Method of regenerating a deNO.SUB.x .catalyst

Abstract

A method for regenerating a deNO.sub.x catalyst includes contacting the catalyst with steam at a temperature in the range of from 250 to 390° C. The method also includes reducing the amount of nitrogen oxide components in a process gas stream that includes a) contacting the process gas with a deNO.sub.x catalyst which results in the conversion of nitrogen oxide components as well as a decline in the NO.sub.x conversion over the deNO.sub.x catalyst; and b) regenerating the deNO.sub.x catalyst to improve the NO.sub.x conversion by contacting the deNO.sub.x catalyst with steam at a temperature in the range of from 250 to 390° C.

Claims

1. A method for regenerating a deNO.sub.x, catalyst comprising contacting the catalyst with a stream comprising process gas, steam, and optionally air, at a temperature in the range of from 250 to 390° C., wherein the steam is present in an amount of 10 to 50 vol. % of the total stream.

2. The method of claim 1, wherein the catalyst is contacted with steam at a temperature in the range of from 290 to 350° C.

3. The method of claim 1, wherein the catalyst is contacted with steam at a temperature in the range of from 310 to 350° C.

4. The method of claim 1, wherein the regeneration is carried out for a time period of from 5 to 168 hours.

5. The method of claim 1, wherein the regeneration is carried out for a time period of from 24 to 48 hours.

6. The method of claim 1, wherein the deNO.sub.x catalyst comprises one or several of the following elements: titanium, tungsten, molybdenum, vanadium or other compounds known to be suitable for the conversion of nitrogen oxides to nitrogen and water.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) Figure depicts the results of Example 3.

DETAILED DESCRIPTION

(2) The invention provides an improved method for regenerating deNO.sub.X catalyst, especially deNO.sub.X catalyst showing a reduced NO.sub.X conversion caused by sulfur-containing compounds in the process gas. This provides an improved NO.sub.X reduction process with extended catalyst life and reduced downtime of the deNO.sub.X unit(s).

(3) The deNO.sub.X catalyst may be any deNO.sub.X catalyst known in the art for reducing the concentration of nitrogen oxides in a process gas stream. The deNO.sub.X catalyst may contain titanium, tungsten, molybdenum, vanadium or other compounds known to be suitable for the conversion of nitrogen oxides to nitrogen and water. The catalyst may be in any suitable shape or it may be a wash coat on a substrate, for example the catalyst may be an extruded honeycomb, a wash coated metal plate, a wash coated corrugated plate or on a foam substrate. In another embodiment, the catalyst may be in the form of pellets.

(4) The process gas may be produced in heaters, furnaces, direct fired boilers, or by any other combustion process or other process. The process gas may contain any number of products, including carbon monoxide, carbon dioxide, nitrogen oxides, sulfur compounds, and other contaminants present in the feed streams that are combusted or otherwise processed in addition to particulates which may contain phosphorous, heavy metals, alkali metals and alkaline earth metals. The sulfur compounds may be sulfur oxides, for example sulfur dioxide and sulfur trioxide. The sulfur compounds are typically generated as a result of sulfur being present in the feed streams, which could include fuel oil or other hydrocarbon streams, coal or waste such as municipal waste, industrial waste and hospital waste.

(5) The process gas may be treated for the removal of any or all of these products and contaminants, and the treating is typically determined by the relevant environmental regulations. The process gas is passed through one or more treatment zones that may comprise one or more catalysts. For example, the process gas may be passed through electrostatic precipitators or fabric filters to remove a portion of the particulates and acid gas removal systems to remove a portion of the acid gases including sulfur dioxide and sulfur trioxide.

(6) The process gas is contacted with a deNO.sub.X catalyst, typically in the presence of ammonia, to convert the nitrogen oxides to nitrogen and water. The catalyst may present in a catalyst module, for example a honeycomb or plate type catalyst module as well as a lateral flow reactor, radial flow reactor or axial flow reactor. The deNO.sub.X reaction may be conducted at a temperature of from 140 to 300° C.

