbing liquid circuit 54, a central controller 82 and a buffer liquid metering pump 84. The sensors 74, 76 and 78 are electrically connected through associated conductors 74a, 76a and 78a to the controller 82 for the transfer of signals representing the size of the variable respectively detected. The controller 82 in turn is electrically connected to the exhaust fan 66, the circulating pump 81 and the metering pump 84 through associated conductors 66a, 81a and 84a for control of the flue gas flow, the throughput of the scrubber liquid conditioning and heat recovery circuit 54 and the temperature and pH of the scrubbing liquid ejected from the spray nozzles 58 respectively according to parameters stored in the controller. The throughput of circuit 54 can also be controlled by an electrically controlled modulating valve 75 (Base Controls, Nepean, Ontario) connected to the controller through conductor 75a. Multiple heat exchangers 64 (not shown) can be provided in combination with a scrubbing liquid distribution arrangement (not illustrated) so that a sufficiently large heatsink is always available for the transfer of energy stored in the scrubbing liquid. Furthermore, to optimize the particulate and dissolved compound removal from the flue gas, the temperature and amount of the scrubbing liquid sprayed into the flue gas is controlled such that the final exhaust temperature is below the dew point (less than 50°C). This allows for the capturing of both the sensible and the latent heat from the flue gas. The sump 62 of the scrubbing tower receives the sprayed liquid plus the water vapour condensed from the flue gas. The liquid in the sump 62 also contains all the entrapped particulates and the dissolved gases, which were converted to acids and then neutralized by the buffer in the scrubbing liquid. The sump has a make-up water supply 86 and is preferably equipped with a conventional automatic ball float valve 88 for liquid level control. However, due to condensation of the water vapour originally in the flue gas stream, there is usually an excess of water in the sump relative to the requirements for scrubbing liquid recirculation. Thus, in general, some liquid is directed either continuously or intermittently to drainage through drainage valves 90. This can be done either before or after clarification and/or filtration of the scrubbing liquid in filter 92, in this embodiment (EMCO Process Equipment, Mississauga, Ontario). An alkaline buffer liquid for the control of scrubbing liquid pH is supplied to the scrubbing liquid circuit 54 from a buffer liquid storage tank 98 through metering pump 84 which is electrically connected to central controller 82 through conductor 84a. The storage tank 98 is provided with a mixing arrangement 100 for the constant or intermittent mixing of the buffer liquid, depending on the buffer liquid respectively used. The preferred buffer compounds are Na^ CO 3 and/or NaHCO 3 , which are stored in an aqueous solution in the buffer liquid storage tank. Make-up water can be added to the buffer liquid storage tank 98 through a make-up water line 94 and make-up water valve 96. A scrubbing liquid bypass circuit 102 is provided in the scrubbing liquid circuit 54 which allows for maintenance and repair of the filter 92 as well as control of the scrubbing liquid throughput thereof. Wet scrubbing towers of this principle construction and function have been used to clean the exhaust of various power plants (Tilsonburg District Memorial Hospital, Tilsonburg, ON; Ottawa Civic Hospital, Ottawa, ON; Gatineau Sewage Treatment Plant, Gatineau, PQ) rated from 20 to 60 MBtu hr. All function to recover and utilize waste heat. In terms of antipoUution performance, these scrubbing systems in general remove over 95% of particulates and substantially all of the SO x gases, but only up to 50% of the NO x gases. This performance is now improved by the addition of the phosphorus handling and injection system in accordance with the invention. The NO x gases consist of N 2 O, NO, and NO 2 . The capture of each by a scrubber depends on its aqueous solubility and on the ease by which it can be transformed (through chemical interactions) in the aqueous phase. NO is the least soluble and NO 2 is the most soluble of the three NO x gases. N 2 O converts spontaneously to N 2 early on when the manifold temperatures are 300°C or greater, hence N 2 O is almost non-existent at the scrubber level. At 300° C, NO accounts for about 90% of the NO x . However, at the pre-scrubber level, it could be in the 50 - 60% range because of slow but spontaneous oxidation of NO to NO 2 . 