KR100297039B1 - How to remove waste during the production of acrylonitrile - Google Patents

Abstract

In a fluidized bed catalyst which improves the process of introducing the organic compound (s) into the fluidized bed catalytic reactor at the point where the organic compound (s) reacts substantially with all of the excess ammonia without affecting the acrylonitrile yield. A process for the substantial or complete removal of ammonium sulfate, which occurs during the production of acrylonitrile, by direct ammonia oxidation of propylene / propane, ammonia and oxygen containing gases such as air.

Description

[Name of invention]

Method for removing waste during the production of acrylonitrile

Detailed description of the invention

The present invention relates to wastes obtained from unreacted ammonia during the production of acrylonitrile by direct ammonia oxidation of unsaturated or saturated hydrocarbons, preferably propylene or propane, ammonia and oxygen, in a fluidized bed reactor containing an ammonia oxidation catalyst and A method of significantly reducing ammonium sulfate and substantially removing unreacted ammonia. In particular, the present invention substantially reduces the amount of ammonia present in the gas effluent exiting the fluidized bed reactor by adding an oxygen containing compound, preferably methanol, in a specific location of the fluidized bed reactor during the production of acrylonitrile. It relates to a method of removal, which translates to completely or substantially reducing the production of ammonium sulfate during recovery and purification of the acrylonitrile produced. Such substantial reduction or complete removal of ammonium sulfate during the production of acrylonitrile provides significant environmental and economic benefits.

There are several patents that describe the process of producing hydrogen cyanide by injecting methanol into a fluidized bed reactor. These patent documents also describe further the preparation of hydrogen cyanide during the production of acrylonitrile by injecting methanol into the acrylonitrile fluidized bed reactor. For example, US Pat. Nos. 3,911,089 and 4,485,079 each describe ammonia oxidation of methanol to produce hydrogen cyanide by injecting methanol into a fluidized bed reactor containing an ammonia oxidation catalyst suitable for the production of acrylonitrile. In addition, each of these documents describes that methanol injection can be performed simultaneously with the preparation of acrylonitrile. Also, Japanese Patent Application Nos. 74-87,474, 79-08655 and 78-35232 all describe similar methods for increasing or producing hydrogen cyanide during the production of acrylonitrile. Japanese Patent Application No. 74-87,874 also suggests that the reduction of the amount of unreacted ammonia together with the decrease in the amount of sulfuric acid used for neutralization is the secondary effect of these processes. All of these patents are primarily concerned with the generation of ancillary hydrogen cyanide.

The present invention relates to the preparation, recovery and purification of acrylonitrile by injecting oxygenate compound (s) or mixtures or organics, preferably methanol, which are capable of reacting with ammonia at specific locations in a fluidized bed reactor. The ammonium sulphate produced during the invention is directed to a specific process which can be removed substantially or completely without any reduction in acrylonitrile production.

The first object of the present invention relates to a method for removing or substantially reducing the amount of ammonium sulphate generated during the production of acrylonitrile.

Another object of the present invention is to remove or substantially reduce the amount of unreacted ammonia flowing out of the reactor effluent during the production of acrylonitrile.

Additional objects, advantages and novel features of the invention will appear in the description which follows, and will be apparent to those skilled in the art by the following examples or learned by practice of the invention. The objects and advantages of the invention may be understood by means and combinations particularly pointed out in the appended claims.

In order to achieve the above objects according to the object of the present invention as described and specified in the present invention, the process of the present invention is a hydrocarbon, ammonia and oxygen selected from the group consisting of propylene and propane to be reacted in the presence of a fluidized bed catalyst. The gas is introduced into the bottom of the fluidized bed catalyst to produce acrylonitrile: an oxygen-containing compound capable of reacting with ammonia without substantially affecting the reaction of hydrocarbons, ammonia and oxygen-containing gases producing acrylonitrile. At the point of a fluidized bed reactor which reacts with substantially all of the unreacted ammonia present in the reactor to substantially remove ammonia from the reactor effluent flowing out of the reactor, the oxygen containing compound is introduced: acrylonitrile Containing substantially unreacted ammonia Containing reactor effluent does not, by passing the quenching tower to cool the reactor effluent in the absence of sulfuric acid with water to remove unwanted impurities and: comprises a process of recovering acrylonitrile from the quenching tower.

