AU2003206260B2 - Process for preparing melamine - Google Patents

Description

PROCESS FOR PREPARING MELAMINE

The invention relates to a process for preparing melamine, comprising a first cooling step from which a mixture containing NH₃, CO₂ and H₂O is released, wherein:

• the mixture and a flow of liquid NH₃ are fed to an absorption section; • the mixture and the flow of liquid NH₃ in the absorption section are contacted with each other, with gaseous NH₃and an ammonium carbamate solution being formed;

• the gaseous NH₃and the ammonium carbamate solution are separately discharged from the absorption section.

A process of the same kind is known from "Melamine and Guanamines", section 4.1.3 of Ullmann's Encyclopedia of Industrial Chemistry, Sixth Edition, 2001 Electronic Release. Furthermore, in the known process, the mixture, prior to being supplied to the absorption section, is subjected to a partial condensation step.

The mixture in the known process contains, as mentioned above, NH₃, CO₂ and H₂O. The CO₂ and a part of the NH₃ in the mixture mainly originate from the reaction of urea to form melamine, which proceeds as follows:

6 CO(NH₂)₂ -> C₃N₆H₆ + 6 NH₃ + 3 CO₂

Usually NH₃ is used as fluisidation gas and atomizing gas during the melamine synthesis, which may also cause NH₃to enter the mixture. Fluidization gas serves to keep the synthesis catalyst in a fluid state. Atomizing gas serves to atomize the urea in the synthesis reactor. The H₂O in the mixture mainly originates from the first cooling step, where an aqueous flow is used as a cooling medium for the reaction product; here the H₂O partly evaporates. The aforementioned known absorption section, which is designed as a column, is intended amongst other things to separate a flow of gaseous NH₃from the mixture and discharge it from the absorption section. The discharged flow of gaseous NH₃ is removed and generally returned to a melamine synthesis reactor to serve there as a fluidization gas and/or atomizing gas. A part of the gaseous NH₃ is passed through a scrubber, whose object it is to to separate and discharge so-called inert compounds such as H₂and N₂. The known absorption section is also intended to form, from NH₃ and from virtually all CO₂ and H₂O from the mixture, an ammonium carbamate solution and discharge that solution. The discharged ammonium carbamate solution is removed, after which generally in downstream steps the CO₂ and the NH₃ are liberated from the discharged ammonium carbamate solution, either as such or in the form of an ammonium carbamate solution with a considerably reduced water content, in which process a practically pure flow of water is released which in general is a waste stream and is discharged. As is known, the urea synthesis efficiency decreases as the quantity of water in the raw materials increases. The liberated CO₂ and a part of the liberated NH₃, as such or in the form of an ammonium carbamate solution with a considerably reduced water content, can serve as a raw material for the production of urea or for the production of ammonium nitrate or ammonium sulfate. The remaining part of the liberated NH₃ is liquefied in the known process and recirculated to the absorption section as part of the flow of liquid NH₃. A disadvantage of the known process is that the recovery of the NH₃ to be recirculated to the absorption section from the ammonium carbamate solution requires a great deal of energy, for example in the form of steam.

The object of the invention is to reduce the energy consumption in the downstream steps that are applied to the discharged ammonium carbamate solution.

The said object is achieved in that a part of the discharged ammonium carbamate solution is returned to the first cooling step and a part of the discharged gaseous NH₃ is liquefied in a second cooling step and returned to the absorption section. The process according to the invention ensures that less NH₃ is removed via the ammonium carbamate solution per unit time than in the known process. As a result, the quantity of NH₃ which is liberated in the downstream steps for recirculation to the absorption section can decrease, which yields an energy saving, for example in steam consumption. A further advantage of the process according to the invention is that less H₂O is removed per unit time via the ammonium carbamate solution than in the known process. This allows a decrease in the liquid load of the equipment items in which the downstream steps are carried out for liberating the CO₂ and the NH₃ from the removed ammonium carbamate solution, for example for the preparation of urea. As a result said downstream steps can be carried out in smaller equipment items and with less energy consumption than in the known process, which is cheaper.