2NO + O 2 2NO 2 i. The degree of conversion depends on the O 2 content, the free O ' radical content, the CO content, the temperature, and the length of the manifold between the boiler and the scrubbing tower 52. Once in solution, NO 2 hydrolyzes with relative ease to form nitrite and nitrate ions as shown by reaction ii, 2NO 2 + H 2 O NO 2 - + NO 3 - + 2H + ii. especially in the presence of a buffer designed to remove H + ions. The little NO that does dissolve in the scrubbing liquor can react with NO 2 to produce nitrites and nitrates as follows: NO + 3NO 2 N 2 O 3 + N 2 O 4 iii. N 2 O 3 + H 2 O 2NO 2 - + 2H + N 2 O 4 + H 2 O NO 2 - + NO 3 - + 2H + Theoretical calculations indicate that up to 90% of all NO x could be recovered by a wet scrubber if all of it were in the NO 2 form when it entered the tower. Chang & Lee (1992) have already demonstrated that the oxidation of NO to NO 2 inside a scrubber is accelerated when P 4 is permitted to oxidize in the same location. The following reaction chain is believed to occur: P 4 + O 2 P 4 O + o- iv.a P 4 O n + O 2 P^, + o- iv.b 2NO + (O + O 3 ) 2NO 2 + O 2 iv.c where n is a number from 1 to 9. These reactions are believed to occur primarily in the vapour phase. Therefore, adding P 4 to the scrubbing liquid spray in the tower as suggested by Chang et al is disadvantageous. To maximize the effectiveness of these reactions, according to the present invention the reaction site is now relocated into the pre-scrubber manifold where the temperatures present ensure relatively high P 4 vapour pressures. In the temperature range from melting (44° C) to boiling (280° C), the partial vapour pressure of P 4 increases exponentially from 0.000233 to 1.0 atmosphere. Pre-scrubber manifold temperatures usually range from 480 to 180° C. At temperatures higher than 280°C, tetrahedral P 4 transforms into the less reactive red (amorphous) phosphorus. Therefore, the optimum temperature window for the chain reactions (iv) is between 180° C and 280° C. The stations of the phosphorus handling and injection system 10 designed for the storage, liquefaction, dilution, emulsification, delivery to the manifold, and atomization of the P 4 /water liquid/liquid emulsion are shown schematically as apparatus units A, B, and C in Figure 1. Enlargements of units A and B are shown in Figures 3 and 4 respectively. White phosphorus is commercially available (Brander's, Baltimore, MD) in 250 kg sealed drums 12 (see Figure 3) containing 200 kg of solid phosphorus 14 layered with about 20 kg of water 16 (the density of solid P 4 is 1.828 g/cc). Before removing the generally threaded filler caps of the drum 12 to attach the plumbing connecting units A and B, it is preferred for safety reasons that the drum be totally immersed in a water bath 18. Besides ensuring no air contact with P 4 (when making connections), the water bath 18 also serves to warm the P 4 above its melting point (44.TC). For this purpose, the water bath 18 is maintained at a constant temperature of 50-55°C. Hot water at a temperature of 55°C is supplied through an input valve 19 on one side and at the bottom of the water bath tank 22 and removed through an output valve 20 located opposite the input valve and at the top of the water bath tank. The water bath input and output connections are preferably welded to the tank 22 at such an angle that circulation of the water bath 18 is achieved. A pump (not shown) ensures adequate supply of heated water. The water bath 18 can be made large enough to hold several drums 12, the number will depend on the rate at which P 4 is utilized. The energy to heat the water bath 18 is obtained through a heat exchanger fed either by steam or incorporated into the heat recovery circuit 54 (see Figure 1). The liquefied P 4 is preferably washed with acid-dichromate solution to remove impurities (As & oil) if required which solution is supplied through a washing solution pipe 24 and four-way valve 26. Liquid P 4 is transferred at a pre-determined rate from the drum 12 to the emulsifying station B through transfer pipe 27, four- way valve 26 and riser pipe 29 by displacing the liquid P 4 with water forced into the drum by