Martin Bajus

Etherification of glycerol with tert-butyl alcohol catalysed by ion-exchange resins

The reaction of glycerol with tert-butyl alcohol in the liquid phase on acid Amberlyst-type ion-exchange resins was studied. The influence of temperature, mole ratio n(TBA)/n(G), water and swelling of gel, and macroreticular type of polymer catalysts on etherification reaction was investigated. The most favourable reaction temperature is 75°C. The conversion of glycerol and yield of glycerol tert-butyl ethers has increased with the mole ratio n(TBA)/n(G). Dry form of macroreticular catalysts provided the best results. Etherification reaction of glycerol with isobutylene in non-aqueous conditions gives the highest yield of desired ethers. The influence of water was studied. The gel forms of ion-exchange resins have very low catalytic activity. It can be concluded that water has an inhibition effect on ion-exchange resins. By comparing the gel and macroreticular forms of Amberlyst ion-exchange resins it can be concluded that very acid forms of macroreticular ion-exchange resins with a high degree of crosslinking are more active catalysts for the studied reaction due to their pores which are sufficiently large so that the voluminous tert-butyl ethers of glycerol can be formed. It was estimated that tert-butyl alcohol as tert-butylation agent is not suitable for etherification of glycerol with the formation of di-and triethers.

Separation and Characterization of Products from Thermal Cracking of Individual and Mixed Polyalkenes

Low-density polyethylene (LDPE), polypropylene (PP), and their mixture in the mass ratio of 1: 1 (LDPE/PP) were thermally decomposed in a batch reactor at 450°C. The formed gaseous and oil/wax products were separated and analyzed by gas chromatography. The oils/waxes underwent both atmospheric and vacuum distillation. Densities, molar masses and bromine numbers of liquid distillates and distillation residues were determined. The first distillate fraction from the thermally decomposed LDPE contained mostly linear alkanes and alk-1-enes ranging from C6 to C13 (boiling point up to 180°C). The second distillate fraction was composed mostly of hydrocarbons C11 to C22 (boiling point up to 330°C). 2,4-Dimethylhept-1-ene was the major component of the first distillate fraction obtained from the product of PP decomposition, while in the 2nd distillate fraction it was 2,4,6,8-tetramethylundec-1-ene. The yields of some gaseous or liquid hydrocarbons obtained by distillation from thermally degraded LDPE/PP differed from the values corresponding to the decomposition of individual plastics due to the mutual influence of polyalkenes during their thermal cracking. Similarly, the yields of propene and methylpropene in the gaseous phase were higher in the case of mixture. Whereas the content of C9 to C17 alkanes and alkenes in the distillates separated from the liquid mixture obtained by the decomposition of LDPE/PP decreased, the formation of 2,4,6,8,10,12-hexamethylpentadec-1-ene remained unchanged. The corresponding mechanisms of thermal cracking were discussed.

The use of carbon catalysts and of nitrous oxide in promoting the conversion of methane

Abstract This paper reports on the coupling of methane to C 2 and higher hydrocarbons over a carbon catalyst in the absence and presence of nitrous oxide and a lithium-promoted carbon catalyst in the absence and presence of nitrous oxide. The kinetics of the methane conversion were studied in a flow system over the temperature range 700–1100°C. At 850°C the conversion of methane was increased by a factor of about 800 in the presence of the carbon catalyst. The selectivity to C 2 hydrocarbons was, however, low and the main products were hydrogen and carbon. The Li/carbon catalyst was similarly effective and led to a better selectivity for C 2 hydrocarbons. Nitrous oxide had a strong promoting effect on the homogeneous coupling of methane but a less noticeable effect in the presence of the catalysts. Nitrous oxide improved the selectivity to C 2 hydrocarbons. Under the conditions of the present experiments the carbon-lithium oxide catalyst is able to facilitate the oxidative coupling of methane to give 36% conversion with selectivity to C 2 hydrocarbons over 70%.

Kinetics and modelling of heptane steam-cracking

The kinetics and product distribution during the cracking of heptane in the presence of steam were investigated. The experiments were performed in a flow reactor under atmospheric pressure in a temperature range of 680–760°C with a mass ratio of steam to heptane of 3: 1. The overall decomposition of heptane is represented by a first-order reaction with activation energy of 249.1 kJ mol−1 and a frequency factor of 3.13 × 1013 s−1. The reaction products were analysed using gas chromatography, the main product being ethylene. The molecular reaction scheme, which consists of a primary reaction and 24 secondary reactions between primary products, was used for modelling the experimental product yields. The yields of ethylene and hydrogen were in good agreement; however the experimental yields of propylene were higher than the predicted yields.

Fuels obtained by thermal cracking of individual and mixed polymers

Utilization of oils/waxes obtained from thermal cracking of individual LDPE (low density polyethylene), HDPE (high density polyethylene), LLDPE (linear low density polyethylene), PP (polypropylene), or cracking of mixed polymers PP/LDPE (1: 1 mass ratio), HDPE/LDPE/PP (1: 1: 1 mass ratio), HDPE/LDPE/LLDPE/PP (1: 1: 1: 1 mass ratio) for the production of automotive gasolines and diesel fuels is overviewed. Thermal cracking was carried out in a batch reactor at 450°C in the presence of nitrogen. The principal process products, gaseous and liquid hydrocarbon fractions, are similar to the refinery cracking products. Liquid cracking products are unstable due to the olefins content and their chemical composition and their properties strongly depend on the feed composition. Naphtha and diesel fractions were hydrogenated over a Pd/C catalyst. Bromine numbers of hydrogenated fractions decreased to values from 0.02 g to 6.9 g of Br2 per 100 g of the sample. Research octane numbers (RON) before the hydrogenation of naphtha fractions were in the range from 80.5 to 93.4. After the hydrogenation of naphtha fractions, RON decreased to values from 61.0 to 93.6. Diesel indexes (DI) for diesel fractions were in the range from 73.7 to 75.6. After the hydrogenation of diesel fractions, DI increased up to 104.9.

Pyrolysis of high-boiling product fractions from petroleum vacuum distillate hydrocracking

Abstract A high-boiling product from petroleum vacuum distillate hydrocracking was used as a feedstock for pyrolysis to light alkenes. The high boiling product was distilled to yield five fractions. Pyrolysis of these fractions was performed in a laboratory pyrolysis apparatus. The fractions pyrolysed were analyzed by a procedure consisting of their separation by liquid adsorption chromatography and subsequent characterization of the chromatographic fractions obtained by elemental analysis, vapour pressure osmometry, 1 H and 13 C NMR spectrometry and mass spectrometry. In this way the relation between the chemical structure and composition of the pyrolysed fractions and the yield of light alkenes was obtained. It was found that the fraction of the high-boiling product boiling above 486°C was not a suitable pyrolysis feedstock even if its BMC index was good; this fraction had a low alkane content.