METHOD FOR THE PREPARATION OF MELAMINE

Abstract: An improved method for the preparation of melamine by the conversion of urea and/or thermal decomposition products thereof. The urea and/or thermal decomposition products are converted to melamine in a fluidized bed of catalytically active material in the presence of a gas mixture containing ammonia and carbon dioxide. The partial pressure of ammonia in the gas mixture in the fluidized bed is maintained at a level of at least 70 kPa, whereby the formation of deamination by-products is susbtantially reduced.

Description: METHOD FOR THE PREPARATION OF MELAMINE The invention relates to a method for the preparation of melamine by converting urea and/or thermal decomposition product thereof in a fluid bed of catalytically active material in the presence of a Oas mixture containing NH3 and CO2, using a gasmixture of ammonia and carbondioxide as the fluidizing gas. From Hydrocarbon Processing, September 1969, pp. 184-186, it is known to prepare melamine at atmospheric pressure and to subsequently separate it from the reaction gases formed by means of a so-called 'dry catch'. The gases freed of melamine, consisting mainly of NH3 and CO2, are partly recirculated as fluidizing gas for the fluid bed of catalytically active material. This method has the disadvantage that, at the pressure applied and the partial pressure of ammonia corresponding with it, so many deamination products of melamine are formed that it is necessary to remove these products prior to the separation of melamine from the reaction gases. This necessitates a hot gas filtration, which requires substantial investments and which is laborious. The purpose of the invention is to provide a method for the preparation of melamine in which hardly any or no deamination products are formed. According to the invention this. method is characterized in that the partial pressure of ammonia in the fluid bed is at least 70 kPa. The fact is that, surprisingly, it has been found that at partial pressures of ammonia of a minimum of 70 kPa already very few deamination products are formed. In a preferred embodiment of the method according to the invention the partial pressure of NH3 is at least 100 kPa, more specifically 350 kPa. In the processes for preparing melamine at atmospheric pressure, the ammonia partial pressure in the fluidized bed is about 50-60 kPa. In the medium pressure processes ammonia partial pressure higher than 70 kPa may occur. In these processes, howevçr, ammonia is used as fluidizing gas. The ratio of ammonia to carbondioxide (molar, or by (volume, which is the same) in the fluidized bed is in these processes about 90-95 to 10-5. The separation of melamine from the gases coming from the reactor can be effected by direct or indirect cooling. For instance, cold NH3 gas or gas mixtures of NH3 and CO2 can be mixed with the reaction gases. Another possibility is the application of a desublimation of melamine in one or more fluid beds of melamine particles with application of indirect cooling. This indirect cooling will preferably be effected with cooling water, in which process, by running the cooling water counter current to the melamine reaction gases, high-quality steam is formed. The advantage of this method is that relatively large melamine particles are obtained with a relatively narrow particle size destribution. Moreover, the melamine obtained in this manner is free flowing, so that it can be conveyed in bulk, which is not the case when direct cooling is applied. The gas mixture of NH3 and CO2, which is used as fluidizing gas in the melamine reactor, preferably consists of 90 ' by weight of NH3 and CO2, while the volume ratio between NH3 and CO2 may be between 1.5-1 and 2.5-1. The total pressure in the fluid bed is preferably 2, 500 kPa at most, more specifically 1,250 kPa at most. As catalyst in the fluid bed in the reactor one of the known catalysts can be used, such as aluminium oxide, aluminium oxide on silican oxide, silicon oxide, titanium oxide, zirconium oxide, boron phosphate or aluminium phosphate or a mixture of 2 or more of these catalysts. The expression catalyst or catalytically active material is understood here to mean any material promoting, under the reaction con- ditions applied, the conversion of urea into melamine. The temperature at which the melamine isbformed from urea is 0 generally more than 325 C. In general, this temperature will not be above 460 OC, more