DE1618294B2 - - Google Patents

Description

rich dehydrocyclization products with a

the ratio of SiO ₂ to alkali oxide is 1: 2 to 1: 4 improved modified aluminum oxide-chromium and that the catalyst may carry out oxide-catalyst,
after fatigue by soaking with a water- This task is carried out by the above

rigen solution of KOH, NaOH, K ₂ Cr ₂ O ₇ or as the method shown in claim solved.
Chromic acid and potassium aluminate in one amount, depending on the composition of the ingredients

which corresponds to about 50% of the bulk volume of the catalyst raw materials rich in aromatic to almost pure aromatic •, drying at 100 ⁰ C and calcining fractions with about 50 to over 90 percent by weight while maintaining the above aromatic compounds in the liquid product with a SiO ₂ substitution, have been reactivated is. Catalysts containing 30 very low levels of fission gas

from about 10 to 15 percent by weight, the cracked gas consisting of about 95% hydrogen on average and thus forms a high quality by-product. For the unexpectedly high aromatic yields at unge-35 comfortably high contact loads is that of the

known comparable contacts differing

The composition of the catalyst is decisive. Noticeable deviations from the given ratios lead to a reduction in activity. In particular, 40 causes the SiOj proportion to be exceeded or ₍ a reduction in the SiO ₂ -K ₂ O ratio a

The invention relates to a process for increased dehydrogenation at the expense of dehydrocyclization. The listed catalyst stands out despite the

Hydrogen with 6 to 10 carbon atoms with a relatively low SiO ₂ content due to high abrasion-use of aluminum oxide-chromium oxide Kataly- 45 strength, which makes it particularly suitable for Wandersat oren. bed and fluidized bed processes are suitable; Furthermore, the dehydrocyclization of hydrocarbons has a high thermal stability and long mixtures in the range of C ₈ to C ₁₀ in terms of modified life. It tolerates a high number of Regene-Aluminum-Oxide-Chromoxid-catalysts is principally with hardly noticeable decrease in activity.
well known. It works under normal pressure 50. The total conversion per catalyst used or overpressure at temperatures between 500 and quantity can be increased if one ^{reaches the catalyst, which is exhausted in the de-600 0} C and on the one hand to gasoline increased hydrocyclization process, knock resistance, with an aromatics recovery only by one Treatment with KOH, NaOH, K ₂ Cr ₈ O ₇ , by extraction is possible. K ₂ CrO ₄ or chromic acid and potassium aluminate react on the other hand, corresponding processes are known, 55 activated and used repeatedly. The catalyst with one or more content, which leads directly to fractions with a high aromatic content, is treated. The catalysts of the specified components used for this purpose contain predominantly / 3-trihydrate as a carrier. This amount of water, which has about 50% of the bulk volume of the catalyst but corresponds, as experience shows, to the catalyst to be impregnated, dries with insufficient thermal stability and 60 about 100 ^° C. and then calcines for 4 hours with inadequate abrasion resistance, which has its universal 450 ^° C. With this re-impregnation, the ratios given prior to use in moving bed reactors must not be exceeded or prevented. To increase the abrasion resistance When the process is carried out continuously with a catalyst of aluminum oxide-chromium oxide catalysts, the circulation of the regenerated catalyst is known in each case with the incorporation of silicon dioxide. 65 such quantities are fed to the reactor, In processes with known catalysts results in that in the reactor in the reduction of Cr ⁴⁺ to the content of SiO _2, to a reduction of the activated Cr ³ + water liberated in this one Partialvität a increased occurrence of cracked products pressure of 1.5 to 6 Torr. This is not necessary