In a preferred embodiment of the process of the invention, the oxygen containing compound is selected from the group consisting of formaldehyde and methane or compounds thereof, most preferably methanol.

In another preferred embodiment of the process of the invention, the oxygen containing compound, preferably methanol, is introduced into the reactor at a temperature below its coking temperature (about 680 ° -700 ° F).

In another preferred embodiment of the process of the present invention, methanol is injected into the reactor through a conduit capable of maintaining a temperature below the coking temperature of the methanol prior to exiting the reactor. Preferably, the conduit comprises an adiabatic sparger containing at least one main tube connected to at least one side tube containing at least one nozzle and / or anodized ceramic or sheath sparger.

In another preferred embodiment of the process of the invention, methanol is injected into the reactor upwards.

In another aspect of the present invention as broadly described and embodied herein, the process of the present invention comprises a process consisting of propylene and propane into the bottom of a fluidized bed reactor containing said catalyst reacted in the presence of a fluidized ammonia oxidation catalyst. A process consisting of introducing acrylonitrile to form selected hydrocarbons, ammonia and oxygen-containing gases, wherein an oxygen-containing compound capable of reacting with ammonia is substantially responsible for the reaction of hydrocarbons, ammonia and oxygen-containing gases that produce acrylonitrile. This oxygen is directed upwards into the upper point of the fluidized bed reactor which reacts with substantially all of the unreacted ammonia present in the reactor to substantially remove ammonia from the reactor effluent flowing out of the reactor without affecting the reactor. Inclusion A method that improves the process of introducing water.

In a preferred embodiment of the invention, methanol is injected into the top of the reactor at a position of at least 70% of the calculated bed height of the expanded flow catalyst.

In another preferred embodiment of the present invention, methanol is injected into the top of the reactor at a position of at least 85% of the calculated bed height of the expanded flow catalyst.

In another preferred embodiment of the invention, methanol is injected into the top of the reactor at a position at least 90% of the calculated bed height of the expanded flow catalyst.

In another preferred embodiment of the invention, methanol is injected into the fluidized bed reactor through a conduit capable of maintaining a temperature below its coking temperature prior to exiting the reactor.

In another preferred embodiment of the method of the present invention, the conduit member for methanol comprises a sparger comprising one or more main tubes in connection with one or more side tubes comprising one or more nozzles.

In another preferred embodiment of the method of the present invention, the interior of the conduit for methanol is maintained at a temperature below the coking temperature of methanol by providing an insulating cover on the outer surface of the conduit. Preferably, the second conduit is provided on the outer surface of the insulation, whereby the surface for the insulation is further protected.

Representative oxygen-containing compounds suitable in the practice of the present invention are aldehydes, carboxylic acids, ketones, alcohols, esters or mixtures thereof. An essential condition of the oxygen-containing compound is that it does not affect the efficiency of the main reaction that reacts with excess ammonia in the reactor to substantially remove the ammonia from the effluent flowing out of the reactor and produce acrylonitrile. Preferred oxygen-containing compounds are formaldehyde and methanol, with methanol being particularly preferred.

In another preferred embodiment of the process of the invention, a mixture of organic compounds comprising at least one compound which can react with substantially all of the excess ammonia in the reactor but does not affect the efficiency of the main reaction producing acrylonitrile. Is introduced into the reactor. Examples of such mixtures may be organic or aqueous waste streams containing olefinic compounds, substituted aromatics and / or oxygen containing compounds.

The specificity of the process in the present invention is for the substantial removal of ammonia breakthrough (eg unreacted NH ₃ ) in a fluidized bed reactor with the major advantage of removing by-product ammonium sulfate during the production of acrylonitrile. To provide a simple and economic way. Removal of ammonium sulfate from the waste stream during the production of acrylonitrile means that the waste stream does not contain any inorganic salts or only minimal amounts of inorganic salts. This provides a significant economic benefit in the implementation of the acrylonitrile process where no deepwell injection can be performed. Generally, waste streams exiting the quench tower contain (NH ₄ ) ₂ SO ₄ at a fairly high concentration that makes it difficult to dispose of these streams in an economically and environmentally acceptable manner. Removal or minimization of such ammonium salts from such streams allows the treatment of these streams in waste treatment processes that do not require stringent conditions or expensive structure (eg incineration) materials, or significant economic and environmental considerations even if cardiovascular injection is not available. It can bring about enemy advantages.

