PROCESS FOR THE PREPARATION OF AN AROMATIC HYDROCARBON MIXTURE

Abstract: The invention relates to a process for the preparation of an aromatic hydrocarbon mixture, wherein one or more monooelfins with two to four carbon atoms per molecule or aliphatic hydrocarbons, at least 50 %wt of which consisting of the said olefins, are contacted at a temperature of between 325 and 700°C with a catalyst containing a crystalline gallium silicate, which silicate has the following distinguishing features after calcination for one hour in air at 500 °C: (a) an X-ray powder diffraction pattern that contains as strongest lines the four lines listed in table A, TABLE A d(A) 11.1 ± 0.1 10.0 ± 0.1 3.84 ± 0.07 3.72 ± 0.06 and, (b) in the formula which gives the composition of the silicate expressed in moles of the oxides, the SiO₂/Ga₂O₃ mol. ratio is between 25 and 250, and wherein, if the silicate has a SiO₂/Ga₂O₃ mol. ratio of 100-250, the catalyst is subjected to a two-stage treatment comprising a first stage in which the catalyst is contacted for at least 15 minutes at a temperature of 350-700°C with a hydrogen-containing reducing gas, followed a second stage in which the catalyst is contacted for at least 15 minutes at a temperature of 350-700 °C with an oxygen-­ containing oxidizing gas. The relation between the C₅ ⁺ content and the aromatics content in the hydrocarbon mixture obtained is improved.

Description: PROCESS FOR THE PREPARATION OF AN AROMATIC HYDROCARBON MI=E The invention relates to a process for the preparation of an aromatic hydrocarbon mixture from mono-olefins with two to four carbon atoms per molecule or from aliphatic hydrocarbon mixtures, at least 50 wt.% of which consists of the said olefins. Mono-olefins with two to four carban atoms per molecule can be converted at a temperature of 325-700 C into aromatic hydrocarbon mixtures by contacting the olefins with a catalyst containing a crystalline aluminium silicate with a special structure. Such crystalline aluminium silicates are characterized by the fact that after calcination in air for one hour at 500 C they possess the following distinguishing features: a) an X-ray powder diffraction pattern containing as strongest lines the four lines listed in Table A, TABLE A d(A) 11.1 + 0.1 10.0 + 0.1 3.84 + 0.07 3.72 # 0.06 and, b) in the formula giving the composition of the silicate expressed in moles of the oxides, the SiO2/A1203 mol. ratio is 25-400. The above-mentioned process results in a product in which, besides the desired C5+ hydrocarbons, C4- hydrocarbons formed as byproducts also occur. The C5+ fraction present in the product is more valuable according as it has a higher aromatic content. Experimental research into the above-mentioned process has shown that the aromatic content of the C5+ fraction obtained depends to a large extent on the chosen reaction temperature and SiO2/Al2O3 mol. ratio of the crystalline silicate. According as a higher reaction temperature and/cr a crystalline silicate with a lower SiO2/Al2O3 mol. ratio is used in the process, a product is obtained whose C5+ fraction has a higher aromatic content. For both these treasures, he, the preparation of a duct whose C5+ fraction has a higher aromatic content is accompanied by a reduction in the yield of the C5+ fraction. The research shod that a particular relationship exists beteeen the in crese in the aromatic content of the C5 fraction and the reduction in the yield of the c5+ fraction, so that, in principle, for every aromatic content of the C5+ fraction being prepared, there is a particular potential yield of that C5+ fraction. This relationship is unfavourable to the extent that only low yields of C5 fractions with a relatively high aromatic content can be obtained. Since a possible application of the process on a commercial scale depends not only on the aromatic content of the C5+ fraction, but also on the potential yield of that C5+ fraction, there is a practical limit to the maximum + aromatic content of the Cg fraction being prepered, due to the fact that the corresponding yield of the C5+ fraction rmst still be acceptable. Purr research into this subject has now shown that considerably better results can be obtained in the above mentioned process if, as crystalline silicate with the previously mentioned special structure, a silicate containing gallium instead of aluminium is used, and if, moreover, the following two requirements are met: : a) in the formula giving the composition of the gallium silicate expressed in moles of the oxides, the SiO2/Ga2O3 mol. ratio should be 25-250, and b) if the gallium silicate has a SiO2/Ga2O3 