way of a positive displacement metering pump 28 (Pump Tech Inc., Mississauga, Ontario) and three-way valve 30 to ensure the delivery of a predetermined constant flow to the emulsifying station. Hot washing water can be supplied to the drum 12, the riser piper 29, the transfer pipe 27 and the three-way and four-way valves 30, 26 through washing water supply pipes 32 for the flushing out of solidified P 4 from the plumbing. With duplication of the plumbing complex, the switch to a second tank 12 can be done quickly and efficiently. An enlargement of the air-tight emulsifying station B is shown in Figure 4. Liquid P 4 and water are pumped into emulsion tank 34 at predetermined constant flow rates designed to produce and to maintain a constant P 4 /water dilution ratio (i.e. about 1:100 for a NO x emission rate of 300 ppm) and are emulsified therein by way of a conventional mixer 38. The unheated transfer pipe 27 (see Figure 3) between the water bath 18 (> 50° C) and the emulsion tank 34 (> 70° C) is insulated to prevent cooling to below the solidification temperature of P 4 (45° C). Transfer pipe 27 enters into the emulsion tank so that the P 4 outflow end 36 of the transfer pipe is directly above the stiffing paddle 37 of the mixer 38 to prevent settling of the heavy immiscible P 4 and ensure immediate emulsification of the two liquids. The temperature of the emulsion 39 is preferably maintained at 70°C by way of a conventional immersion heater 35. The P 4 /water emulsion 39 is conveyed at a preset rate by way of a conventional metering pump 40 (Pump Tech Inc., Mississauga, Ontario) to an atomizer nozzle 41 located in the flue gas stream in the intake manifold 51 of the wet scrubbing tower 52 (see Figure 1). The emulsion is instantly dispersed by the nozzle 41 into microdroplets (< 60 μm diam.) by way of compressed air (or steam) supplied to the nozzle 41, which microdroplets are ejected into the flue gas stream. The compressed air is produced by a conventional air compressor (not shown) and according to specifications of the nozzle manufacturer. Selection of the atomizer nozzle 41 will depend on the geometry (angle distance, width, sectional profile) of the spray desired. Multiple orifice nozzles are commercially available (Turbo Sonic Inc., Waterloo, Ontario) which produce any spray profile (circular, square, rectangular) and with any set of dimensions so that the profile of the spray can be precisely tailored to the dimensions of any flue gas manifold. The variables to be considered in selecting the atomizer nozzle are: a) the desired flow rate and temperature of the P4/water emulsion 39; b) the flow rate and temperature of the flue gas stream in the manifold 51 as determined by way of flow and temperature sensors 44, 45; c) the pressure of the compressed air (or steam) supplied to the nozzle 41; and d) the number, size, shape, and grouping of the orifices in the nozzle. The pump rate of metering pump 40 immediately upstream thereof is controlled by way of the central controller 82 through conductor 40a in order to maintain and match the rate of liquid entry to the rate of liquid exit in the emulsifying tank 34. The development of a negative pressure in the emulsifying tank 34 must be especially avoided since it encourages air entry during equipment failure (i.e. leakage of seals in pumps and valves). As a safeguard, that part of the tank above the emulsion 39 is kept filled with nitrogen gas (N 2 ) at a slightly positive pressure. A conventional modulating valve 45 is provided between the emulsion tank 34 and a N 2 tank 43 and is programmed to open when the pressure falls to zero and to close when a small positive pressure develops. From the above chain reactions (iv), it is apparent that a tetrahedral P 4 molecule has the potential to produce 10 oxygen radicals which in turn have the potential to oxidize 10 molecules of NO. Thus, the best P/N molar ratio one can expect is 0.4. This theoretical optimum ratio can be achieved when the half-life (t, /2 ) of the O radical (either O " or O 3 ) is such that it can survive long enough to collide with an NO molecule. The A values listed below in Table 2 illustrate how dependent ozone survival is on temperature and ozone concentration (Kirk Othmer, "Encyclopedia of Chemical Technology", John Wiley & Sons, 2nd ed., Vol. 14; 410 - 416, 1967). TABLE 2 UNCATALYZED THERMAL DECOMPOSITION OF OZONE IN O 3 + O 2 MIXTURES Initial Ozone Concentration O 3 /O 2 Wt.