Preferred embodiments of the present invention will be described later in detail.

The present invention reacts with oxygen containing compound (s) or ammonia into a fluidized bed reactor that allows substantial or complete reaction between excess ammonia and oxygen containing compounds in the reactor without substantially affecting the efficiency of acrylonitrile production. Mixtures of one or more compounds, preferably organic compounds, including methanol, are added to minimize the production of ammonium sulfate that occurs during the production of acrylonitrile. Substantial or complete removal of ammonium sulfate from the waste stream discharged from the quench tower of the acrylonitrile plant significantly enhances the environmental impact and economics associated with the implementation of the acrylonitrile process.

In a preferred implementation of the present invention, methanol has the opportunity to react with all or substantially all of the excess ammonia, but does not affect the propylene ammonia oxidation main reaction occurring at the bottom of the catalyst, through a sparger in a fluidized bed reactor. Into the catalyst zone or to said zone (ie at least 100% of the height of the expanded catalyst bed). For the purposes of the present invention, fluidized bed reactors include certain reactors, such as mobile line reactors, granular reactors or circulating reactors, which can not only include conventional fluidized bed reactors but also maintain the catalyst in a fluidized state.

In another preferred embodiment of the present invention, the location of the methanol feed should be at the 70% level, preferably at the 80-90% level, most preferably above 90% of the height of the expanded catalyst bed. As used herein, expanded catalyst bed height refers to catalyst bed height while the catalyst is in a fluidized bed state. That is, it refers to the phase height when the gas component is present in the fluidized bed reactor and mixed with the catalyst.

Oxygen-containing (preferably methanol) can be injected purely or in the presence of other gases or combinations thereof, such as nitrogen, water, air, circulating exhaust gases. It may be injected in liquid or vapor form in a particular direction, preferably in an upward direction, by one or more means, such as a sparger or a spray. The feed tube may enter the reactor at a suitable height in a suitable sparger / design / direction or from a pipe near or at the bottom of a conventional feed grid / sparger.

The amount of methanol used may vary but should be sufficient to neutralize any excess ammonia spill in the reactor effluent. Unreacted methanol obtained in the effluent may be recovered and recycled to the reactor or disposed of by conventional procedures (eg oxidation).

In another preferred embodiment of the invention, methanol is introduced into the catalyst at a temperature below its coking temperature (about 680-700 ° F.). This is a common sparger design (large mains, medium sized side pipes, and side pipes that are allowed to be distributed to the main building), which is modified to prevent the temperature of methanol from reaching its carbonization (cocking) temperature before being released into the catalyst bed. It is preferably carried out by the use of (uniformly distributed nozzles). The sparger is deformed by coating a monolayer on the outer surface of the sparger to prevent the temperature of the inner surface of the sparger tube / nozzle from reaching the methanol coking temperature. The most preferred sparger is modified to include a first tube having a second tube nested inside the first tube and forming a space away from the first tube. The space between the tubes is filled with conventional insulation. This design protects the insulation from corrosion of its surface by the fluidized bed catalyst.

Each propylene / propane ammonia oxidation catalyst acts to some degree different feed rates and operating conditions, taking into account maximum acrylonitrile yield and / or economics. The amount of excess ammonia exiting the propylene ammonia oxidation reactor will depend somewhat on the catalyst used. The amount of methanol to be added will also vary depending on the type of catalyst and the nature of the reactor. Thus, in the practice of the present invention, the amount of methanol injected into the reactor will be determined by the conditions used and the catalyst. In the case of catalysts operating on poor oxygen, it may be necessary to add additional oxygen to the reactor. However, catalysts operating in excess oxygen will not require the addition of oxygen to the reactor. In general, any ammonia oxidation catalyst can be used in the practice of the present invention. For example, catalysts as described in US Pat. Nos. 3,642,930, 4,485,079, 3,911,089, 4,873,215, 4,877,764, Japanese Patent Application Nos. 74-87474 and 78-35232 are disclosed It is suitable for carrying out and is referred to in the present invention.