The process according to the invention comprises a first cooling step for cooling an essentially gaseous flow originating from a melamine synthesis reactor and containing essentially melamine, NH₃ and CO₂. The flow from the melamine synthesis reactor is contacted with a coolant. The coolant comprises a flow consisting essentially of an ammonium carbamate solution to be discussed later. The coolant comprises in addition generally also a flow essentially consisting of water; for this purpose use is usually made of an aqueous flow originating from a recovery section. The coolant flows can be supplied separately or jointly to the first cooling step. As the flow from the melamine synthesis reactor is contacted with the coolant there evolve a solution (containing dissolved melamine in an aqueous phase) or a slurry (containing melamine crystals in an aqueous phase) and a generally gaseous mixture containing NH₃, CO₂ and H₂O. The solution or the slurry is discharged from the first cooling step and fed to a recovery section in which melamine crystals are formed (if necessary) and separated. The said mixture is usually gaseous and usually contains more than 40 wt% NH₃, less than 50 wt% CO₂ and less than 40 wt% H₂O at a pressure usually between 0.1 MPa and 4 MPa, and is fed to an absorption section. In addition a flow of liquid NH₃ is also fed to the absorption section. The percentages stated here and hereafter are percentages by weight, unless otherwise indicated. In the absorption section according to the invention the mixture is contacted with the flow of liquid NH₃. This gives rise to a flow of gaseous NH₃ and virtually all CO₂ and H₂O go into the liquid phase. To facilitate the transition of CO₂ into the liquid phase, an additional flow consisting essentially of water may be fed to the absorption section. The required quantities of the flow of liquid NH₃ and of the additional flow consisting essentially of water that are fed to the absorption section are largely determined by the desired purity of the discharged flow of gaseous NH₃. Usually a purity of 99% or higher is desired. The higher the desired purity of the discharged gaseous NH₃, the larger the required quantities of the flow of liquid NH₃ and of the additional flow consisting essentially of water. The flow of gaseous NH_3l consisting essentially of NH₃ and which in addition may contain up to approximately 1 wt% of other compounds such as CO₂, H₂O, N₂ and H₂, is discharged from the absorption section. In the process according to the invention a part of the discharged gaseous NH₃ is liquefied in the second cooling step and returned to the absorption section; the remaining part is removed and, as previously indicated, usually used as fluidization gas and/or atomizing gas in the melamine synthesis reactor. It is an advantage of the process according to the invention that the gaseous NH₃ can be used directly as fluidization gas an/or atomising gas, without the need of an evaporating step as is the case when the NH₃ to be used is supplied in liquid form. Liquefication in the second cooling step may be accomplished by means known per se, such as for example by means of a heat exchanger. An advantage of the process according to the invention is that the quantity of fresh liquid NH₃ to be fed to the absorption section can decrease, because a flow of liquid NH₃ is already available. A further advantage of the process according to the invention is that inert compounds such as for example N₂ and H₂, which cannot be easily liquefied because their condensation temperature is much lower than that of NH₃, can readily be separated from the liquefied NH₃ and removed as an inert gaseous vent stream. The inert vent stream will in general still contain a residual quantity of NH₃. If it is desired to remove this residual quantity of NH₃ the inert vent stream can be passed through a scrubber, which can however be significantly smaller than the aforementioned scrubber in the known process.

The liquid phase formed in and discharged from the absorption section consists essentially of an ammonium carbamate solution. By this is meant a solution of ammonium carbamate in water, which in addition may contain other compounds such as free dissolved NH_3l free dissolved CO₂ and ammonium bicarbonate. In the process according to the invention a part of the discharged ammonium carbamate solution is returned to the first cooling step; the remaining part is removed. The returned ammonium carbamate solution serves as a coolant in the first cooling step, will largely evaporate into NH₃, CO₂ and H₂O and will thus be absorbed in the mixture which is released in the first cooling step and is fed to the absorption section; in this way there is formed in the process according to the invention a circulation flow between the first cooling step and the absorption section.