mol. ratio of 100-250, the catalyst should be subjected one or more times to a two-stage treatment comprising a first stage in which the catalyst is contacted for at least 15 minutes at a temperature of 350-700 C with a hydroncontaining reducing gas, followed by a second stage in which the catalyst is contacted for at least 15 minutes at a temper- ature of 350-700 C with an oxygen-containing oxidizing gas. The research showed that in the case of the present crystalline gallium silicates corresponding with the previously mentioned crystalline aluminium silicates, the higher the reaction temperature and/or the lower the SiO2/Ga2O3 mol. ratio of the silicate employed, the higher the aromatic content of the C+ fraction of the product obtained, and also that for both + measures the preparation of a product whose C5 fraction has a higher aromatic content is accompanied by a reduction in the yield of the C5 fraction. For the crystalline gallium silicates there is also a relationship between the increase in the aromatic content of the C5+ fraction and the reduction in the yield of the C5+ fraction, whereby, in principle, for every aromatic content of the C5+ fraction being prepared there is a particular + potential yield of that C5 fraction. The important difference between the crystalline aluminium silicates and the present crystalline gallium silicates is that the previously mentioned relationship for the gallium silicates is considerably more favourable, so that considerably higher yields of C5 fractions with a relatively high aromatic content can be obtained than is the case for the aluminium silicates. Comparison of the results obtained fran a systematic investigation into processes for preparing aromatic hydrocarbons from a given feed, but employing a variety of aluminium silicates and gallium silicates at various temperatures showed that if the processes were aimed at the preparation of products whose C5+ fraction had a particular aromatic content, the gallium silicates gave a higher yield of the C5+ fraction, whereas if the processes were aimed at the preparation of products with a given content of the C5 fraction, the gallium silicates gave a C5+ fraction with a higher aromatic content. The present patent application therefore relates to a process for the ration of an aranratic hydrocarbon mixture, wherein one or more mono-olefins with two to four carbon atmos per molecule or aliphatic hydrocarbons, at least 50 %wt of which consisting of the said olefins, are contacted at a temperature Cf between 325 and 700 C with a catalyst containing a crystalline uiuii silicate, which silicate has the following distin- guishing feELures after calcination for one hour in air at 500 Oc: : a) an X-ray powder diffraction pattern that contains as strongest lines the four lines listed in Table A, and b) in the formula which gives the composition of the silicate expressed in moles of the oxides, the SiO2/Ga2O3 mol. ratio is between 25 and 250, and w rein, if the silicate has a SiO2/Ga2O3 mol. ratio of 100-250, the catalyst is subjected one or more times to the above-mentioned two-stage treatment. The staring material for the process according to the invention should be one or more mono-olefins having two to four carbon atoms per molecule or aliphatic hydrocarbons, at least 50 %wt of which consists of the said olefins. The mono-olefins with to to four carbon atoms per molecule, which should form at least 50 %wt of the feed, are ethylene, prcpylene, butylene-1, butylene-2 and iso-butylene. If a hydrocarbon is employed that in addition to the said C@ mono-olefins also contains other aliphatic hydrocarbons, these other hydrocarbons may be paraffins, di-olefins or C5+ mono-olefins. In the process according to the invention a feed is preferably employed which consists of at least 75 %wt and in particular substantially catpletely of one or more irm-olef ins with three or four carbon atoms per molecule. A very suitable feed for the present process is a hydrocarbon mixture consisting substantially of C3 and/or C4 monc-olefins, this mixture being obtained as byproduct of the catalytic or thermal cracking of hydrocarbons, in particular the steam cracking of lwdrocaobons for the preparation of ethylene. The e process according to the invention is preferably carried out at a temperature of 350-575 OC, a pressure of 1-20 bar and particularly 1-10 bar, and a space velocity of 0.1-10 kg.kg -1 and in particular of 0.5-5 kg.kg Ú.hour-1 In the process according to the invention the feed is contacted with a catalyst containing a crystalline gallium silicate defined amongst other things by the X-ray