As already stated, each propylene / propane ammonia oxidation catalyst will operate at somewhat different feed rates and operating conditions. During the performance of the process of the present invention, the standard operating conditions under which the propyllan / propane catalyst in the reactor operates should not change but may vary with feed and catalyst conditions. Conventional operating conditions and feed rates are suitable for the preparation of acrylonitrile as described in US Pat. Nos. 3,911,089 and 4,873,215 and are referred to in the present invention. However, if the catalyst used is low or at least operate in an oxygen environment, it may be necessary to put a certain amount of oxygen into the reactor so that the process of the present invention operates most efficiently. This can be done by increasing the oxygen ratio in the feed or by actually supplying oxygen into the reactor by individual means.

For purposes of illustration only, the following examples are described describing the process of the present invention.

Example 1

Into a 1.5 inch diameter reactor is charged 550 g of activated BiMoFeO propylene ammonia oxidation catalyst. The feed of propylene / air / ammonia is passed through the catalyst bed at a WWH space velocity (weight per hour) of 443 ° C., 12.0 psig, 0.045 at a molar ratio of 1 / 10.5 / 1.15. After 2 hours of operation, the propylene conversion was 98.3%, the per pass conversion (PPC) to acrylonitrile (AN) was 76.3%, and the PPC to hydrogen cyanide (HCN) was 7.1%, about 15 % Ammonia feed leaks. Similar tests performed for 27 hours under the same conditions showed propylene conversion, PPC to AN and PPC to HCN, respectively, 97.8%, 75.1% and 8.7%, and for 9 hours, 99.1%, 73.8% and 8.3, respectively. % And both sides leak about 15% ammonia.

Example 2

The procedure of Example 1 is repeated but methanol is introduced into the catalyst bed 75% from the top of the expanded catalyst bed in a molar ratio of 0.18 to 1.0 relative to propylene. The recovery process was carried out after 75 hours (total operating time) of operation. As a result, the propylene conversion was 98.4%, the PPC to AN was 72.1%, the PPC to HCN was 10.1% and about 9% ammonia leaked (Example 6% less than 1).

Example 3

The procedure was carried out in the same manner as in Example 2, but when methanol was introduced in an upward direction at an expanded catalyst bed height of 70%, the propylene conversion was 96.3%, the PPC to AN was 73.3%, and the PPC to HCN was 9.4% and the ammonia leak in the effluent is only 2% of the amount fed into the reactor.

Example 4

A 1.5 inch diameter reactor is charged with 550 g of an activated BiMoFeO propylene ammonia oxidation catalyst having a composition different from that used in Examples 1-3. The feed of propylene / air / ammonia is passed through the catalyst bed at 440 ° C., 12 psig, WWH medium rate (weight per hour) of 0.075 at a molar ratio of 1 / 9.3 / 1.15. After 283 hours of operation, the recovery process is performed to determine the amount of product formed. As a result, the total propylene conversion was 96.6%, the PPC to AN was 78.7%, the PPC to HCN was 5.6%, and 5.4% ammonia leaked out.

Example 5

The procedure of Example 4 is repeated, but methanol is introduced in the upward direction from the top of the expanded catalyst bed to the catalyst at 30% point in the molar ratio of 0.09 to 1.0 relative to propylene. As a result of the recovery process in 332 hours of operation, the total propylene conversion was 96.9%, the PPC to AN was 78.1%, the PPC to HCN was 5.8%, and no ammonia leak was found. Therefore, the methanol conversion rate is 100%.

Example 6

Further testing was carried out using the same catalyst as the inlet feed conditions described in Example 5 and changing the molar ratio of propylene / air / ammonia / methanol to 1 / 9.3 / 1.08 / 0.09, whereby the total propylene conversion was 96.1%, PPC to AN is 77.9%, PPC to HCN is 4.9% and no ammonia leak. In this case as well, the methanol conversion rate is 100%.