The removed ammonium carbamate solution is generally the most important medium for removing the CO₂ evolving in the urea-to-melamine reaction. As a result, the quantity of CO₂, as such or as an ion, in the removed ammonium carbamate solution is usually an important control parameter for operating an absorption section in a process for the preparation of melamine and also for operating the absorption section according to the invention. The part of the discharged ammonium carbamate solution that is returned to the first cooling step is determined preferably in relation to the quantity of CO₂ that is present in the removed ammonium carbamate solution either as such or as an ion. The quantity of CO₂ in the removed ammonium carbamate solution is hereinafter referred to as removed CO₂. The quantity by weight of ammonium carbamate solution which is returned to the first cooling step divided by the quantity by weight of removed CO₂ is preferably between 0.01 and 5, more preferably between 0.3 and 2.0 and most preferably between 0.7 and 1.7. The part of the discharged gaseous NH₃ which is liquefied can also be expressed in relation to the quantity of removed CO₂. The quantity by weight of discharged gaseous NH₃ which is liquefied divided by the quantity by weight of removed CO₂ is preferably between 0,01 and 5, more preferably between 0.1 and 2.0 and most preferably between 0.5 and 1.5. The absorption section may be of any known design, such as for example a trayed column so configured that the formed ammonium carbamate solution and the formed flow of gaseous NH₃ can be discharged separately.

In order to form the ammonium carbamate solution in the absorption section it is generally necessary to withdraw heat from the mixture. Therefore, prior to being fed to the absorption section, it is preferred to subject the mixture to a third cooling step, wherein partial condensation takes place whereby a liquid phase and a gas phase are formed. The liquid phase then consists essentially of an ammonium carbamate solution. In a further preferred embodiment the liquid phase is separated from the mixture. It is then possible to remove this liquid phase separately from the ammonium carbamate solution coming from the absorption section or to wholly or partially return it to the first cooling step. An advantage of the performance of the said third cooling step is that the operation of this step appears to be a control tool in determining the quantity of gaseous NH₃ that is released from the absorption section as a consequence of the fact that not all compounds of the mixture condense proprotionately; particularly H₂O condenses preferentially, which makes it easier to separate gaseous NH₃ in the absorption section.

In another preferred embodiment of the process according to the invention a compression step is carried out on least the part of the discharged gaseous NH₃ that needs to be liquefied in the second cooling step. This presents the advantage that the condensation temperature of the gaseous NH₃ rises, which simplifies condensation. Preferably the gaseous NH₃ pressure is increased to at least 1.5 MPa, more preferably 1.8 MPa or even higher, for example 2 MPa or more. This presents the advantage that the condensation temperature of NH₃ at the stated pressures exceeds the temperature level at which plant cooling water circuits usually operate. This preferred embodiment can readily be combined with the aforesaid preferred embodiments such as the application of partial condensation.

The ammonium carbamate solution being formed in the absorption section has an amount of NH₃ and NH₃-derived compounds such as ammonium ions, and an amount of CO₂ and CO₂-derived compounds such as carbamate- or carbonate ions. The weight ratio between these two amounts is expressed as the N/C ratio of the ammonium carbamate solution. In a further embodiment of the process according to the invention, the N/C ratio in the ammonium carbamate solution is reduced to 1.4 or less by returning a part of the discharged ammonium carbamate solution to the first cooling step and by subjecting the gaseous NH₃ and/or the mixture to a second, respectively third cooling step. Preferably, the N/C ration is reduced to 1.3 or less, more preferably to 1.25 or less, most preferably to 1.2 or less. In this embodiment, it is preferred that the third cooling step comprises a partial condensation step on the mixture as describer above, prior to the mixture being fed to the absorption section, with a liquid phase and a gas phase being formed. Preferably, the liquid phase is subsequently separated from the mixture. Advantageously, a part of the discharged gaseous NH₃ is liquefied in the second step and returned to the absorption section, as described above. Here, it is preferred as described above that a compression step is carried out on at least the part of the discharged gaseous NH₃ that is to be liquefied. The process according to the invention is elucidated on the basis of the following drawings.