powder diffraction pattern of the silicate after calcination for one hour in air at 500 OC. This should contain as strongest lines the four lines given in Table A. The complete X-ray powder diffraction pattern of a typical example of the present crystalline gallium silicates after calcination for one hour in air at 500 C is represented in Table B. TABLE B d(A) Rel. int. d(A) Bel. int. 11.1 100 3.84 (D) 57 10.0 (D) 70 3.72 (D) 31 8.93 1 3.63 16 7.99 1 3.47 < 1 7.42 2 3.43 5 6.68 7 3.34 2 6.35 11 3.30 5 5.97 17 3.25 1 5.70 7 3.05 8 5.56 10 2.98 11 5.35 2 2.96 3 4.98 (D) 6 2.86 2 4.60 4 2.73 2 4.35 5 2.60 2 4.25 7 2.48 3 4.07 2 2.40 2 4.00 4 (D) = doublet Suitable catalysts for use in the process according to the invention are those containing a crystalline gallium silicate with a B2.{Ga203 mol. ratio of 25-250. If the crystalne gallium silicate has a SiO2/Ga2O3 mol. ratio of 100-250, it should be subjected one or more times to the above-described two-stage treatment. Although crystalline gallium silicates with a SiO2/Ga2O3 mol. ratio of less than 100 are suitable as such for use in the process according to the invention, they are also preferably subjected one or more times to the above-described two-stage treatment. In the prowess according to the invention, preferred crystalline gallium silicates have a SiO2/Ga203 mol. ratio of 60-220. When employing a crystalline gallium silicate with a maximum SiO2/Ga203 mol. ratio of 110, the twc-stage treatment is preferably not performed more than three times. When employing a crystalline gallium silicate with a SiO2/Ga203 mol. ratio of more than 110, but not more than 130, the twc- stage treatment is preferably performed at least three times, but not more than ten times. When employing a crystalline gallium silicate with a SiO2/Ga203 mol. ratio of more than 130, but not more than 220, the silicate is preferably first suo- jected to calcination at a temperature of 600-1000 OC, after which the tsc-stage treatment is performed on it at least three times, but not more than ten times. During the first stage of the two-stage treatment the catalyst should be contacted for at least 15 minutes at a temperature of 350-700 C with a hydrogen-containing reducing gas. The e first stage of the two-stage treatment can in principle be performed in two ways. In the first place the hydrogen- containing reducing gas can be fed to the catalyst from outside. In that case a gas is preferably employed that contains at least 20 vol.% and in particular at least 40 vol.% hydrogen. The gas employed can very suitably contain, besides hydrogen, either mainly nitrogen or mainly carbon monoxide or mainly C4 hydrocarbons. Suitable gases which, besides hydrogen, contain mainly carbon monoxide can be obtained as synthesis gas from a highly carbonaceous material, such as coal, by gasification, or fran light hydrocarbons, such as natural gas, by steam reforming or partial oxidation. Suitable gases which, besides hydrogen, contain mainly C4 hydrocarbons can be obtained as byproduct from the catalytic conversion of hydrocarbons in the presence of hydrogen, such as cracking, isomerization and reforming. In the second place the hydrogen-containing reducing gas can be produced in situ by contacting the catalyst for a maximum of five hours with a hydrocarbon or a hydrocarbon mixture. A very suitable hydrocarbon or hydrocarbon mixture would in this case be the feed employed in the present process. In the second stage of the two-state treatment the catalyst should be contacted for at least 15 minutes at a temperature of 350-700 C with an oxygen-containing oxidizing gas. The gas employed preferably contains at least 5 vol.% and in particular at least 10 vol.% oxygen. The second stage can very suitably be performed using a gas which, besides oxygen, contains either mainly nitrogen ar otherwise mainly nitrogen, carbon monoxide and carton dioxide. A suitable gas that, besides oxygen, ccntains mainly nitrogen is air. Suitable gases which, besides oxygen catain mainly nitrogen, carbon monoxide and carbon dioxide are offgases oeaened during the remeeal of carbon by means of an excess of air from deactivated hydrocarbon con- version catalysts. Preferably, the two stages of the two-stage treatment are performed at a temperature of 400-650 C and in particular at a temperature of 475-575 OC. It is also preferable that the two stages be performed at the same temperature. The crystalline gallium silicates employed in the process according to the invention can very suitably be prepared from an aqueous mixture containing the following compounds: one or more compounds of an alkali