Example 7

Approximately 18 tonnes of propylene ammonia oxidation catalyst (activated BiMoFeO) is placed in a larger acrylonitrile reactor. A feed with a molar ratio of propylene / air / ammonia of 1 / 10.0 / 1.2 is passed through the catalyst bed at 840 ° F, 12.0 psig. After 24 hours of operation, the propylene conversion was 99.8%, the PPC to AN was 75.3%, and the PPC to HCN was 8.2%. In particular, the ammonia leak is 12% of the feed, and in order to neutralize the excess ammonia in the reactor, the amount of sulfuric acid used in the downstream quench operation under these conditions is 0.33 gpm. After three days of operation under the same conditions, the propylene conversion was 99.6%, the PPC to AN was 75.7%, the PPC to HCN was 8.2% and about 14% ammonia feed was leaked.

Example 8

Pure methanol superheated steam is injected at about 0.05, 0.1, 0.15, 0.2 and 0.26 moles per mole of propylene into the catalyst at 95% of the height of the expanded catalyst bed in the reactor while running under the same reactor and reaction conditions as in Example 7. As a result of the recovery process at a MeOH / propylene ratio of 0 to 0.26, the average propylene conversion was 99.6%, the PPC to AN was 76.1%, and the PPC to HCN was 7.2%. The total methanol conversion is 99.6% on average and the PPC conversion of methanol to HCN is 65% on average. The relationship between methanol ratio, ammonia leak rate, and sulfuric acid usage is shown in Table 1 below:

TABLE 1

This demonstrates no ammonium sulfate production (last three steps in Table 1) without adversely affecting normal acrylonitrile production.

Example 9

While repeating under similar conditions as in Example 8, methanol is introduced at a different ammonia feed rate onto the catalyst at 90% of the height of the expanded catalyst bed in the reactor. The amount of propylene ammonia oxidation catalyst is increased by about one ton such that the relative position of the methanol sparger in the catalyst bed is about 90% expanded catalyst bed height. Feeds with a propylene / air / ammonium molar ratio of 1 / 10.0 / 1.1 similarly pass through the catalyst bed. At 14 days of operation, the propylene conversion was 99.8%, the PPC to AN was 74.4%, and the PPC to HCN was 8.3%. Unreacted ammonia is 8.4% of the reactor feed ammonia. The amount of sulfuric acid used is 0.26 gpm during the downstream quench operation to neutralize excess ammonia in the reactor. This example shows that the relative position of the methanol injection point can be easily adjusted by simply changing the weight of the reactor contents.

Methanol vapor is introduced at 90% of the height on the reactor catalyst under these conditions. When the recovery process is performed at a molar ratio of MeOH / propylene of 0.09, the total conversion is 99.7%, the PPC from propylene to AN is 74.8%, the PPC to HCN is 8.0%, the total methanol conversion is 99.8%, methanol PPC to HCN is 58%, ammonia leakage is reduced to 4.1% of the feed and sulfuric acid consumption is reduced to 0.07 gpm. When the recovery process is performed at a molar ratio of MeOH / propylene of 0.12, the total conversion is 99.7%, the PPC from propylene to AN is 74.9%, the PPC to HCN is 7.9%, the total methanol conversion is 99.8%, methanol PPC to HCN is 53%, and ammonia leakage is reduced to 0% of feed ammonia, thus no sulfuric acid is required and no ammonium sulfate is formed.

Example 10

The test was repeated under similar conditions as in Examples 8 and 9, but the introduction of methanol to the 85% point of the normal expansion catalyst bed height in the reactor resulted in a reduction of the reactor feed ammonia leakage rate from 11% to 1.8%. Subsequent decreases in ammonium sulfate also occur, but also reduce the yield of AN compared to those introduced at 90% or more of the height of the expansion catalyst while increasing the selectivity of methanol to HCN.

Example 11

Different bismuth molybdate type ammonia oxidation catalyst (550 g) is placed in a reactor (1.5 inch diameter). The feed with a propylene / air / ammonium molar ratio of 1 / 9.5 / 1.2 is passed through the catalyst bed at 450 ° C., 10 psig, 0.060 WWH medium speed (weight per hour). Water in the form of steam is introduced onto the catalyst in a molar ratio of 0.3 to 1.0 relative to propylene. As a result, the acrylonitrile conversion was 72.6%, at 89.4% propylene conversion, hydrogen cyanide was 4.3% and 6.4% of the supplied ammonia leaked out.