% 2 1 0.5 0.1 Temp. Half-Life (t, /2 ) of Ozone ° °CC K K sec 150 1.40 105 210 420 2,100 200 0.030 2.25 4.5 9.0 45 250 0.00133 0.1 0.20 0.40 2 (t, /2 ) = 150K/(Wt%) where K is a complex function of temperature and of the decomposing constant (k) of O 3 to O 2 Example The system in accordance with the invention can be used with a boiler rated at 100 MBtu/hr emitting a flue gas stream of 21,000 cu. ft./MBtu at a temperature of 200 ° C. which contains 4% 0 2 and 300 ppm of NO x (90% as NO). From this information, one obtains a total volume flow of 583 cu. ft/sec, containing NO at 0.16 cu.ft./sec (F.D. Friedrich & A.C.S. Hayden, "A Combustion Handbook", Vol. 2, Mines Branch Monograph 879, Information Canada, Ottawa, 1973). According to reaction iv.c shown above, the ozone content (volume flow) created in the flue gas stream must be at least equal to the NO content (volume flow). Using a conversion factor of 0.73 moles/cu.ft at 200° C, one calculates the required ozone (and NO) content as 0.115 moles/sec. Using a P/N molar ratio of 0.4, one calculates that P must be ejected into the flue gas stream at a rate of 0.05 moles/sec. The phosphorus emulsion 39 is ejected from nozzle 41 (1% P 4 /water emulsion) and dispersed by compressed air producing a flow of 20 cu.ft min. at 60 psig (TurboSonic Inc. instructions). The ejected vaporized volume is then about 12 cu.ft/sec, producing about a 2% increase in the flue gas stream. Water vapour will account for most of the newly created volume flow. After the P 4 /water emulsion is injected, the O 2 content of the flue gas (volume flow) will be (0.04)(583) cu.ft sec. Since the ozone content is 0.16 cu.ft/sec, the O 3 /O 2 ratio (w/w) is calculated to be about 1.0%. At this O 3 /O 2 ratio, the ozone half-life ( /2 ) at 200°C should be 4.5 seconds according to Table 2. If the velocity of flow is 30 ft/sec in the manifold 51 and 15 ft/sec in the scrubbing tower 52 (based on geometry) and if the P 4 /water emulsion 39 is ejected at about 20 ft upstream of the inlet port 72 and if the 'scrubbing' length of the tower 52 is about 25, then the total 'residence time', during which the P 4 /O 2 /O 3 /NO interactions (iv) are contained, will be 2.3 seconds (about 0.7 sec in the manifold 51 and about 1.6 sec in the tower 52) . According to the pilot-scale experiments by Chang & Lee (1992), up to 90% of NO x was absorbed as NO 2 after a contact time between NO and P 4 (only in the scrubber chamber) of about 1.2 sec. No doubt, the rate limitations in the chain reactions (iv.a-c) in their experiments are to be found in a relatively low liquid/gas interphase surface area and in the relatively low P 4 partial pressure achieved at 80°C . In the preferred system according to the invention, microdroplets are formed which helps to increase the liquid/gas interphase surface area. Also, since the temperature at the spray site will be about 200° C, one can expect to achieve a much higher P 4 partial pressure for interaction with O 2 and the creation of ozone (iv.a, iv.b). Therefore, the chain reactions (iv) should proceed to completion in a much shorter time than was observed by Chang & Lee (1992) . In the preferred system of the invention, the P 4 to NO 2 reactions will be complete within about 1 second, thus before the flue gas comes into contact with the scrubbing liquid. During this time period, one can expect some of the O 3 to decompose, according to the simple exponential decay equation (O 3 )/(O 3 ) 0 = exp(-kt). Using this equation and the 4.5 sec half-life given in Table 2 (at 200° C), one calculates that only about 14% of the O 3 will decay in the first second before it can interact with NO. Therefore, a large portion of the NO in the flue gas will be converted to NO 2 prior to entry of the flue gas into the scrubbing tower 52, i.e., before it comes into contact with the buffer liquid cascading down the packing of the tower. When the scrubbing tower 52 is sized to recover up to 90% of the flue gas waste heat it has enough scrubbing liquid throughput to capture the more soluble gases (NO 2 , SO 2 ) and organics, especially when the fuel is natural gas. The concomitant absorption by the scrubbing tower 52 of P 4 O 10 , its hydrolysis to phosphoric acid, and its neutralization by the circulating buffer in the scrubbing liquid is not expected to require