1 618 291

continuation

example Chlorofluorine
alkane Amine-based polyol Delay
middle lot
(%) Visc
(at;
original
solution jsity
5 ° C)
after
4 weeks
at 50 ° C fa
original
solution beet
after
4 weeks
at 50 ° C i-g CCl ₃ F the same the same 2 810 850 G-I G-12 1-h CCl ₃ F the same the same 3 820 840 G-I G-12 1-i CCl ₃ F ' the same the same 5 830 840 G-I G-12 i-j CCl ₃ F the same the same 7th 820 850 G-I G-12 control CCl ₃ F the same - 0 810 4500 G-I > G-18 2-a C ₂ Cl ₃ F ₃ Ν, Ν, Ν ', Ν'-tetrakis-
2-hydroxypropyl
ethylenediamine the same 0.05 520 1500 G-I > G-18 2 B C ₂ Cl ₃ F ₃ the same the same 0.08 540 1300 G-I G-18 2-c C ₂ Cl ₃ F ₃ the same the same 0.1 520 1020 G-I G-17 2-d C ₂ Cl ₃ F ₃ the same the same 0.3 530 650 G-I G-12 2-e C ₂ Cl ₃ F ₃ the same the same 0.5 540 600 G-I G-Il 2-f C ₂ Cl ₃ F ₃ the same the same 1 520 610 G-I G-10 2-g C ₂ Cl ₃ F ₃ the same the same 2 530 590 G-I G-10 2-h C ₂ Cl ₃ F ₃ the same the same 3 530 600 G-I G-10 2-i C ₂ Cl ₃ F ₃ the same the same 5 540 580 G-I G-10 2-j C ₂ Cl ₃ F ₃ the same the same 7th 530 600 G-I G-10 control C ₂ Cl ₃ F ₃ the same the same 0 530 2900 G-I > G-18 3-a CCl ₃ F Ν, Ν, Ν ', Ν'-tetrakis-
2-hydroxyethyI-
ethylenediamine the same 0.05 550 2400 G-I > G-18 3-b CCl ₃ F the same the same 0.08 540 1300 G-I G-17 3-c CCl ₃ F the same the same 0.1 560 930 G-I G-15 3-d CCl ₃ F the same the same 0.3 550 610 G-I G-10 3-e CCl ₃ F the same the same 0.5 540 590 G-I G-9 3-f CCl ₃ F the same the same 1 550 570 G-I G-9 3-g CCl ₃ F the same the same 2 550 590 G-I G-8 3-h CCl ₃ F the same the same 3 530 580 G-I G-8 3-i CCl ₃ F the same the same 5 540 580 G-I G-8 3-j CCl ₃ F the same the same 7th 540 570 G-I G-8 control CCl ₃ F the same the same 0 550 3000 G-I > G-18 4-a CCl ₃ F Ν, Ν, Ν ', Ν'-tetrakis-
2-hydroxypropyl
ethylenediamine the same 0.05 540 2400 G-I > G-18 4-b CCl ₃ F the same the same 0.08 530 1300 G-I G-18 4-c CCl ₃ F the same the same 0.1 520 1030 G-I G-18 4-d CCl ₃ F the same the same 0.3 530 640 G-I G-12 4-e CCl ₃ F the same the same 0.5 550 600 G-I G-ii 4-f CCl ₃ F the same the same 1 540 580 G-I. G-10 4-g CCl ₃ F the same the same 2 540 590 G- G-10 4-h CCl ₃ F the same the same 3 530 590 G- G-10 4-i CCl ₃ F the same the same 5 530 580 G- G-10 4-j CCl ₃ F the same the same 7th 550 590 G- G-10 control CCl ₃ F the same the same 0 520 3200 G- > G-18 \ 5-a
Comparison) CCl ₃ F the same Hydro
chinone 1 530 3200 G-I > G-18 I.

1 618 291

continuation

example Chlorofluorine
alkane Amine-based polyol Delay
middle lot
(%) Viscx
(at 2
original
solution isity
5 ° C)
after
4 weeks
at 50 ° C fa
original
solution beet
after
4 weeks
at 50 ⁰ C 5-b
(Comparison) CCl ₃ F the same the same 5 520 3100 G-I > G-18 6-a
(Comparison)
6-b
(Comparison) CCl ₃ F
CCl ₃ F the same
the same p-allyl
toluene
the same 1
5 530
520 3300
3200 GI
GI > G-18
> G-18

Patent claims:

1. Chlorofluoroalkane composition that opposes the reaction with amino group-containing polyols is stable, consisting of trichlorofluoromethane and / or trichlorotrifluoroethane and 0.1 to 5 percent by weight p-Isopropenyholuene, based on the weight of the chlorofluoroalkane or the chlorofluoroalkanes.

2. chlorofluoroalkane composition according to claim 1, characterized in that the p-isopropenyltoluene is contained in an amount of 0.2 to 2 percent by weight.

Claims (1)

1 2 and increased carbon deposition on the Patentansoruoh ·? ^ata ' ^y ' ^at _f ^Or · ^Experiment * «« to the carbon deposit Claim. _by adding diluents such as water substance or inactive gases within reasonable limits Process for the dehydrocyclization of non-5 and thus the running time of the catalyst to or predominantly non-aromatic hydrocarbons extend, so one must have an impaired product with 6 to 10 carbon atoms with or and a correspondingly reduced contact load without diluent at 500 to 600 ⁰ C below accept. Furthermore, the tired catalyzer normal or overpressure with Raumgeschwindig- saloren for the dehydrocyclisierungsprozess are unusable above 0.5 in the fixed or moving bed in 10 bar and must be replaced by new active contact presence of modified aluminum oxide. Chromium oxide catalysts, thereby The invention pursues the purpose of aromatics indicates that the catalyst consists of highly enriched fractions at high volume velocities to win, taking a burden 10 to 20 percent by weight of Cr ₃ O ₃ , ^l * of the process avoided by diluents can be and the per unit of quantity of the 1 to 5 percent by weight SiO ₂ , used catalyst, achieved amount of higher quality 2 to 10 percent by weight alkali oxide and reaction products is increased significantly. "., _,, The invention is therefore based on the object 60 to 90 percent by weight of Al ₂ O ₃ , _{ao said} method of producing aromatics