In the drawings Figure 1 shows an embodiment with a cooling vessel in which the first cooling step is carried out, an absorption section consisting of an absorber, a condenser wherein the gaseous NH₃ is liquefied in the second cooling step and wherein the gaseous NH₃ and the ammonium carbamate solution are returned to the absorber and the cooling vessel, respectively.

Figure 2 shows an embodiment wherein, in comparison with the embodiment of Figure 1, the mixture from the first cooling step is first passed through a condenser, where the third cooling step is executed, before being fed to the absorber. Figure 3 shows an embodiment wherein, in comparison with the embodiment of Figure 2, the liquid phase is separated from the flow coming from the condenser placed between cooling vessel and absorber and is added to the ammonium carbamate solution coming from the absorber.

Figure 4 shows an embodiment wherein, in comparison with the embodiment of Figure 1 , the part of the flow of gaseous NH₃ from the absorber that needs to be liquefied is compressed in a compressor, prior to the liquefaction in the second cooling step.

Figure 5 shows an embodiment according to the state of the art. The first digit of the numbers in the figures is the same as the number of the figure. Where the last two digits of the numbers of different figures are the same, they refer to the same item.

In Fig. 1 a gaseous flow coming from a melamine synthesis reactor is fed via line 102 to cooling vessel 104 and cooled with a coolant consisting of an aqueous flow supplied via line 106 and an ammonium carbamate solution, to be discussed later, which is supplied via line 108. During cooling there are formed a melamine slurry, which is discharged via line 110, and a gaseous mixture containing NH₃, CO₂ and H₂O, which is discharged via line 112 to absorber 114. Absorber 114 is supplied with a flow of liquid NH₃ via line 116 as well as an auxiliary flow, consisting essentially of water, via line 118. It is possible to combine lines 116 and 118 into one line. Contacting the mixture with the liquid NH₃ and the auxiliary flow results in the formation of a flow of gaseous NH₃, which is discharged via line 120, and an ammonium carbamate solution, which is discharged via line 122. The ammonium carbamate solution discharged via line 122 is split: one part is removed via line 124, the other part is returned via line 108 to cooling vessel 104. The gaseous NH₃ discharged via line 120 is split: one part is removed via line 126 and generally used as fluidization gas and/or atomizing gas for the melamine synthesis reactor, the other part is supplied via line 128 to condenser 130. In condenser 130 the NH₃ is liquefied and added via line 132 to liquid NH₃ supplied via line 133, after which the liquid NH₃ is fed to absorber 114. The compounds that are not liquefied in condenser 130, such as N₂ and H₂, as well as a small quantity of NH₃, are discharged as an inert vent stream via line 134.

In Figure 2, in comparison with the embodiment of Figure 1 , the gaseous mixture containing NH₃, CO₂ and H₂O, which is discharged via line 212 from the cooling vessel 204, is fed to condenser 236. In condenser 236 partial condensation takes place so that a liquid phase and a gas phase are formed. The liquid phase and the gas phase are fed via line 238 to absorber 214.

In Figure 3, in comparison with Figure 2, a separator 340 is inserted between the condenser 336 and absorber 314. The liquid phase and the gas phase formed through partial condensation in condenser 336 are fed via line 338 to separator 340. The liquid phase is discharged via line 342 and combined with the ammonium carbamate solution discharged from absorber 314 via line 322. The combined flow is then discharged via line 344, after which the flow is split into a part that is fed to the cooling vessel and a part that is removed. The gas phase coming from the separator is fed to absorber 314 via line 346.