iretal (M), one or more organic nitrogen compounds (RN) containing an organic cation or from which an organic cation is formed during the preparation of the silicate, one or more silicon compounds and one or more gallium compounds. preparation is effected by maintaining the mixture at an elevated temperature until the silicate has been formed and then separating the silicate crystals from the mother liquor and washing, drying and calcining the crystals. The aqueous mixture fran which the silicates are prepared should contain the various compounds in the following molar ratios, except for the organic nitrogen compounds, expressed in moles of the oxides: : : SiO2 = 0.01-0.35, RN : : SiO2 = 0.02-1.0, SiO2 : Ga203 = 25-400, and H2O : SiO2 = 5-65. The silicates can very suitably be prepared from a basis mixture containing a quaternary ammonium caround as organic nitrogen ccnqxxund, a sodium catpound as alkali natal compound and amorphous silica as silicon catpocnd. The silicates prepared according to the above method contain alkali metal ions. By means of suitable exchange techniques these can be replaced by other cations, such as hydrogen ions or ammonium ions. The crystalline gallium silicates employed in the process according to the invention preferably have an alkali metal content of less than 0.05 wt. In the process according to the invention the crystalline gallium silicates can be used as such or in combination with a binding material, such as kaolin or bentonite. The invention will now be illustrated with the aid of the following example. EXAMPLE Two crystalline aluminium silicates (silicates 1 and 2) and three crystalline gallium silicates (silicates 3-5) were prepared by heating mixtures of NaOR, amorphous silica, (C3H7)4NOH and either Al(NO3)3, or Ga(NO3)3 in water in an autoclave under autogenous pressure for 24 hours at 150 OC. After the reactants had cooled down, the resulting silicates were filtered off, washed with water until the pH of the wash water was about 8, and dried at 120 OC. After calcination for one hour in air at 500 OC, silicates 1-5 had the following properties: a) an X-ray powder diffraction pattern corresponding such stantially with that given in Table B, and b) a value for the SiO2/A1203 or SiO2/Ga203 mol. ratio as given in Table C. TABLE C Silicate No. SiO2/Al2O3 mol. SiO2/Ga2O3 mol. ratio ratio 1 77 2 250 3 - 70 4 - 130 5 350 Fran silicates 1-5 were prepared silicates I-V by boiling silicates 1-5 with 1.0 molar NH4NO3 solution, washing with water, again boiling with 1.0 molar NE4N03 solution, and washing, drying at 120 C and calcining at 500 OC. Samples of silicates III-V were repeatedly subjected to a two-stage treatment comprising a first stage in which the silicate was contacted for 30 minutes with n-butane at a temperature of 550 C, a pressure of 1.5 bar and a space velocity of 8 g.g-1.hour-1, followed by a second state in which the silicate was contacted for one hour with air at a temperature of 550 C and a pressure of 1.5 bar. By performing this stage treat iaent three times on silicate Ill and ten times on silicates IV and V, silicates IIIA-VA were obtained from silicates III-V respectively. Silicates I, II, IIIA, IV, IVA and VA were tested in twelve experiments (experiments 1-12) for the preparation of C5 fractions from iso-butylene (experiments 1-11) and from propylene (experiment 12). All experiments were performed at a pressure of 1.5 bar and a space velocity of 2 kg.kg-1.hour-1 in a reactor containing a solid catalyst. Conversion of the feed was practically complete in all the experiments. The tempera tures at which the experiments were carried out and the results of these experiments are given in Table D. Of experiments 1-12, only experiments 5-7, 9 and 12 are experiments according to the invention. The other experiments fall outside the scOpe of the invention. They are included in the patent application for the purpose of comparison. No crystalline gallium silicate was used in the comparative epperi- menus 1-4. In the comparative experiments 8, 10 and 11, despite the fact that a crystalline gallium silicate was used, the results were nevertheless unsatisfactory, the reasons being that the silicate was not pre-treated in experiment 8, the reaction temperature was too low in experiment 10, and the gallium silicate had a too high SiO2/Ga203 mol. ratio in experiment 11. A comparison of experiment 7 (with gallium silicate) and experiment 3 (with aluminium silicate) shows that for an equal yield of C5+ fraction (63 %wt) the gallium silicate produces a C5+ fraction with a rtuch higher aromatic content (83 %wt) than the aluminiiin