any significant deviations from standard operating and design principles of conventional wet scrubbers. The best defence against excess emission of O 3 and P O 10 to the atmosphere is a careful matching of P 4 ejection to NO content. Ozone is continuously monitored by an ozone sensor 46 located at the exhaust 70 of the scrubbing tower 52. NO, O 2 , CO and NO 2 is continuously monitored proximal to and upstream of the P 4 ejection site with a gas sensor 47. The signals from these sensors are sent to the central controller 82 through electrical conductors 46a and 47a. The controller 82 in turn operates the modulating devices (metering pump 40, air compressor) in the P 4 injection system according to preselected P 4 to NO ratios stored in the controller. The ozone content at the exhaust 70 is a good indicator of excess P 4 , hence also excess P O 10 , because the O 3 survival rate increases dramatically as its concentration decreases and as the temperature decreases (Table 2). The P 4 O 10 content at the exhaust 70 will be lower than the excess P 4 O 10 as determined from stoichiometry (iv), since the solubility of P 4 O ]0 is better than the solubility of 0 3 . Thus, the absorption rate of P 4 O 10 in the scrubbing liquid relative to O 3 will be higher. Reaction v.a shows the hydrolyzation of the last (others are similar) phosphorus oxide once it is absorbed into the liquid phase. P 4 O 10 + 6H 2 0 4H 3 P0 4 v.a Since the scrubbing liquid will contain an alkali buffer, much of the H 3 PO 4 will be SUBSTITUTE SHEET (RULE 26, in the H 2 PO 4 - form. Preselected amounts of lime stored in a chemical tank (not shown) will be added at 48 to the scrubbing liquid in the clarifier 92 to selectively precapitate H 2 PO 4 - as the very insoluble calcium phosphate (v.b) 2H 2 PO 4 - + 3Ca(OH) 2 Ca 3 (PO 4 ) 2 + 4H 2 O + 2OH- v.b Calcium phosphate can be sold, for example, to the fertilizer manufacturing industry which will allow further recovery of operating costs. Changes and modifications in the specifically described embodiments can be carried out without departing from the scope of the invention which is intended to be limited only by the scope of the appended claims.

Claims: THE EMBODIMENTS OF THE INVENTION IN WHICH AN EXCLUSIVE PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS: A system for reducing the NO x content of a flue gas stream, comprising means for preparing a P 4 in water liquid/liquid emulsion; means for injecting a metered amount of the emulsion as a mist into the flue gas stream; and means for removal of NO 2 and phosphorus oxides from the flue gas stream, the means for removal being positioned at a selected location downstream of the means for injecting so that the phosphorus-accelerated oxidation of NO in the flue gas stream induced by injection of the emulsion is substantially complete prior to the removal of NO 2 2. A system as defined in claim 1, wherein the means for removal is a wet scrubbing tower and the means for injecting is an atomization nozzle positioned in the flue gas stream at a selected location upstream of the scrubbing tower so that the phosphorus accelerated oxidation of NO in the flue gas stream induced by injection of the emulsion is substantially complete prior to contact of the flue gas stream with an aqueous scrubbing liquid in the scrubbing tower. 3. A system as defined in claim 1, wherein the means for preparing the P 4 in water emulsion includes a heated water bath for melting solid phosphorus stored in a container, the container being completely submersible in the bath to prevent contact of the phosphorus with air, an emulsion tank sealed from ambient, means for supplying liquefied phosphorus from the container to the emulsion tank, and means for admixing the liquefied phosphorus with water at a preselected ratio and in the emulsion tank. 4. A system as defined in claim 3, wherein the emulsion tank includes an immersion heater for maintaining the emulsion at a selected temperature above the melting point of P 4 and means for filling all space in the emulsion tank not occupied by the emulsion with gaseous N 2 at a selected positive pressure. 5. A system as defined in claim 4, further including means for washing the liquefied P 4 with a solution of an acid-dichromate. 6. A system as defined in claim 4, wherein the means for supplying is an insulated transfer pipe, the emulsion is maintained at a temperature of about 70° C and the selected ratio of P 4 to water is 1:100. 