(7) Over time, the NO.sub.X conversion over the deNO.sub.X catalyst is reduced. This may be a result of the active sites being physically covered, i.e., with particulates and/or the active sites chemically reacting with other process gas components in a way that they are no longer active for nitrogen oxide conversion. Dust and/or other particulates from the process gas may be physically deposited on the catalyst surfaces, and over time more and more sites will be obscured. Ammonium sulfate, ammonium bisulfate and other ammonium salts, such as ammonium chloride and ammonium nitrate, may form through the reaction of injected ammonia with components in the process gas. These ammonium salts may condense or otherwise deposit on the catalyst increasing the sulfur concentration on the catalyst.

(8) In addition, sulfur compounds, such as sulfur oxides may deposit on the catalyst, to increase the sulfur concentration on the catalyst and result in a reduction in NO.sub.X conversion. As the process gas passes across the deNO.sub.X catalyst, the concentration of sulfur deposited on the catalyst increases. The sulfur content may increase to a concentration of more than 0.2 wt % on the catalyst, calculated as elemental sulfur as a percentage of the total weight of the catalyst. The amount of sulfur on the catalyst may increase even higher to 1.0 wt % or 2 wt % or even higher concentrations. The NO.sub.X conversion over the catalyst will be reduced as a result of this concentration of sulfur on the catalyst.

(9) In order to regenerate the deNO.sub.X catalyst, it is contacted with steam under regeneration conditions. These regeneration conditions include desired temperature, flow rates, steam content and regeneration time. The steam may be produced in a high pressure boiler nearby, be part of the steam utility system or be produced in the same processes that produce the process gas to be treated. This last embodiment is especially useful because the steam is produced at almost the same place as where it needs to be used for the regeneration.

(10) The regeneration may be carried out at the same temperature that the process gas contacts the catalyst or the steam may provide sufficient heat to heat the catalyst to a higher temperature during the regeneration. Alternatively, heat may be provided by heaters or other heat sources. The regeneration temperature is preferably in the range of from 250 to 390° C., more preferably in the range of from 250 to 370° C., and even more preferably in the range of from 290 to 350° C. In another embodiment, the temperature may be in the range of from 310 to 350° C.

(11) The pressure in the regeneration step is typically at or near ambient pressure.

(12) During the regeneration step, in addition to the steam, the catalyst may be contacted with a flow of air.

(13) In another embodiment, the catalyst may continue to be contacted with the process gas during the regeneration step. In this embodiment, the amount of steam that is needed will depend on the amount of steam that may already be present in the process gas. If the process gas continues to pass through the catalyst, then the underlying process does not have to be stopped during the regeneration step.

(14) The flow of process gas may be reduced during the regeneration step. The flow may be reduced to 50% of its normal flow, preferably 25% of its normal flow, more preferably to 10% of its normal flow and most preferably to 5% of its normal flow. The flow may be reduced to 2 to 5% of its normal flow. In one embodiment, the flow of the process gas may be stopped. The flow of the process gas may be stopped when steam and/or air are fed during the regeneration step.

(15) The catalyst may be contacted with an amount of steam of from 10 to 50 vol. % of the total gas stream during the regeneration step. The total gas stream may comprise from 15 to 40 vol. % of steam.

(16) During the regeneration the ammonia that is typically contacted with the catalyst and process gas during deNO.sub.X operation may be stopped or it may continue to flow at a reduced flow rate. In a preferred embodiment, the ammonia flow is stopped during the regeneration.

(17) The steam and optionally air flow through the catalyst during the regeneration step can unlock ammonium salts which are then decomposed and removed from the catalyst. This improves the performance of the catalyst and helps to return the NO.sub.X conversion rate to at least 50% of the NO.sub.X conversion rate of fresh catalyst.

(18) The regeneration step also removes sulfur compounds present on the catalyst. The regeneration can reduce the level of sulfur on the catalyst to less than 1.3 wt %, preferably less than 0.9 wt % and more preferably to less than 0.6 wt % of sulfur on the catalyst.

(19) The regeneration may be carried out for a sufficient time period to restore the catalyst to at least 50% of its initial NO.sub.X conversion rate, preferably at least 80% of its original NO.sub.X conversion rate, more preferably at least 90% of its initial NO.sub.X conversion rate, and even more preferably at least 95% of its initial NO.sub.X conversion rate. The regeneration may be carried out for a time period of from 5 to 168 hours, preferably from 12 to 72 hours, and more preferably from 24 to 48 hours.