specifically preference is given to temperatures of 0 between 370 and 400 C. The temperature applied depends, in part, on the pressure in the reactor. The invention will now be eludicated by means of a drawing in which fig. 1 gives a graph in which the content of deamination products in the reactor .gases has been plotted as a function of the natural logarithm of the partial pressure of ammonia in the fluid bed and fig. 2 gives a diagrammatic embodiment of a method for the preparation of melamine in which the method according to the invention can be applied. From fig. 1, in which the relative content of deamination products in the melamine-containing reaction gas(A) has been plotted as a function of the natural logarithm of the partial pressure of ammonia (B, kPa) in this gas, it is clear that as the partial pressure increases this content decreases very strongly. The content of deamination products has been given in respect of the value at the NH3 partial pressure of 100 kPa, which has been fixed at 1. In figure 2 a diagrammatic embodiment of the method according to the invention has been given. In reactor l'urea is atomized, through sprayers 2, 3, in a fluid bed of catalyst particles. This bed is fluidized by means of a gas mixture supplied through fluidizing gas supply 4 and gas distributor plate 5. In the fluid bed the desired temperature is maintained by means of heat exchanger pipes 6, which have been shown here diagrammatically. The melamine-containing reactor gases are fed, through cyclone 7 and line 8, to desublimator 9. In this desublimator 9, which is in the form of one or more fluid beds of melamine particles, melamine is desublimated. Through heat exchanger tubes 10, the heat released in this process is removed and converted into high pressure steam. At the bottom of desublimator 9 solid melamine particles are removed through line 11, In separator 12 melamine is separated from the gases. The gases are returned, through line 13, to the desublimator 9. Through line 14, and after pressure reduction via valve 15, the melamine is removed. Through cyclone 16 and line 17 the off gas mixture, freed of melamine, is removed. A part of the off gas mixtures removed through line 18, for instance to a urea synthesis, an NH3-CO2 separation or a fertilizer preparation. The remaining part is recirculated, throug linel9, compressor 20, line 21 and heat exchanger 22, to the reactor 1. The invention will now be elucidated by means of an example but is not restricted to it. Example The melamine preparation was performed in an installation as described in figure 2. To the melamine reactor, operating at a pressure of 1,000 kPa 0 and a temperature of 375 C, 20,000 kg of urea and 30,000 kg of gaseous NH3 and CO2 were fed per hour. The partial pressure of NH3 was 600 kPa. The reaction gases, containing melamine vapours, were fed to desublimator 9, which also operated at a pressure of 900 kPa. This desublimator contained a fluid bed with melamine particles. Per hour about 7,000 kg of melamine with good free-flowing properties and a purity of 99,9 % was discharged from the desublimator. Of the off gas mixture, largely freed of melamine, 80 % was recirculated to the melamine reactor, after compression to compensate for the fall in pressure across the reactor and the desublimator, and heat exchange. The remaining 20 was fed to an NH /Co separation. 3 2

Claims: CLAIMS 1. Method for the preparation of melamine by converting urea and/or thermal decomposition products thereof in a fluid bed of catalytically active material in the presence of a gas mixture containing NH3 and CO2, using a gasmixture of NH3 and CO2 as the fluidizing gas, characterized in that the partial pressure of ammonia in the fluid bed is at least 70 kPa. 2. Method according to claim 1, characterized in that the partial pressure of NH3 is at least 100 kPa. 3. Method according to claim 2, characterized in that the partial pressure of NH3 is at least 350 kPa. 4. Method according to claim 1, characterized in that the gas mixture consists for at least 90 % of NH3 and CO2. 5. Method according to claim 1, characterized in that the volume ratio of NH3 to CO is between 1.5-1 and 2.5-1. 2 6. Method according to claim 1, characterized in that the total pressure in the fluid bed is 2,500 kPa at most, but specifically 1,250 kPa.

Inventors: VAN HARDEVELD, RUDOLF
Applicants: STAMICARBON B.V.
Application year: 1980
Main classification: C07D251
IPC codes: C07D251