Example 12

The procedure of Example 11 is repeated but an aqueous (59 vol% mole) stream containing 0.3 mole ratio of organic compound per mole of propylene is introduced onto the catalyst at 70% of the height of the expansion catalyst bed. It is mole%, containing other trace components with 0.5% acrolein, 4.3% ethanol, 0.4% oxalic acid, 3.4% acetone, 6.9% methyl formate and 1.8% acrylic acid. After 5 hours of operation, the recovery rate was measured. The conversion rate of propylene was 89.7%, acrylonitrile PPC was 68.2%, hydrogen cyanide was 3.9%, and ammonia leakage was reduced to 2.8% of feed. . This waste stream reduces the ammonia remaining in the reactor effluent by 50% or more, ie reduces the need to neutralize and / or produces less ammonium sulfate, generates no additional hydrogen cyanide, and hazardous wastes such as acrylic acid. Clearly encouraging as the by-products can be used simultaneously and the result is the conversion of them to more useful materials.

Example 13

The same test as in Example 12 was conducted, but a nonaqueous feed was used as the ratio of 0.5 moles of waste organics per 1.0 mole of propylene. It is a mole percent that can be reacted with ammonia on a bismuth molybdate type catalyst as 5.3% n-propanol, 3.3% isobutyl formate, 11.0% ethylene glycol, 12.8% isobutanol, 1.5% ethylether , 0.6% m-xylene, 0.5% 1-methyl-1-cyclohexene, and minor amounts of other components. As a result of the analysis of the reactor effluent, these components are in most cases converted to acrylonitrile, acetonitrile or methacrylonitrile and there is a corresponding decrease in these organic wastes. Dicyanobenzene is found from m-xylene, which shows that it can be used as a selected aromatic compound in waste solutions, such as a nitrile derivative of an olefinic substituted cyclohexene.

Example 14 below illustrates the process of the present invention injecting methanol above the catalyst bed height.

Example 14

0.4 mole of methanol per mole of propylene is introduced into the reactor at a point above the catalyst dense phase in the dilution zone (more than 100% of the height of the expanded catalyst bed). Comparative analysis of the product and effluent before and after the introduction of methanol shows a 15% reduction in post-use ammonia leakage compared to before use of methanol.

The above example clearly illustrates the dramatic improvement that occurs when performing the method. Each example shows a significant reduction in the amount of NH ₃ leak, thereby substantially eliminating the (NH ₄ ) ₂ SO ₄ amount that is generated without any significant effect on acrylonitrile yield. On the other hand, these embodiments are intended to illustrate the implementation of the invention, not intended to limit the applicant's invention to them, and obviously many variations and modifications may be possible in light of the above description. It is intended that the scope of the applicant's invention be limited by the claims appended hereto.

Claims (20)

