Preliminary oil separation

Z 6 Physicochemical purification of effluents from preliminary oil separators... [Pg.80]

Porter and Lammerink (1994) studied the density of coriander essential oil over the temperature range 20 to 60°C. The density of the oil decreased as temperature increased. There was some variation between oils in the temperature coefficients with the change in density. The density differentials between oil and water and their temperature coefficients varied markedly between different oils. A preliminary separation coefficient is used to indicate the effect of oil density and condensate water viscosity on oil separation at different temperatures. Separation of less dense oils with small differentials would benefit more from increased temperatures than less dense oils with large differentials (C. sativum). It was necessary to use both density and viscosity data to determine whether temperature control of a separator was required to obtain efficient separation of an oil from the condensate stream following steam distillation. [Pg.195]

Fast pyrolysis of pine sawdust in a small vortex reactor operating at 10 to 20 kg/h and 480 to 520 °C produces high yields of primary pyrolysis oils (over 55% by weight on a dry basis). The vortex reactor transmits very high heat fluxes to the sawdust, causing primarily depolymerization of the constituent polymers into monomers and oligomers. A preliminary scheme separates the raw oils into a carbohydrate-derived aqueous fraction and a phenolic-rich ethyl acetate (EA) soluble fraction. The EA fraction is washed with water and with aqueous sodium bicarbonate to remove acids yielding 20% to 25% of the feed as phenols and neutrals (P/N) in the EA solution. [Pg.138]

This type of clarifier is used in applications such as preliminary oil-water separations in refineries and clarification of waste streams in steel mills. When multiple units are employed, common walls are possible, reducing construction costs and saving on floor space. Overflow clarities, however, generally are not as good as with circular clarifiers, due primarily to reduced overflow weir length for equivalent areas. [Pg.74]

The pressure extraction system (see Fig. 5.1) is operated as follows. The quantity of petroleum from each oil well (produced with the natural layer pressure) is serially measured using an automatic group measurement unit. Then, the petroleum from various oil wells in the field is transported to the local separation station. The quantity of the petroleum from the oil wells is measured after the preliminary gas separation with the centrifugal separator. After that, the petroleum and gas are directed to a local separation unit, where gas is separated from the petroleum by the first stage separator at the pressure 4—5 bar and then directed to the gas processing station. Petroleum with layer water and solved gases will be pumped to the central processing station, where the second step of separation... [Pg.231]

Nowadays, entrainment traps with string orifices are adopted. The vertical mesh orifice can be used as the section for final separation of liquid drops (Fig. 2.12, a), or to carry out preliminary separation and droplet coagulation (Fig. 2.12, b). In the latter case, the final separation of droplets is achieved in a horizontal mesh installed before the gas output branch pipe. In some gravitational gas-oil separators, the gas-liquid stream is directed toward a special reflector called a deflector (or baffle). The wall of the vertical separator can also act as a baffle. As a result of an impact of the liquid-gas mixture against the obstacle, the initial separation of gas from liquid occurs. To ensure smooth flow of liquid without foaming, separators are provided with a series of horizontal and inclined surfaces -shelves, cones, or hemispheres. [Pg.25]

The hyphenation of LC-GC systems to mass spectrometric detectors has also been reported for the analyses of neroli [142], bitter and sweet oranges, lemon, and petitgrain mandarin oils [143]. It has to be highlighted that the preliminary LC separation, which reduces mutual component interference, greatly simpli es MS identi cation. [Pg.221]

The circular separator with scraping at two separation steps can be considered for diameters greater than 6 m and therefore flow rates of at least 75 to 100 m h h Building a "preliminary oil removal well" outside simplifies conscruotion for oil separator diameters of 4 to 6 m but requires a sunk pump to extract the sludge from the well. [Pg.76]

This purification process is the intermediate phase between preliminary oil removal (API or lamella separators) and biological purification. [Pg.80]

This is an analysis frequently conducted on oil lubricants. Generally, the additive is known and its concentration can be followed by direct comparison of the oil with additive and the base stock. For example, concentrations of a few ppm of dithiophosphates or phenols are obtained with an interferometer. However, additive oils today contain a large number of products their identification or their analysis by IR spectrometry most often requires preliminary separation, either by dialysis or by liquid phase chromatography. [Pg.62]

Whilst the solution is still hot, add dilute hydrochloric acid until the stirred solution is just acid to litmus, and then distil off as much ethanol as possible, using the water-bath. Now add more dilute hydrochloric acid to the residual hot solution until it is just acid to methyl-orange. The 5,5-dimethyl-cyclohexan-1,3-dione separates as an oil which solidifies on cooling. Filter the product at the pump, wash it with ice-cold water, and dry it in a desiccator. Yield of the pale cream-coloured crystals, 12 g. m.p. 136-145 (preliminary softening). [Pg.278]

In the feed pretreatment section oil and water are removed from the recovered or converted CCI2F2. The reactor type will be a multi-tubular fixed bed reactor because of the exothermic reaction (standard heat of reaction -150 kJ/mol). After the reactor the acids are selectively removed and collected as products of the reaction. In the light removal section the CFCs are condensed and the excess hydrogen is separated and recycled. The product CH2F2 is separated from the waste such as other CFCs produced and unconverted CCI2F2. The waste will be catalytically converted or incinerated. A preliminary process design has shown that such a CFC-destruction process would be both technically and economically feasible. [Pg.377]

Single-stage flash distillation processes are used to make a coarse separation of the light components in a feed often as a preliminary step before a multicomponent distillation column, as in the distillation of crude oil. [Pg.499]

Water may be found in the crude either in an emulsified form or in large droplets. The quantity is generally limited by pipeline companies and by refiners, and steps are normally taken at the wellhead to reduce the water content as low as possible. However, after a spill, water can be introduced by climatic conditions, and the relevant tests (ASTM D96, D954, D1796 IP, 2004) are regarded as important in crude oil analyses. Prior to analyses, it is often necessary to separate the water from a crude oil sample, and this is usually carried out by one of the procedures described in the preliminary distillation of crude petroleum (IP 24). Overall, there are several methods that can be employed for organic semivolatile sample preparation and cleanup procedures (Table 6.4). [Pg.165]

In an automatic instrument developed by Lidzey and Stockwell [19] for the analysis of ftirftiraldehyde in gas oil, a preliminary separation is performed on a GC column coupled to a specific colorimetric reagent in a continuously flowing hquid stream. A back-flushing... [Pg.109]

The work presented here is essentially a preliminary study of the solubilization of oil in simple binary aqueous systems which can be used as model systems for microemulsions. Still, it was demonstrated that the use of phase separation to recover the oil... [Pg.42]

Full-scale separation/washing and bioslurry reactor operations have been used to treat creosote-contaminated soil at the former Southeastern Wood Preserving Site at Canton, Mississippi (Jerger et al., 1994 Woodhull Jerger, 1994). Here, an estimated 10 500 yd3 of soil and sludge were excavated from various process areas, stabilized with kiln dust and stockpiled for subsequent treatment. Based on the results of preliminary bench studies, four 680 000 liter reactors were eventually established to handle 7050 yd3 of the screened (200-mesh) soil fraction at a solids content of 20-25%. Other oil fractions and waters were handled separately (data and costs not reported). [Pg.170]

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