EXAMPLES

(20) In the examples, deNO.sub.X catalyst that was used in two different industrial locations to treat process gas was tested and then regenerated under different conditions to determine the effect on NO.sub.X conversion of the catalyst.

Example 1

(21) In this example, an industrial deNO.sub.X catalyst was regenerated after it was used to treat process gas. The catalyst was a vanadium-containing deNO.sub.X catalyst in the form of trilobes. The catalyst was regenerated under 4 different sets of conditions as shown in Table 1. The measured NO.sub.X conversion of the catalyst is shown in table 2 as well as a column showing the conversion recovery. Conversion recovery is defined as the NO.sub.X conversion of the regenerated catalyst divided by the NO.sub.X conversion of fresh catalyst. Table 2 also shows the amount of sulfur on the catalyst. Table 2 shows the above data for fresh catalyst, for catalyst after it has been used to treat process gas and then after each of the regeneration conditions shown in Table 1.

(22) TABLE-US-00001 TABLE 1 Regeneration Condition A B C D Air flow (hr.sup.−1) 1000 1000 1000 1000 H2O (vol. %) 30 40 30 30 T (° C.) 350 350 325 310 Duration (hrs) 48 24 48 48

(23) TABLE-US-00002 TABLE 2 Fresh After catalyst use A B C D NO.sub.x Conversion (%) 76.0 23.5 76.7 72.3 75.1 68.3 Conversion Recovery 101 95.1 98.8 89.9 (%) Sulfur (wt %) 0.10 4.30 0.29 0.41 0.55 1.18

(24) As can be seen from the tables, the regeneration process using steam under regeneration conditions is effective in restoring the NO.sub.X conversion rate of the deNO.sub.X catalyst to or close to its original NO.sub.X conversion rate.

Example 2

(25) In this example, the same type of catalyst was contacted under different industrial conditions with a different process gas. In this example, the catalyst was regenerated under different conditions, some of which included the continued contacting with process gas (or process gas components, such as NO.sub.X and SO.sub.2). Table 3 shows the different regeneration conditions. Table 4 shows the catalyst performance and other data for fresh catalyst, after use in the SCR process and then after each of the regeneration conditions shown in Table 3.

(26) TABLE-US-00003 TABLE 3 Regeneration Condition E F G H I Air flow (hr.sup.−1) 1000 1000 1000 1000 1000 H.sub.2O (vol. %) 30 15 40 20 20 NO.sub.x (ppmv) 0 0 200 200 200 SO.sub.2 (ppmv) 0 0 0 0 8 T (° C.) 325 325 325 325 325 Duration (hrs) 48 48 24 24 24

(27) TABLE-US-00004 TABLE 4 Fresh After catalyst use E F G H I NO.sub.x Conversion 76.0 45.9 75.2 71.8 75.5 72.5 72.8 (%) Conversion 98.9 94.5 99.3 95.4 95.8 Recovery (%) Sulfur (wt %) 0.10 1.95 0.64 0.88 0.82 1.13 1.22

(28) As can be seen from Example 2, the regeneration process is effective even when continuing to flow process gas through the catalyst as shown by the flow of NO.sub.X and SO.sub.2 during the regeneration step.

Example 3

(29) In this example, a deNO.sub.x catalyst was contacted with a process gas containing 7 ppm of SO2. The subsequently deactivated catalyst was regenerated by contacting it with steam at a temperature of 260° C. for 24 hours. During the regeneration, the catalyst was contacted with a stream comprising 40 vol % steam. The figure depicts the NO.sub.x conversion at a number of temperatures, from 160° C. to 200° C., of the fresh catalyst (A), the catalyst after contacting with process gas for 48 hours (B), the catalyst after contacting with process gas for 96 hours (C); and the catalyst after the regeneration step (D). As can be seen from the figure, the regeneration was effective at restoring the NO.sub.x conversion rate of the catalyst to substantially the same NO.sub.x conversion rate as the fresh catalyst.