In Figure 4, in comparison with Figure 1 , the part of the discharged flow of gaseous NH₃ to be liquefied is fed via line 428 to compressor 448. The flow of compressed gaseous NH₃ is subsequently fed via line 450 to condenser 430, where it is liquefied. The increased pressure makes it easier to liquefy the NH₃, since the condensation temperature of NH₃ increases when the pressure is increased.

Figure 5 shows the state of the art without the presence of any means of liquefying a part of the flow of gaseous NH₃ and returning it to the absorber, and without any means of returning a part of the ammonium carbamate solution coming from the absorber to the cooling vessel. In addition a part of the flow of gaseous NH₃ discharged from absorber 514 via line 520 is discharged via line 552 to a scrubber unit in order to separate the inert compounds. The process according to the invention is elucidated further on the basis of an example and a comparative experiment. The example has been conducted according to the embodiment described in Figure 2. The comparative experiment has been conducted according to the embodiment of Figure 5. See Table 1 and Table 2 for the results. In the tables ammonium carbamate is not represented as such but as converted quantities of CO₂ and NH₃.

The results indicate that, with melamine-containing gaseous feed streams of equal quantity and composition (via 202 and 502) and with virtually equal quantities of removed CO₂ (via 224 and 524) and removed gaseous NH₃ (via 226 and 526), the quantity of NH₃ that is discharged per unit time via the ammonium carbamate solution (via 224 and 524) is significantly smaller in the example than in the comparative experiment (7 tonnes/hour and 9 tonnes/hour, respectively). As a result, steam consumption in downstream steps for liberating NH₃ from the removed ammonium carbamate solution drops from 15 tonnes/hour steam for the ammonium carbamate solution removed via 524, to 12 tonnes/hour for the ammonium carbamate solution removed via 224.

In addition the quantity of H₂O that is removed (via 224 and 524 respectively) is significantly lower in the example than in the comparative experiment (8.6 tonnes/hour and 13 tonnes/hour, respectively); this allows energy savings in utilizing the discharged CO₂ and NH₃ (for example for the synthesis of urea). Also the required quantity of liquid NH₃ that needs to be supplied in the example via 233 is significantly lower than the quantity of liquid NH₃ that needs to be supplied in the comparative experiment via 516 (3 tonnes/hour and 9 tonnes/hour, respectively).

Furthermore, the inert vent stream according to the invention which is discharged via 234 and which in this example contains between 0.001 and 0.1 tonne/hour inert compounds such as N₂ and H₂, contains only little NH₃ (0.02 tonne/hour) so that separating the inert compounds is accomplished much more easily in comparison with the treatment which is necessary in the comparative experiment for the flow that is discharged via line 552, which flow in relation to the quantity of inert compounds, which also in this comparative experiment is between 0.001 and 0.1 tonne/hour, contains very much NH₃ (5 tonnes/hour).

The results also indicate that the N/C ratio in the ammonium carbamate stream discharged from the absorption section according to the invention via 222 is 10/8, i.e. 1.25, which is significantly lower than the N/C ratio of the ammonium carbamate stream discharged from the absorption section in the comparative experiment via 522, which is 9/6, i.e. 1.5.

Table 1 - Results of the comparative experiment (see Fig. 5)

Flow 502 506 510 512 516 518 520 522 524 526 538 552

Melamine 5 0 5 0 0 0 0 0 0 0 0 0

NH₃ 28 0.9 0.9 28 9 0 28 9 9 23 28 5

C0₂ 6 0.3 0.3 6 0 0 0 6 6 0 6 0

H_zO 0 19 6 13 0 0.6 0.002 13.6 13.6 0.002 13 0

Total 39 20.2 12.2 47 9 0.6 28 28.6 28.6 23 47 5

[tonnes/h]