7. A system as defined in claim 2, wherein the scrubbing tower includes a sump for collecting spent scrubbing liquid and a scrubbing liquid conditioning circuit for recovering from the scrubbing liquid heat energy taken up from the flue gas. 8. A system as defined in claim 7, wherein the scrubbing liquid is recirculated to the scrubbing tower after recovery of the heat energy. 9. A method for reducing the NO x content of a flue gas, comprising the steps of preparing a P 4 in water liquid/liquid emulsion; injecting a selected amount of the emulsion as a mist into the flue gas and at a preselected location ; and removing NO 2 from the flue gas at a distance downstream from the predetermined location, the distance being selected such that the phosphorus-accelerated oxidation of NO in the flue gas induced by injecting the emulsion is substantially complete prior to the removal of NO 2 . 10. A method as defined in claim 9, wherein the flue gas is contacted with an aqueous scrubbing liquid for removal of NO, and phosphorus oxides. 11. A method as defined in claim 10, wherein the emulsion is prepared by heating solid P 4 in a water bath to prevent contact of the phosphorus with air and admixing the liquefied P 4 with water in a preselected ratio and under a N, atmosphere. 12. A method as defined in claim 9, wherein the emulsion is injected into the flue gas by atomizing the emulsion with compressed air or steam. 13. A system for reducing the NO x content of a flue gas, comprising a wet scrubbing tower having a flue gas treatment chamber, a flue gas entry port for introducing a stream of the flue gas into the treatment chamber, a spray assembly for introducing an aqueous scrubbing liquid into the stream of flue gas in the treatment chamber, a scrubbing liquid sump for collecting used scrubbing liquid and a flue gas exhaust for treated flue gases; and a phosphorus emulsion injection arrangement including means for preparing a P 4 in water liquid/liquid emulsion, and means for injecting a metered amount of the emulsion as a mist into the flue gas prior to entry into the scrubbing tower, the means for injecting being positioned at a selected location upstream of the flue gas entry port so that phosphorus accelerated oxidation of NO x in the flue gas induced by injection of the emulsion is substantially complete prior to contact of the flue gas with the scrubbing liquid. 14. A system as defined in claim 13, wherein the means for preparing the P 4 in water emulsion includes a heated water bath for melting solid phosphorus stored in a container, the container being completely submersible in the bath to prevent contact of the phosphorus with air, an emulsion tank sealed from ambient, means for supplying liquefied phosphorus from the container to the emulsion tank, and means for admixing the liquefied phosphorus with water at a preselected ratio and in the emulsion tank. 15. A system as defined in claim 14, wherein the emulsion tank includes an immersion heater for maintaining the emulsion at a selected temperature above the melting point of P 4 and means for filling all space in the emulsion tank not occupied by the emulsion with gaseous N at a selected positive pressure. 16. A system as defined in claim 15, further including means for washing the liquefied P 4 with a solution of an acid-dichromate. 17. A system as defined in claim 15, wherein the means for supplying is an insulated transfer pipe, the emulsion is maintained at a temperature of about 70° C and the selected ratio of P 4 to water is 1 :100. 18. A system as defined in claim 13, wherein the scrubbing tower includes a sump for collecting spent scrubbing liquid and a scrubbing liquid conditioning circuit for recovering from the scrubbing liquid heat energy taken up from the flue gas. 19. A system as defined in claim 18, wherein the scrubbing liquid is recirculated to the scrubbing tower after recovery of the heat energy. 20. A system as defined in claim 13, wherein the means for injecting is at least one atomizer nozzle for atomizing the emulsion with compressed air or steam.

Inventors: HINKE JOSEPH DR, HINKE THOMAS V, TRIEBE ROB, HINKE, JOSEPH, HINKE, THOMAS, V., TRIEBE, ROB
Applicants: THERMAL ENERGY INT INC, THERMAL ENERGY INTERNATIONAL INC.
Application year: 1996
Main classification: B01D53
IPC codes: B01D53