Catalytic Naphtha Research Articles

Production of paraffinic solvents

The low-boiling paraffinic solvents n-hexane and n-heptane are obtained from dearomatized catalytic reformer naphthas (raffinates) by fractionation and subsequent treatment to bring the content of unsaturated hydrocarbons down to the levels required for use in high-density polyethylene production, in the food industry, or in light industry. Proposes the natural adsorbent A-4M for use in treating paraffinic solvents. Compares 2 variants of the production of paraffinic solvents from catalytic reformer naphtha raffinate: variant I consists of treatment of the naphtha on the A-4M adsorbent, followed by fractionation; variant II consists of fractionation followed by treatment of the hexane (65-70 C) and heptane (92-100 C) cuts on the A-4M adsorbent. Finds that the treatment of the reformer raffinates on the A-4M adsorbent provides removal of the unsaturated hydrocarbons and the production of hexane and heptane solvents of the required quality. Recommends that in producing high-quality paraffinic solvents, it is more desirable to treat the hexane and heptane cuts separately than to treat the original catalytic reformer naphtha raffinate.

Selective separation and identification of olefins in petroleum and synthetic fuel naphtha

An analytical procedure, based on the specific and quantitative conversion of olefins to alcohols by the hydroboration-oxidation reaction, is described. The alcohols are subsequently separated from the hydrocarbon mixture by chromatography on alumina. The conversion was monitored by proton magnetic resonance (p.m.r.). A gas chromatograph interfaced with a quadrupole mass spectrometer (g.c.-m.s.) was used to identify the individual alcohols, using retention indices of pure compounds as well as library search data. The assignment of structures to the parent olefins is based on the stereochemistry of the hydroboration reaction. The procedure was applied to two synthetic fuel naphthas produced by thermal and catalytic processing of the Lloydminster heavy oil. The results indicate that the olefins are produced during processing. The olefins of the catalytic naphtha have predominantly higher average molecular weights ( C 7− C 10) than those of the thermal naphtha ( C 5− C 8). Chemical configurations have been assigned for 24 different olefins in both products. The hydroboration-oxidation procedure permits highly selective isolation of olefins in the form of alcohols and provides a pure alcohol mixture for identification by g.c.-m.s.

Effect of feedstock distillation range on yield and octane number of catalytic reformer naphtha

Effect of feedstock distillation range on yield and octane number of catalytic reformer naphtha

6 Development of mobil's kinetic reforming model

Mobil Research and Development has developed a kinetic process model for catalytic naphtha reforming which is currently used extensively throughout Mobil for commercial reformer monitoring, research guidance, new process designs, planning, and optimization. The experimental and mathematical development of Mobil's kinetic reforming model is presented in this paper.

Economic efficiency of recovery of n-paraffins from catalytic reformer naphtha raffinate

Economic efficiency of recovery of n-paraffins from catalytic reformer naphtha raffinate

Pyrolysis of naphtha-raffinate

1. Analysis of the hydrocarbon composition of a commercial sample of raffinate from catalytic reformer naphtha has shown that it consists of 88% paraffins, out of which about 52% consists of isoparaffins, including some 40% monosubstituted compounds. 2. The experiments at 850°C demonstrated that the optimal pyrolysis regime was obtained at this temperature with a corresponding contact time of 0.5 sec; gasification was 81.8%, ethylene yield 32.8%, and propylene yield 16.2% of feedstock weight. 3. After mathematical treatment of the experimental results, equations were derived for determining the ethylene and propylene yields as functions of temperature and contact time, these equations being applicable to this feed-stock with processing temperatures of 700–850°C and contact times of 0.3–1.1 sec. 4. On the basis of the yields of the desired olefinic hydrocarbons that were obtained in the high-temperature pyrolysis regime, this raffinate can be characterized favorably as a pyrolysis feedstock. The hydrocarbon composition of the raffinate is such that greater propylene yields can be obtained, and the ethylene and propylene regimes in effect coincide.

Catalytic Naphtha Reforming

Abstract During the past twenty years, the demand for high octane motor fuels has resulted in the installation of catalytic naphtha reforming capacity at a much higher rate than was forecasted by some of the

Surface-active products from oxidation of catalytic naphtha and subsequent sulfonation of the oxidation product

1. The processes of oxidation of catalytic cracking naphtha and sulfonating the oxidation products have been studied with the objective of preparing flotation agents. 2. Optimum oxidation conditions have been found: temperature, 130–135°C; duration, 7–9 h; catalyst, manganese naphthenate in an amount of 1% by wt.; air input, 3.5–4 liters/kg per min. 3. Optimum conditions of sulfonating the oxidate have been found: temperature during additon of sulfonating agent, 10–15°C; additional treatment at 28–30°C; time, 3 h; ratio of oxidate to sulfonating agent in sulfonation with 97–100% sulfuric acid, 1∶3; in sulfonation with oleum (13% free SO3), 1∶1 or 1∶1.5. 4. It has been shown that the water- and alkali-soluble components of oxidized catalytic naphtha (OCN) and their sulfonation products possess well-displayed surface-active properties, especially the sulfonation product of OCN with 97% sulfuric acid in a 1∶3 ratio. 5. The surface-active reagents obtained can be used successfully as collectors and foam-formers in flotation of lead-baryte, lead-zinc, or other ores, and can completely replace flotation oil foaming agent or DS in flotation of polymetallic ores.

Chloride Corrosion and Fouling In Catalytic Reformers With Naphtha Pretreaters

Abstract A study was made of chloride corrosion and fouling occurring in low-temperature sections of catalytic reformer naphtha pretreaters. These problems were related to corrosion by aqueous HCl-H 2 S-NH 3 solutions. Laboratory corrosion studies were made with these solutions to establish the effect of pH and composition in the presence or absence of an air atmosphere. Suppression of corrosion by ammonia neutralization and amine-type inhibitors also was studied. Elevated temperature tests were conducted in a nitrogen atmosphere. Field tests were made on six metals in a commercial pretreater reactor effluent stream. The removal of ammonium chloride fouling deposits was discussed briefly. 8.4.3, 4.3.2, 5.7.7, 3.3.2

Composition of Virgin, Thermal, and Catalytic Naphthas from Mid-continent Petroleum

Composition of Virgin, Thermal, and Catalytic Naphthas from Mid-continent Petroleum