silicate (48 %wt). A carparison of experiment 7 (with gallium silicate) and experiment 4 (with aluminium silicate) shows that for an almost identical aromatic content of the C5+ fraction (81-83 wt%) the gallium silicate gives a much higher yield of C5+ fraction (63 %wt) than the aluminium silicate (38 %wt). This was also shown by a comparison of experiments 5 and 3. TABLE D EMI12.1 Experiment <SEP> No. <SEP> 1 <SEP> 2 <SEP> 3 <SEP> 4 <SEP> 5 <SEP> 6 <SEP> 7 <SEP> 8 <SEP> 9 <SEP> 10 <SEP> 11 <SEP> 12 <tb> Silicate <SEP> No. <SEP> II <SEP> I <SEP> II <SEP> II <SEP> IIIA <SEP> IIIA <SEP> IIIA <SEP> IV <SEP> IVA <SEP> IIIA <SEP> VA <SEP> IIIA <tb> Temperature, <SEP> C <SEP> 400 <SEP> 400 <SEP> 450 <SEP> 575 <SEP> 350 <SEP> 425 <SEP> 550 <SEP> 425 <SEP> 425 <SEP> 315 <SEP> 500 <SEP> 550 <tb> Yield <SEP> of <SEP> C4fraction, <SEP> %wt <SEP> 16 <SEP> 37 <SEP> 37 <SEP> 62 <SEP> 28 <SEP> 33 <SEP> 37 <SEP> 36 <SEP> 30 <SEP> 3 <SEP> 67 <SEP> 39 <tb> Yield <SEP> of <SEP> C5+ <tb> fraction, <SEP> %wt <SEP> 84 <SEP> 63 <SEP> 63 <SEP> 38 <SEP> 72 <SEP> 67 <SEP> 63 <SEP> 64 <SEP> 70 <SEP> 97 <SEP> 33 <SEP> 61 <tb> Aromatic <SEP> content <SEP> of <tb> C5+ <SEP> fraction, <SEP> %wt <SEP> 19 <SEP> 49 <SEP> 48 <SEP> 81 <SEP> 48 <SEP> 65 <SEP> 83 <SEP> 48 <SEP> 52 <SEP> 2 <SEP> 11 <SEP> 85 <tb>

Claims: CLAIMS 1. Process for the preparation of an aromatic hydrocarbon mixture, characterized in that one or more olefins with two to four carbon atoms per molecule or aliphatic hydrocarbons, at least 50 %wt of which consisting of the said olefins, are contacted at a temperature of between 325 and 700 C with a catalyst containing a crystalline gallium silicate, which silicate has the following distinguishing features after calcination for one hour in air at 500 OC: : a) an X-ray powder diffraction pattern that contains as strongest lines the four lines listed in Table A, and b) In the formula which gives the composition of the silicate expressed in moles of the oxides, the SiO2/Ga2O3 mol. ratio is between 25 and 250, and that, if the silicate has a SiO2/Ga203 mol. ratio of 100-250, the catalyst is subjected one or more times to a tsc-stage treatment comprising a first stage in which the catalyst is contacted for at least 15 minutes at a temperature of 350-700 C with a hydrogen-containing reducing gas, followed by a second stage in which the catalyst is contacted for at least 15 minutes at a temperature of 350-700 C with an oxygen-containing oxidizing gas. 2. Process according to claim 1, characterized in that it is applied to a feed, 75 wt of which consists of one or more mono-olefins with three or four carbon atoms per molecule. 3. Process according to claim 2, characterized in that the feed consists substantially completely of one or more mono- olefins with three or four carbon atoms per molecule. 4. Process according to claim 3, characterized in that the feed is a hydrocarbon mixture consisting substantially of C3 and/or C4 mono-olefins, this mixture being obtained as byproduct of the catalytic or thermal cracking of hydrocarbons. 5. Process according to one of claims 1-4, characterized in that it is carried out at a pressure of 1-20 bar and a space velocity of 0.1-10 kg.kg-1.hour-1. 6. Process according to one of claims 1-5, characterized in that a crystalline gallium silicate is used with a SiO2/Ga2O3 mol. ratio of 60-220. 7. Process according to one or more of claims 1-6, characterized in tbat the crystalline gallium silicate is prepared from an aqueous mixture containing the following compounds: one or more ccoooands of an alkali metal (N), one or more organic nitrogen compounds (RN) containing an organic cation or from which an organic cation is formed during the preparation of the silicate, one or more silicon compounds and one or more gallium compounds, and in which mixture the various compounds are present in the following molar ratios, except for the organic nitrogen compounds, expressed in moles of the oxides: : : SiO2 = 0.01-0.35, RN : SiO2 = 0.02-1.0, SiO2 : Ga2O3 = 25-400, and H2O : SiO2 = 5-65 by maintaining the aqueous mixture at an elevated temperature until the silicate has been formed and then separating the silicate crystals from the mother liquor and calcining them. 8. Process according to one of claims 1-7, characterized in that the crystalline gallium silicate has an alkali metal content of less than 0.05 %wt.

Inventors: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.
Applicants: SHELL INTERNATIONALE RESEARCH MAATSCHAPPIJ B.V.
Application year: 1985
Main classification: C07C2
IPC codes: C07C2, C07C15, B01J29, C01B39, C10G35, C07C1, C01B33, C07B61, C07C67