Introducing a hydrocarbon, ammonia and oxygen containing gas selected from the group consisting of propylene and propane to be reacted in the presence of a fluidized bed catalyst to the bottom of the fluidized bed reactor to produce acrylonitrile; Under temperatures below the coking temperature of oxygen-containing compounds such as methanol that can react with ammonia, the oxygen compounds produce acrylonitrile without affecting the reaction of hydrocarbons, ammonia and oxygen-containing gases, At least 70% of the calculated expansion flow catalyst bed height where the ammonia in the reactor effluent flowing out of the reactor in response to unreacted ammonia is reduced or completely removed, introduces the oxygen containing compound to the upper point of this fluidized bed reactor and; Reactor effluent containing acrylonitrile and containing little or no traces of unreacted ammonia is passed through a quench tower to cool the reactor effluent with water in the absence of sulfuric acid to remove unwanted impurities; A process for removing ammonium sulfate and ammonia leaks formed during the production of acrylonitrile, characterized by the process of recovering acrylonitrile from the quench tower. The method of claim 1 wherein the oxygen containing compound is selected from the group consisting of formaldehyde and methanol or mixtures thereof. The method of claim 1 wherein the oxygen containing compound is methanol. 4. The process of claim 3 wherein the hydrocarbon is selected from propylene. 4. The method of claim 3 wherein the methanol is introduced into the reactor through a conduit capable of maintaining the temperature of the methanol below the coking temperature of the methanol prior to exiting the reactor. 6. The method of claim 5 wherein the conduit comprises an insulated sparger comprising one or more main tubes connected with one or more side tubes comprising one or more nozzles. 6. The process of claim 5 wherein methanol is introduced into the reactor at a point of at least 70% of the calculated height of the expanded catalyst bed. The method of claim 5 wherein methanol is injected into the reactor from above. Acrylonitrile, consisting of preparing acrylonitrile by introducing hydrocarbon, ammonia and oxygen containing gas selected from the group consisting of propylene and propane into the bottom of the reactor containing the catalyst reacting in the presence of a fluidized ammonia oxidation catalyst. As a method of removing ammonia leaks during the production of oxygen, oxygen-containing compounds, such as methanol, which can react with ammonia are present in the reactor without affecting the reaction of hydrocarbons, ammonia and oxygen-containing gases that produce acrylonitrile. Coking temperature of the oxygen-containing compound, upwards into the upper point of the fluidized bed reactor at a position above 70% of the calculated expanded flow catalyst bed height where the ammonia is reduced or removed from the reactor effluent exiting the reactor in response to the reacted ammonia At temperatures below A method of improving the process of introducing an oxygen-containing compound. 10. The process of claim 9 wherein the hydrocarbon is selected from propylene. The process of claim 10 wherein the oxygen containing compound is injected into the top of the fluidized bed reactor at a point of at least 85% of the calculated height of the expanded fluidized bed. 10. The method of claim 9, wherein the oxygen containing compound is introduced into the fluidized bed reactor through a conduit that maintains its temperature below the coking temperature of the oxygen containing compound before flowing into the reactor. 13. The method of claim 12, wherein the inner wall of the conduit for the oxygen containing compound is provided at a temperature below the coking temperature of the oxygen containing compound by providing an insulation covering around the outer wall of the conduit. The method of claim 13, wherein a second conduit is provided around the outer surface of the insulation to protect the surface for the insulation. 15. The method of claim 14, wherein the oxygen containing compound consists essentially of methanol. Introducing a hydrocarbon, ammonia and oxygen containing gas selected from the group consisting of propylene and propane to be reacted in the presence of a fluidized bed catalyst to the bottom of the fluidized bed reactor to produce acrylonitrile; Calculated to produce acrylonitrile without affecting the reaction of hydrocarbons, ammonia and oxygen-containing gases and to react with unreacted ammonia present in the reactor to reduce or eliminate the ammonia in the reactor effluent exiting the reactor At a position of at least 70% of the height of the expanded flow catalyst bed, introducing a mixture of organic compounds capable of reacting with ammonia and containing olefinic compounds or substituted aromatics to the upper point of the fluidized bed reactor; Reactor effluent containing acrylonitrile and containing little or no traces of unreacted ammonia is passed through a quench tower to cool the reactor effluent with water in the absence of sulfuric acid to remove unwanted impurities; A process for removing ammonium sulfate and ammonia leaks formed during the production of acrylonitrile, characterized by the process of recovering acrylonitrile from the quench tower. 17. The process of claim 16, wherein the mixture of organic compounds is selected from the group consisting of organic waste streams and aqueous waste streams containing olefinic compounds, substituted aromatics and oxygen containing compounds and mixtures thereof. 18. The process of claim 17, wherein the hydrocarbon is selected from propylene. Acrylonitrile, prepared by introducing hydrocarbon, ammonia and oxygen containing gases selected from the group consisting of propylene and propane into the bottom of a fluidized bed reactor containing said catalyst reacting in the presence of a fluidized bed ammonia oxidation catalyst. As a method of reducing or eliminating ammonia leaks during the production of ronitrile, a mixture of organic compounds that can react with ammonia and contain olefinic compounds or substituted aromatics is used to produce propylene, ammonia and oxygen-containing gases. Upper point of the fluidized bed reactor at a position of at least 70% of the calculated expanded flow catalyst bed height where ammonia is reduced or removed from the reactor effluent exiting the reactor by reacting with unreacted ammonia present in the reactor without affecting the reaction My prize Improving the process of introducing the mixture in the 20. The method of claim 19, wherein the mixture is injected into the fluidized bed reactor from above.