T [°C] 400 80 117 117 15 15 6 80 80 6 80 6 P [MPa] 0.6 0.6 0.6 1.6 1.6 0.5 0.5 0.5 0.5 0.5 0.5 Wt% gas 100 0 0 100 0 0 100 0 0 100 49 100

Table 2 - Results of the example (see Fig. 2)

Flow 202 206 208 210 212 216 218 220 222 224 226 228 233 234 23

Melamine 5 0 0 5 0 0 0 0 0 0 0 0 0 0

NH₃ 28 1 3 2 30 8 0 28 10 7 23 5 3 0.02 3

C0₂ 6 1 2 1 8 0 0 0 8 6 0 0 0 0

H₂0 0 14 3 6 11 0 0.6 0.003 11.6 8.6 0.003 0 0.6 0 1

Total 39 16 8 14 49 8 0.6 28 29.6 21.6 23 5 3.6 0.02 4

[tonnes/h]

T [°C] 400 80 74 112 112 29 29 7 74 74 7 7 21 7 P [MPa] 0.6 0.5 0.6 0.6 1.6 1.6 0.5 0.5 0.5 0.5 0.5 1.6 0. Wt% gas 100 0 0 0 100 0 0 100 0 0 100 100 0 100 4

ind H₂O are all present in a flow that consists of less than 100 wt% gas, said compounds are at least partly present in the urn carbamate solution.

Claims (9)

1. Process for preparing melamine, comprising a first cooling step from which a mixture containing NH₃, CO₂ and H₂O is released, wherein: • the mixture and a flow of liquid NH₃ are fed to an absorption section;

• the mixture and the flow of liquid NH₃ in the absorption section are contacted with each other, with gaseous NH₃ and an ammonium carbamate solution being formed;

• the gaseous NH₃ and the ammonium carbamate solution are separately discharged from the absorption section, characterized in that a part of the discharged ammonium carbamate solution is returned to the first cooling step, and that a part of the discharged gaseous NH₃ is liquefied in a second cooling step and returned to the absorption section.

2. Process according to claim 1, wherein the mixture, prior to being fed to the absorption section, is subjected to a third cooling step, wherein partial condensation takes place whereby a liquid phase and a gas phase are formed.

3. Process according to claim 2, wherein the liquid phase is separated from the mixture.

4. Process according to any one of claims 1 - 3, wherein a compression step is carried out on at least the part of the discharged gaseous NH₃ that is to be liquefied.

5. Process for preparing melamine, comprising a first cooling step from which a mixture containing NH₃, CO₂ and H₂O is released, wherein:

• the mixture and a flow of liquid NH₃ are fed to an absorption section;

• the mixture and the flow of liquid NH₃ in the absorption section are contacted with each other, with gaseous NH₃ and an ammonium carbamate solution being formed having an N/C ratio; • the gaseous NH₃ and the ammonium carbamate solution are separately discharged from the absorption section, characterized in that the N/C ratio in the ammonium carbamate solution is reduced to 1.4 or less by returning a part of the discharged ammonium carbamate solution to the first cooling step and by subjecting the gaseous NH₃ and/or the mixture to a second, respectively third cooling step.

6. Process according to claim 5, wherein the N/C ratio is reduced to 1.3 or less.

7. Process according to claim 5, wherein the N/C ratio is reduced to 1.2 or less.

8. Process according to claim 5, wherein the third cooling step comprises a partial condensation step on the mixture, prior to the mixture being fed to the absorption section, with a liquid phase and a gas phase being formed.

9. Process according to claim 8, wherein the liquid phase is separated from the mixture.

10 Process according* to claim 5 or 8, wherein a part of the discharged gaseous NH₃ is liquefied in the second cooling step and returned to the absorption section. 11. Process according to claim 10, wherein a compression step is carried out on at least the part of the discharged gaseous NH₃ that is to be liquefied in the second cooling step.